201132851 六、發明說明： 【發明所屬之技術領域】 本發明相關於機械工程，並且可被用來將來自各種不 同來源包括太陽、內燃機或外燃機、高溫燃料槽（fuel cell)、地熱等的熱有效地轉換成流體動力。 【先前技術】. 美國專利第5 57,964號中所揭示的裝置可實施將熱轉 換成流體動力的方法。此方法包含在氣體壓縮下將工作液 體栗啣至液氣積蓄器（hydropneumatic accumulator)(下 文稱爲積蓄器）內，而氣體膨脹在液體從積蓄器被排出之 下發生，並且對氣體供應熱及從氣體移除熱被實施以使得 膨脹期間的平均氣體溫度應高於壓縮期間的平均氣體溫度 〇 此方法係藉著包含至少兩個液氣積蓄器（上述前案中 稱爲「第一及第二液體槽」）的裝置而被實施。在每一個 積蓄器中，與液體供應及吸取機構連通的液體貯器是藉著 可移動的分隔件而與和加熱及冷卻機構連通的氣體貯器隔 開，其中加熱及冷卻機構被建構成可加熱及冷卻進來的氣 體。加熱及冷卻機構包含氣體接收器（gas receivers)( 上述前案中稱爲「第一及第二氣體容器」），而氣體接收 器的每一個與各別（第一或第二）積蓄器的氣體貯器連通 ，並且加熱及冷卻機構包含在接收器內的氣體加熱及冷卻 機構（上述前案中分別稱爲「第一及第二加熱及冷卻機構 -5- 201132851 j)、及被建構成可使氣體冷卻及加熱在接收器中交替進 行的控制系統。液體供應及吸取機構包含液壓泵、液壓馬 達、及閥。 熱是從熱的熱傳遞媒質經由加熱用熱交換器的壁部而 被供應至接收器內的氣體，而加熱用熱交換器被放置在接 收器的外部且將熱經由接收器的壁部而傳遞至氣體，或是 被放置在接收器的內部以將熱經由其本身的強固壁部而傳 遞至氣體。所提出的是使用例如內燃機的排氣成爲熱的熱 傳遞媒質。 來自接收器內的氣體的熱係直接經由接收器的壁部或 是經由放置在接收器內部的分開的冷卻用熱交換器的強固 壁部而被抽取至外部的冷卻用熱傳遞媒質。所提出的是使 用周圍空氣或水成爲冷卻用的熱傳遞媒質》 從熱供應切換至熱移除以及切換回熱供應是藉著使用 閥來關斷熱的熱傳遞媒質流及打開冷卻用的熱傳遞媒質流 且反之亦然而實施。 每一積蓄器與其接收器及加熱及冷卻機構爲分開的將 熱轉換成流體動力的轉換器。不同積蓄器的氣體貯器不連 通’而液體貯器則是經由分開的閥而連接於液體供應及吸 取機構。爲減少輸入及輸出流於該裝置內的波動（pulsation )，兩個或多於兩個的此類轉換器被使用，以使得將液體 泵唧至一個轉換器的積蓄器內相應於液體從另一個轉換器 的積蓄器被排出。 在此類的每一個轉換器內，前述方法是成爲循環性過 -6 - 201132851 程而被實施，此循環性過程包含四個連續的階段： -在氣體壓縮及氣體從積蓄器被排出至接收器內之下 ，以及在熱從接收器內的氣體被移除至外部的冷卻用熱傳 遞媒質之下，將工作流體從液體供應及吸取機構泵啷至積 蓄器內， -藉著從例如熱的熱傳遞媒質供應熱至氣體而將接收 器內的氣體等體積（isochoric)加熱， -在氣體從接收器被排出至積蓄器內之下，在液體從 積蓄器被排出至液體供應及吸取機構內之下，以及在從例 如熱的熱傳遞媒質繼續供應熱至接收器內的氣體之下，進 行氣體膨脹， -藉著將熱從接收器內的氣體移除至外部的冷卻用熱 傳遞媒質而將氣體等體積冷卻。 由於在等體積加熱及隨後的膨脹階段中對氣體的熱供 應以及在等體積冷卻及隨後的壓縮階段中從氣體的熱移除 ，膨脹期間的氣體的平均溫度（且因此平均壓力）比在壓 縮期間高，因此氣體膨脹功（gas expansion work )超過氣 體壓縮功（gas compression work )。結果，熱的一些部份 被轉換成爲額外的流體動力。 但是，氣體的循環性加熱及冷卻發生在同一氣體接收 器的體積內，此表示不只是循環性加熱及冷卻氣體，並且 也循環性加熱及冷卻熱交換器以及接收器的壁部。高壓（ 數百巴（bar ))的氣體與低壓（對於排氣而言低至數巴 )的熱交換媒質之間有熱交換。具有相關強度的熱交換器 201132851 以及接收器的壁部很龐大，並且其熱容量（thermal capacity )顯著高於（至少數十倍）接收器內的氣體的熱容量。具 有相關強度的熱交換器以及接收器的壁部的熱容量大幅高 於（數百及數千倍）大氣空氣及每秒被泵啷通過熱交換器 的排氣的熱容量。 結果，裝置的熱慣性（thermal inertia )高，而氣體冷 卻及加熱率低，此降低操作速率及裝置的平均功率密度（ average power density)，且因此爲所提出的方案的第一 個顯著缺點。接收器內的氣體加熱及冷卻由於氣體熱傳導 及自然對流而發生，此也降低加熱及冷卻速率及相關的比 功率（specific power)。 在此情況中，外部熱源的大部份的熱耗費在加熱於循 環的先前階段中被冷卻的龐大的熱交換器及接收器的壁部 而非用在轉換成流體動力。在氣體膨脹完成時，積蓄在熱 交換器中的熱被傳遞至冷卻用熱傳遞媒質及被釋放。因此 ，熱利用效率顯然低，此爲所提出的方案的第二個並且也 是最實質的缺點。上開前案所提出的使用在接收器之一的 冷卻期間從其移除的熱來加熱另一接收器所容許減少的熱 損失不超過50%。 另外的熱損失發生在經加熱的氣體流進入積蓄器時， 此時氣體吹送經過積蓄器的氣體貯器的壁部而快速地將熱 給予這些壁部。 也應注意在所提出的方案中，增加氣體循環的熱力學 效率（thermodynamic efficiency)與增加將外部熱源的熱 201132851 轉換成流體動力的槪括效率首要地不相容。企圖增加氣體 循環效率，上開前案建議將接收器內的氣體加熱’直到接 收器內的氣體溫度趨近熱的熱傳遞媒質的溫度。類似地’ 上開前案提出將接收器內的氣體冷卻，直到其溫度與周圍 空氣的溫度或另一冷卻用熱傳遞媒質的溫度相等。但是， 當熱交換器的溫度趨近熱的熱傳遞媒質的溫度時，從熱傳 遞媒質移除至熱交換器的熱的部份傾向零。因此，雖然氣 體循環的熱力學效率成長，但是外部熱源的熱轉換成流體 動力的效率降得甚至更低。速率及平均功率也降低，因爲 接收器內溫度相等化的過程爲漸近式的（asymptotic)。 接收器及熱交換器的本體在高壓下的循環性加熱及冷 卻加速其疲勞破壞且降低所提出的裝置的可靠性及安全性 。另外，必須藉著閥來切換熱的熱傳遞媒質流也降低裝置 的可靠性，特別是在使用結合高溫（高至800°C至900°C ) 及化學侵略性（chemical aggressive)的內燃機排氣時， 切換排氣流的閥的故障可能導致接收器內氣體的危險的不 受控制的過熱且伴隨有增加超過最大可容許位準的壓为， 或是在堵塞的排氣導管的情況中導致內燃機的故障。 因此，低的熱轉換成流體動力的效率及轉換率、低的 比功率、及低的可靠性爲所提出的方案的主要缺點。所:胃 出的方案的另一實質缺點爲在熱的熱傳遞媒質流的暫時性 停止運轉或減少期間不可能蓄積熱及產生流體動力。 【發明內容】 -9 - 201132851 發明本質 本發明的目的爲增加將熱轉換成流體動力的效率及速 率。 本發明的另一目的爲增加將熱轉換成流體動力的裝置 的功率密度及可靠性。 本發明的另一目的爲確保在熱供應功率的暫時性停止 運轉或降低期間熱儲存及轉換成流體動力的可能性。 方法 所提出以用來達成這些目的的將熱轉換成流體動力的 方法包含將工作液體泵唧至至少一個液氣積蓄器（下文稱 爲積蓄器）的流體貯器內，而使氣體壓縮發生在此至少一 個積蓄器的氣體貯器內，氣體膨脹則在流體從另外至少一 個積蓄器的流體貯器被排出之下發生在此另外至少一個積 蓄器的氣體貯器內，並且對氣體的熱供應及從氣體的熱移 除被實施以使得膨脹期間的平均氣體溫度高於壓縮期間的 平均氣體溫度。 藉著確保在使用至少兩個積蓄器之下，且在氣體經由 較熱的熱交換器及另一較冷的熱交換器在不同積蓄器之間 被傳遞之下，熱是藉著將氣體傳遞通過較熱的熱交換器而 被供應至氣體，並且熱是藉著將氣體傳遞通過另一較冷的 熱交換器而從氣體被移除，可達成上述目的。 爲將熱交換器保持較熱，此熱交換器被帶至與熱源熱 接觸（藉著熱傳導、輻射、或藉由加熱用的熱傳遞媒質流 -10 - 201132851 的熱傳遞）。爲將熱交換器保持較冷，此熱交換器被帶至 與冷卻用的熱傳遞媒質熱接觸。由於膨脹期間的平均氣體 溫度比壓縮期間的平均氣體溫度高（且因此平均氣體壓力 也高）的此事實，氣體膨脹功（gas expansion work)超過氣 體壓縮功（gas compression work)。結果，從熱源經由熱 交換器及氣體流被運載至冷卻用的熱傳遞媒質的熱的一些 部份被轉換成額外的流體動力，其可被用來實施機械工作 。爲泵啷工作液體及使用藉由較熱氣體排出液體而獲得的 額外流體動力，液體供應及吸取機構被使用，而其可包含 液壓泵及馬達或液體壓力變換器（下文稱爲液壓變換器（ hydraulic transformer))。 由於不同積蓄器之間經由熱交換器的氣體傳遞，因此 只有被傳遞的氣體而非龐大的熱交換器承受循環性的加熱 及冷卻》此導致顯著較低的熱損失及顯著增加的熱轉換成 流體動力的轉換效率。 流動通過熱交換器的氣體的強制對流確保其高加熱及 冷卻率，此容許以高轉換率及特定功率將外部熱源的熱轉 換成流體動力。 消除在高壓下的熱交換器及加熱及冷卻機構的其他元 件的循環性加熱及冷卻可增加這些組件將熱轉換成流體動 力的可靠性及安全性。 積蓄在較熱的熱交換器內的熱不被釋放，而可在外部 熱源的功率的暫時停止運轉或降低期間被用來轉換成流體 動力。 -11 - 201132851 爲減小積蓄器的氣體貯器的壁部被經加熱或經冷卻的 氣體流吹送通過時的熱損失，至少一個積蓄器的氣體貯器 的壁部被保持較冷，且氣體經由較冷的熱交換器而被傳遞 至此氣體貯器內，而另一個積蓄器的氣體貯器的壁部被保 持較熱，且氣體經由較熱的熱交換器而被傳遞至此氣體貯 器內。 爲減小由積蓄器內的氣體與液體的溫度差所造成的經 由積蓄器分隔件的氣體熱損失，至少一個積蓄器的液體貯 器的壁部及在此液體貯器內的工作液體被保持較冷，並且 至少一個其他積蓄器的液體貯器的壁部及在此液體貯器內 的工作液體被保持較熱。 爲防止工作液體流所伴隨的熱損失，本發明提供當較 熱（或較冷）工作液體被泵啷及排出時液體流的熱絕緣及 熱再生。 對於熱再生，從至少一個積蓄器被排出的工作液體通 過再生液體熱交換器。當工作液體被泵唧至此積蓄器內時 ，工作液體於相反方向通過同一再生液體熱交換器。 對於液體流的熱絕緣，較熱的工作液體是藉著至少一 個可移動的熱絕緣體而與較冷的工作液體隔開。 對於在積蓄器之間有增大的溫度差之下的操作，一種 工作液體被用在較冷的液體貯器中，另一種工作液體被用 在較熱的液體貯器中，而這兩種不同的工作液體是由至少 一個可移動的分隔件隔開。此可移動的分隔件也可爲可移 動的熱絕緣體，例如爲由具有低的熱傳導係數的材料（聚 -12- 201132851 合物或陶瓷）製成的活塞，或爲塗鍍有開放胞（open-cell )發泡彈性體的彈性分隔件。 高溫有機（例如以二苯基（diphenyl)或二苯基氧化物 (diphenyloxide )爲基礎）或砂-有機（silicon-organic)(例 如以一甲基砂氧焼（dimethylsiloxane)爲基礎）工作液體 的使用容許將較熱的積蓄器及其內的工作液體的溫度保持 於3 00°C至4〇〇°C。無機工作液體（例如熔融錫或其他金屬 )的使用容許將最大溫度提高上至積蓄器壁部的材料的溫 度應力極限（temperature stress limit)。 較熱積蓄器及其內的工作液體的增大的溫度增加熱轉 換成流體動力的轉換效率，特別是當以前述方式消除液體 流所伴隨的熱損失時。 在高壓下的積蓄器的強固外殻的穩定溫度情況也增加 積蓄器將熱轉換成流體動力的可靠性及安全性。爲使氣體 壓縮過程趨近等溫（isothermal )過程，至少三個積蓄器 被使用，而在此至少三個積蓄器中的至少兩個積蓄器內的 氣體貯器的壁部被保持較冷，並且氣體經由較冷的熱交換 器而在壓縮之下在此至少兩個積蓄器之間被傳遞。 爲使氣體膨脹過程趨近等溫過程，至少三個積蓄器被 使用，而在此至少三個積蓄器中的至少兩個積蓄器內的氣 體貯器的壁部被保持較熱，並且氣體經由較熱的熱交換器 而在膨脹之下在此至少兩個積蓄器之間被傳遞。 爲將最大氣體溫度增加至至少一個積蓄器內的工作液 體或分隔件的最大可容許溫度以上，氣體貯器的壁部是藉 -13- 201132851 著隔熱（thermal protection )而與經加熱的氣體流隔開。 爲使至少一個積蓄器的氣體貯器內的氣體壓縮或膨脹 過程較爲接近等溫過程及進一步增加熱轉換成流體動力的 效率，使用氣體循環泵（下文爲簡潔起見稱爲氣體鼓風機 (gas blower))以產生強制氣體對流。 外部氣體鼓風機及在積蓄器內部（在其殻體內或在氣 體貯器內）實施的氣體鼓風機二者均可被使用。 爲更佳地趨近等溫性，強制對流是藉著利用氣體鼓風 機將氣體傳遞通過至少一個熱交換器而產生，而使氣體從 至少一個積蓄器的氣體貯器被抽出且使氣體返回至同一氣 體貯器內。較佳的是爲減小在氣體管線內的加熱及冷卻損 失，來自此氣體貯器的氣體應經由一個氣體管線被抽出， 而經由另一個氣體管線返回。 氣體鼓風機可經由驅動器的軸件或另一運動連桿（ kinematic link)而被電馬達、液壓馬達、或其他馬達致動 ，而驅動器的軸件或運動連桿設置有防止被壓縮的氣體滲 漏的密封件。爲減小於密封件的滲漏及摩擦損失，氣體鼓 風機驅動器的運動連桿是由以接近的液體壓力（與氣體鼓 風機內的氣體壓力的差異較佳地不大於數巴（bar))工 作的液壓馬達致動。較佳的是當液體經由此液壓馬達而被 泵啷至積蓄器中的至少一個積蓄器的液體貯器內或從此液 體貯器被排出時，液壓馬達應由在此液壓馬達與此液體貯 器之間流動的液體致動。 爲增加熱力學效率（thermodynamic efficiency) ’特 -14 - 201132851 別是在壓縮或膨脹接近等溫壓縮或膨脹時’轉換是成爲具 有氣體熱再生的循環而被實施，其中至少於一個階段，熱 在氣體冷卻之下從氣體被移除’並且至少於一個階段，熱 在氣體加熱之下被供應至氣體’而在冷卻階段從氣體移除 的熱的一些部份被用來在加熱階段供應至氣體。爲此目的 ，熱在冷卻階段從氣體被移除至再生熱交換器’並且熱在 加熱階段首先從再生熱交換器且然後從外部熱源被供應至 氣體。 當使用由高溫的熱源例如高溫燃料槽、太陽的熱、或 另一輻射能量源所給予的熱時，使用分開的再生熱交換器 較佳。於氣體冷卻階段，氣體首先於冷卻方向通過分開的 再生熱交換器，然後通過較冷的熱交換器，而於氣體加熱 階段，氣體首先於較佳的是與冷卻方向相反的加熱方向通 過再生熱交換器，然後通過較熱的熱交換器。 當熱是藉著在熱移除之後被釋放的熱的熱傳遞媒質（ 例如排氣）而從熱源被傳遞時，逆流式（counterflow )的 較熱的熱交換器被使用以增加效率》氣體在熱供應期間於 與熱的熱傳遞媒質流的方向相反的方向被傳遞通過逆流式 的較熱的熱交換器，使得熱從離開熱交換器的熱傳遞媒質 被供應至進入熱交換器的氣體，而熱從進入熱交換器的熱 傳遞媒質被供應至離開熱交換器的氣體。此確保熱的熱傳 遞媒質（例如，燃料燃燒的終端產品的輸出流或水液流） 的較高的氣體加熱以及冷卻率。較佳的是此同一逆流式熱 交換器（或其一部份）應被使用成爲再生熱交換器，其中 -15- 201132851 氣體在冷卻期間於一個方向通過逆流式熱交換器（或其一 部份），且在加熱期間於相反方向通過逆流式熱交換器（ 或其一部份）。 於增大的熱再生程度，包含兩個等溫階段及兩個等壓 (isobaric)階段（或是在「溫度-熵（entropy)」座標中等 距離的兩個其他階段，例如等體積（isochoric )階段）的 氣體循環趨近廣義的卡諾循環（generalized Carnot cycle )，其容許熱以最大的熱力學效率轉換成氣體功（gas work )° 爲減小液壓機械（hydromechanical)損失，在被傳遞 通過液壓機械裝置的期間曝露於大幅的壓力改變的液體部 份被減少。爲此目的，氣體是藉著將液體泵啷至至少一個 積蓄器的液體貯器內且將液體從至少另外一個積蓄器的液 體貯器排出而在積蓄器的氣體貯器之間被傳遞。液體流產 生在這些積蓄器的液體貯器之間成爲使得在此液體流內的 液體的任何部份之間的壓力差不超過液體被泵啷所至的液 體貯器內的液體壓力的30%，較佳地此壓力差應不超過該 液體壓力的5%。 在傳統積蓄器中，每一個氣體貯器相應於一個液體貯 器，而二者的壓力差爲相當小的値，其只與活塞分隔件行 進的摩擦或彈性分隔件的變形有關。在這些積蓄器之間的 液體流是藉著積蓄器間液體傳遞的液壓機械機構（例如液 體泵或液壓變換器）而產生，其中液壓機械機構克服所具 有的氣體貯器經由熱交換器而連通的積蓄器的液體貯器之 -16- 201132851 間的壓力差。 通過具有經由熱交換器而連通的氣體貯器的積蓄器的 液體貯器之間的液體流的不同部份之間的壓力差是由熱交 換及連通管線（氣體及液體管線）的阻抗以及由積蓄器間 液體傳遞的液壓機械機構的效率所決定。與積蓄器內液體 的總壓力相比，此壓力差相當小（較佳地不超過數巴）。 因此，與積蓄器間液體傳遞的液壓機械機構的滲漏及摩擦 有關的損失也相當小。 液壓機械機構可包含流體泵，其經由驅動器的軸件或 另一運動連桿而被電馬達、液壓馬達、或其他馬達致動， 而驅動器的軸件或運動連桿設置有防止液體滲漏的密封件 。爲減小於密封件的滲漏及摩擦損失，積蓄器之間的此液 體流較佳地是藉著具有至少三個液體通口的液壓變換器而 產生。爲產生積蓄器間液體流，上述至少三個液體通口中 的兩個液體通口與各別積蓄器的液體通口連接，並且液壓 變換器是由流動通過液壓變換器的至少另外一個通口的另 一液體流致動。較佳的是此另一液體流應爲從積蓄器（進 入此積蓄器的氣體將液體從其排出）進入液壓機械機構的 液體流與離開液壓變換器而至積蓄器（進入此積蓄器的液 體將氣體從其排出）內的液體流之間的差動液體流（ differential liquid flow)。 可使用不同的液壓變換器，包括具有分開而在運動學 上（kinematically)互連或是具有整合的泵及液壓馬達（ 包括轉子液壓馬達及線性液壓馬達二者）的液壓變換器， -17- 201132851 例如相位調節的（phase-regulated)液壓變換器，宜中每 —缸筒在循環的一個部份的期間作用成爲馬達，而在另一 個部份的期間作用成爲泵。 就小型化而言，較佳的是使用至少一個結合液氣積蓄 器及液壓變換器的功能的積蓄器。此種積蓄器包含至少兩 個液體貯器，而此至少兩個液體貯器是藉著—個共同的活 塞分隔件而與一個氣體貯器隔開。這些液體貯器具有獨立 的液體通口並且互相隔開’此容許在這些液體貯器內保持 不同壓力’使得在分隔件上的液體的總壓力的力與在分隔 件上的氣體壓力的力平衡。爲產生前述的積蓄器間的液體 流，此積蓄器的至少一個液體貯器內的液體的壓力被保持 在此同一積蓄器的氣體貯器內的氣體壓力之上，而此積蓄 器的至少另外一個液體貯器內的液體的壓力被保持在該氣 體壓力之下。與至少另外一個積蓄器的液體貯器連接的這 些液體貯器中的至少一個參與該積蓄器間液體流，而同一 積蓄器的至少另外一個液體貯器被用來依據氣體傳遞方向 而保持液體壓力的比例。參與積蓄器間液體傳遞的液體貯 器內的壓力藉著閥而相對於氣體壓力被升高或降低至足以 產生液體流。爲此目的，未涉入積蓄器間液體傳遞的液體 貯器內的壓力則藉著閥而依據保持活塞分隔件上的壓力的 力平衡所必要者被降低或升高。當氣體被傳遞至此積蓄器 的氣體貯器時，液體流從此積蓄器的液體貯器中的至少一 個產生至另一積蓄器，以將此液體貯器內的壓力保持於比 此氣體貯器內的氣體壓力高，而同一積蓄器的至少另外一 -18- 201132851 個液體貯器內的壓力被保持於比該氣體壓力低。當氣體從 此積蓄器的氣體貯器被傳遞時，液體流從另一積蓄器產生 至此積蓄器的液體貯器中的至少一個，以將此液體貯器內 的壓力保持於比此氣體貯器內的氣體壓力低，而同一積蓄 器的至少另外一個液體貯器內的壓力被保持於比該氣體壓 力高。 本發明提供使通過液壓變換器及必要的閥的液體流直 接產生在不同積蓄器的液體貯器之間，或是經由中間的液 體緩衝器以移動液體緩衝器的可移動的分隔件或熱絕緣體 〇 爲進一步減小液壓機械損失，被排出的工作液體的吸 取及其泵唧是藉著液體供應及吸取機構而被實施，而此液 體供應及吸取機構包含具有第一壓力的管線及具有第二壓 力的管線。第一及第二壓力均被保持於高壓（較佳地爲數 十或數百巴），而第二壓力比第一壓力高。轉換是成爲循 環而被實施，此循環包含在具有較冷的氣體貯器的積蓄器 內的氣體壓縮階段、氣體從具有較冷的氣體貯器的積蓄器 經由較熱的熱交換器被傳遞至具有較熱的氣體貯器的積蓄 器內的氣體傳遞階段、在具有較熱的氣體貯器的積蓄器內 的氣體膨脹階段、及氣體從具有較熱的氣體貯器的積蓄器 經由較冷的熱交換器被傳遞至具有較冷的氣體貯器的積蓄 器的氣體傳遞階段。 來自具有較熱的氣體貯器的積蓄器的氣體是在積蓄器 內的工作液體壓力低於第一壓力之下被傳遞至具有較冷的 -19- 201132851 氣體貯器的積蓄器內。從具有第一壓力的管線至 的氣體貯器的積蓄器的液體貯器的工作液體流被 前述的液壓變換器，而液壓變換器產生從具有較 貯器的積蓄器至具有較熱的氣體貯器的積蓄器的 液體流。 來自具有較冷的氣體貯器的積蓄器的氣體是 內的工作液體壓力高於第二壓力之下被傳遞至具 氣體貯器的積蓄器內。從具有較熱的氣體貯器的 液體貯器至具有第二壓力的管線的工作液體流被 前述的液壓變換器，而液壓變換器產生從具有較 貯器的積蓄器至具有較冷的氣體貯器的積蓄器的 液體流。 在具有較冷的氣體貯器的積蓄器（至少一個 體是藉著將工作液體從也連接於具有第一壓力的 有第二壓力的管線的液壓變換器泵啷至此具有較 貯器的積蓄器的液體貯器內而被壓縮。此液壓變 著將液體流從具有第二壓力的管線引導通過液壓 被致動。在氣體壓縮期間，從液壓變換器泵唧至 器內的液體的壓力是藉著提高從第二管線流至液 的液體的體積流量（volumetric flow rate)與從 器流至該液體貯器的液體的體積流量之間的比而 在具有較熱的氣體貯器的積蓄器（至少一個 體膨脹是藉著產生從此具有較熱的氣體貯器的積 體貯器排出至也連接於具有第一壓力的管線及具 具有較熱 引導通過 冷的氣體 上述工作 在積蓄器 有較熱的 積蓄器的 引導通過 熱的氣體 上述工作 )內的氣 管線及具 冷的氣體 換器是藉 變換器而 該液體貯 壓變換器 液壓變換 被升高。 )內的氣 蓄器的液 有第二壓 -20- 201132851 力的管線的液壓變換器的工作液體流而被致動。此工作液 體流致動液壓變換器而產生從液壓變換器至具有第二壓力 的管線的工作液體流。在氣體膨脹期間，從該液體貯器排 出至液壓變換器內的液體的壓力是藉著減小從液壓變換器 流至第二管線的液體的體積流量與從該液體貯器流至液壓 變換器的液體的體積流量之間的比而被降低。 因此，由於每一轉換循環的結果，工作液體的一些部 份從具有第一壓力的管線被傳遞至具有較高的第二壓力的 管線。液壓變換器的滑動密封件在差壓（differential pressure )而非全壓力之下工作，此減小滲漏及摩擦的損失。 藉由前述的液體至具有第二壓力的管線的傳遞而接收 的流體動力可被用於連接在具有第一壓力的管線與具有第 二壓力的管線之間的負載。爲擴展使用所獲得的流體動力 的可能性’所提出的方案爲利用液壓變換器，其中此液壓 變換器的兩個通口被連接於具有第一壓力的管線及具有第 =壓力的管線’並且兩個另外的通口被連接於具有高及低 輸出壓力的管線。因此，壓力解耦 (pressure decoupling )被實施’而可藉著選擇上述管線的第一及第二壓力而使 氣體循環的效率最佳化，並且可藉著選擇高及低輸出壓力 而使負載體系（load regime)最佳化。 裝置 法可藉著一種將外部熱源的熱轉換成流體動 Λ的I裝置而被實施，而此裝置包含至少兩個液氣積蓄器， -21 - 201132851 其中與液體供應及吸取機構連通的此至少兩個液氣積蓄器 的每一個的液體貯器是藉著可移動的分隔件而與和加熱及 冷卻機構連通的氣體貯器隔開’而加熱及冷卻機構被建構 成可加熱及冷卻流入的氣體。加熱及冷卻機構包含至少兩 個氣體熱交換器’此至少兩個氣體熱交換器被安裝成可將 氣體經由此至少兩個氣體熱交換器而在不同積蓄器的氣體 貯器之間傳遞’而加熱及冷卻機構被建構成可將這些熱交 換器中的至少一個熱交換器保持較冷，並且將至少一個另 外的熱交換器保持較熱。 至少一個熱交換器被建構成可從外部熱源將熱供應至 氣體。至少一個熱交換器被建構成可將熱從氣體移除至冷 卻用的熱傳遞媒質。以下在工作裝置的敘述中，第一類型 的熱交換器被稱爲較熱的熱交換器，而第二類型的熱交換 器被稱爲較冷的熱交換器。在類似情況中，被建構成可將 熱從氣體移除且可將移除的熱供應至氣體的熱交換器被稱 爲再生（regenerating)熱交換器。 爲消除積蓄器的氣體貯器的壁部的循環性加熱及冷卻 的熱損失，所提出的實施例爲其中加熱及冷卻機構被建構 成可將至少一個積蓄器的氣體貯器的壁部保持較冷，且將 氣體經由較冷的熱交換器而傳遞至此氣體貯器內，而可將 至少另外一個積蓄器的氣體貯器的壁部保持較熱，且將氣 體經由較熱的熱交換器而傳遞至此氣體貯器內。 爲消除經由分隔件的熱損失，所提出的實施例爲其中 加熱及冷卻機構被建構成可將至少一個積蓄器的液體貯器 -22- 201132851 的壁部及在此液體貯器內的工作液體保持較冷，而可將至 少另外一個積蓄器的液體貯器的壁部及在此液體貯器內的 工作液體保持較熱。 爲在工作液體熱的再生之下實施上述方法，液體供應 及吸取機構包含至少一個液體再生熱交換器。此至少一個 液體再生熱交換器與至少一個積蓄器的液體貯器連接，且 被建構成可在液體從此積蓄器被排出通過液體再生熱交換 器的期間從液體移除熱，並且在液體被泵唧通過液體再生 熱交換器而至此積蓄器內的期間將移除的熱供應至液體。 爲在使工作液體的較熱部份與較冷部份熱絕緣之下實 施上述方法，液體供應及吸取機構包含至少一個液體緩衝 器（liquid buffer )，而此至少一個液體緩衝器包含由可 移動的熱絕緣體隔開的兩個液體貯器。 爲在不同積蓄器中使用不同工作液體以實施上述方法 ，液體供應及吸取機構包含至少一個液體緩衝器，而此至 少一個液體緩衝器包含由可移動的分隔件隔開的兩個可變 體積的貯器。 上述液體緩衝器的每一個液體貯器被安裝成可與至少 一個積蓄器的液體貯器連通。 爲減小裝置的質量及尺寸以及氣體連通管線的合計內 部體積，至少一個氣體熱交換器被建構在例如積蓄器的殻 體內成爲此積蓄器的氣體通口，而可將熱供應至氣體或將 熱從氣體移除（較佳的是成爲氣體接觸表面的面積與體積 之間具有增大的比的氣體通口）。由於去除了兩個中間通 -23- 201132851 口及氣體管線，因此氣體傳遞通過此熱交換器的期間的氣 體動態損耗也被減小。 爲在使氣體壓縮過程較爲趨近等溫過程之下實施上述 方法，所提出的裝匱實施例包含至少三個積蓄器，而加熱 及冷卻機構被建構成可將這些積蓄器中的至少兩個積蓄器 的氣體貯器的壁部保持較冷，並且將氣體經由較冷的氣體 熱交換器而在此至少兩個積蓄器之間傳遞。 爲在使氣體膨脹過程較爲趨近等溫過程之下實施上述 方法，所提出的裝置實施例包含至少三個積蓄器，而加熱 及冷卻機構被建構成可將至少兩個積蓄器的氣體貯器的壁 部保持較熱，並且將氣體經由較熱的氣體熱交換器而在此 至少兩個積蓄器之間傳遞。 爲減少熱損失，至少一個積蓄器設置有隔熱（thermal protection )機構，此隔熱機構被建構成可將積蓄器的氣 體貯器的壁部與進入的氣體流隔開。 當氣體被加熱至低於150°C至200°C時，爲減少分隔件 摩擦的損失及降低成本，積蓄器被建構成具有彈性分隔件 ，而隔熱機構包含與彈性分隔件連接的撓性多孔狀熱絕緣 當氣體被加熱至較高溫度時，積蓄器較佳地被建構成 具有活塞分隔件，而隔熱機構包含沿著積蓄器的氣體貯器 的圓柱形側壁安裝的可變長度的熱屏幕（thermal screen ) 、及相對於分隔件及氣體貯器底部安裝的熱屏幕。對於 3 00 °C以上的溫度，上述熱屏幕較佳地由金屬製成，而對 • 24- 201132851 於較低溫度則可由聚合物製成，例如可由有機-矽聚合物 製成。 爲在使氣體壓縮或膨脹過程較爲趨近等溫過程之下實 施上述方法，氣體加熱及冷卻機構包含至少一個氣體循環 泵（以下爲簡潔起見稱爲氣體鼓風機），其可在至少一個 積蓄器的氣體貯器內產生強制氣體對流。 爲增進等溫性，至少一個積蓄器的氣體貯器藉著至少 兩個氣體管線而與氣體加熱及冷卻機構連通，而可藉著氣 體鼓風機經由上述至少兩個氣體管線中的一個氣體管線將 氣體從氣體貯器移除，將移除的氣體傳遞通過至少一個熱 交換器，且經由另一個氣體管線而使氣體返回至同一氣體 貯器。 在就簡單性及可靠性且包含氣體鼓風機而言較佳的裝 置的實施例中，液體供應及吸取機構包含與至少一個氣體 鼓風機在運動學上連接的至少一個液壓馬達，而此液壓馬 達被安裝成可被在液壓馬達與至少一個積蓄器的液體貯器 之間的液體流致動。 爲藉由具有熱再生的循環來實施轉換方法，所提出的 裝置具有被實施成爲再生氣體熱交換器的至少一個氣體熱 交換器，亦即可在氣體於一個方向被泵啷通過此至少一個 氣體熱交換器時從氣體移除熱，且在氣體於相反方向被泵 唧通過此至少一個氣體熱交換器時將從氣體移除的熱供應 至氣體。 本發明提供對於各種不同熱源的利用。較熱的熱交換 -25- 201132851 器與熱源的熱接觸是藉著熱傳導或熱及質量傳遞（heat-and-mass transfer)，包括冷凝（condensation )熱傳遞，或是藉 著輻射熱傳遞以及這些的組合而被實施。 爲確保藉著熱及質量傳遞而與熱源熱接觸，至少一個 氣體熱交換器具有供外部熱傳遞媒質通過而可將熱從此熱 傳遞媒質供應至氣體的通道。 爲增加使用熱的熱傳遞媒質時的效率，至少一個熱交 換器被建構成爲逆流式熱交換器，亦即此逆流式熱交換器 具有供外部熱傳遞媒質通過而可將熱從此熱傳遞媒質供應 至氣體的通道，使得熱從離開熱交換器的外部熱傳遞媒質 被供應至進入熱交換器的氣體，而給離開熱交換器的氣體 的熱係供應自進入熱交換器的外部熱傳遞媒質。爲了使上 述熱交換器被使用成爲再生熱交換器，上述熱交換器具有 至少一個額外通口，以可將氣體引入熱交換器內，而加熱 及冷卻機構包含將上述的額外氣體通口與積蓄器連接的至 少一個通道且被建構成可閉鎖此通道。 爲在產生積蓄器間液體流之下實施上述方法，一種裝 置實施例被提出，其中液體供應及吸取機構包含積蓄器間 液體傳遞機構，其被實施成可在至少兩個積蓄器的液體貯 器之間產生液體流，使得在此液體流內的液體的任何部份 之間的壓力差不超過液體被泵唧所至的液體貯器內的液體 壓力的30%，較佳地此壓力差不超過該液體壓力的5%。 積蓄器間液體傳遞機構可有各種不同的實施例，包括 使用轉子及線性液體泵以及液壓馬達二者的機構，以及使 -26- 201132851 用結合泵及馬達的液壓變換器的機構。在後一種情況中， 積蓄器間液體傳遞機構包含具有至少三個液體通口的至少 一個液壓變換器，此至少一個液壓變換器被安裝成可經由 此液壓變換器的兩個通口而與至少兩個積蓄器的液體貯器 連通，並且可在液體流動通過此液壓變換器的另外至少一 個通口時在上述的至少兩個積蓄器之間產生液體流。可使 用各種不同的液壓變換器，例如具有相位控制（phase control )的旋轉軸向活塞（rotary axial-piston)液壓變換器（如 在美國專利第6,11 6,138號中），其中每一缸筒在循環的 一個部份的期間作用成爲馬達，而在循環的另一個部份的 期間作用成爲泵，或是具有數位控制的多容室線性液壓變 換器（如在美國專利第7，47 5，5 3 8號中）。在較爲小型化 的實施例中，至少一個積蓄器結合液氣積蓄器與液壓變換 器的功能，如在美國專利第5,971，027號中。此種積蓄器 包含至少兩個液體貯器，此至少兩個液體貯器是藉著一個 共同的活塞分隔件而與一個氣體貯器隔開，而積蓄器間液 體傳遞機構被建構成可在此積蓄器的液體貯器中的至少一 個與另一個積蓄器的至少一個液體貯器之間產生液體流。 爲在將液體從具有第一高壓力的管線傳遞至具有第二 高壓力的管線之下實施轉換方法，液體供應及吸取機構包 含第一及第二管線、及具有至少三個通口的液壓變換器， 其中第一及第二管線可在其內分別保持第一及第二壓力， 而液壓變換器被安裝成可在至少一個積蓄器的液體貯器內 的壓力與第一及第二管線內的第一及第二壓力不同之下， -27- 201132851 在第一及第二管線與此液體貯器之間進行液體交換。 爲在使負載壓力從上述第一及第二管線內的第一及第 二壓力解耦之下實施上述方法，液體供應及吸取機構包含 具有至少四個通口的液壓變換器，此液壓變換器被安裝成 可將兩個通口與第一及第二管線連接，及將另外兩個通口 與兩個輸出管線連接，並且可將上述兩個輸出管線內的壓 力保持成與第一及第二管線內的第一及第二壓力不同。 本發明的細節顯示在以下所給的由圖式顯示的例子中 【實施方式】 本發明的主要原理顯示在圖1中》主要原理的改良顯 示在圖2中。圖3至8顯示主要元件及部份的特定實施例 〇 根據圖1的裝置包含兩個液氣積蓄器1及2，其液體 貯器3及4與液體供應及吸取機構14連通。液體貯器3 及4藉著可移動的分隔件5及6而與氣體貯器7及8隔開 ，而氣體貯器7及8係與加熱及冷卻機構9連通。爲了氣 體的加熱及冷卻’加熱及冷卻機構9包含流動氣體熱交換 器1 0及1 1，其經由氣體管線1 2及閥1 3而與氣體貯器7 及8以及積蓄器1及2連接。熱交換器1〇係建構成可與 外部熱源熱接觸’且可將熱從熱源供應至氣體。熱交換器 11係建構成可與冷卻熱傳遞媒質熱接觸，且可將熱從氣體 移除至冷卻熱傳遞媒質。 -28- 201132851 本發明提供對於各種不同熱源的利用，包括內燃機或 外燃機、高溫燃料槽、太陽、地熱源等，以及在與較熱的 熱交換器熱接觸時進行的放熱反應的直接熱量。與熱源的 熱接觸是藉著使用熱的熱傳遞媒質的熱傳導或熱及質量傳 遞（heat-and-mass transfer)或藉著輻射熱傳遞以及這些 的組合而實施，其中熱的熱傳遞媒質例如爲內燃機（ICE)的 排氣或蒸汽渦輪機的排出蒸汽。也可用冷凝（condensation ) 熱傳遞來進行熱及質量傳遞，例如在蒸汽渦輪機的排出蒸 汽的熱的回收期間或是在使用熱管（heat pipe)時。 圖3顯示氣體熱交換器1〇(或11)的實施例，而與 此熱交換器的熱接觸是藉著熱及質量傳遞而實施。熱交換 器包含從內部軸向通道16徑向發散的內部槽溝型（slot-type) 氣體通道 15， 而 內部軸 向通道 16 除 了收集器部份 (collector part) 17外的大部份是由插塞18阻塞。氣體 的輸入及輸出是經由凸緣20 (圖中未顯示第二凸緣）的通 口 19而實施。較佳的是熱交換器1〇、11的內部通道15、 16中的合計氣體體積不應超過積蓄器的氣體貯器7、8中 的最大合計氣體體積的1〇%。對於供應自外部熱源的熱， 根據圖3的熱交換器包含螺旋狀外部通道21，而在熱交換 器1 0與外部熱源之間循環的加熱熱傳遞媒質經由外部通 口（圖中未顯示）而被泵唧通過螺旋狀外部通道21。較佳 的是熱交換器1〇應被建構及安裝成爲逆流式熱交換器， 以可將熱從加熱熱傳遞媒質供應至氣體’使得熱從離開熱 交換器10的外部熱傳遞媒質被供應至進入熱交換器10的 -29- 201132851 氣體，而給離開熱交換器10的氣體的熱是供應自進入熱 交換器10的外部熱傳遞媒質。如此，同時達成外部熱源 的熱的較完全利用以及較高程度的氣體加熱。冷卻熱傳遞 媒質被泵唧通過外部通道的熱交換器也是以類似的方式被 實施及安裝。 氣體熱交換器10被外部熱源加熱而變得較熱。氣體 熱交換器11被冷卻熱傳遞媒質冷卻而變得較冷。 對於將外部熱源的熱轉換成爲流體動力，氣體的壓縮 及膨脹與熱的供應及移除結合，使得平均氣體溫度在膨脹 期間比在壓縮期間高。下文的壓縮及膨脹意指由於在至少 —個積蓄器內的氣體貯器體積的改變所造成的氣體密度的 改變（分別爲密度的增加或減小）。 根據圖1的裝置可被用來在實施結合等壓（isobaric )、等體積（isochoric)、與接近絕熱（adiabatic)的多變（ polytropic )階段的循環（cycle )之下將熱轉換成爲流體 動力，其中上述循環例如爲顎圖（Otto )循環、布雷頓（ Brayton)循環、狄賽爾（Diesel)循環、或其他循環。在 下文中，氣體循環中的實際過程會藉著理想化的階段（例 如絕熱、等溫（isothermal )、等壓、或等體積）而被近 似地敘述。 在無氣體傳遞通過熱交換器之下的氣體密度改變（藉 著氣體膨脹或壓縮）會以增加的膨脹或壓縮率實施趨近絕 熱膨脹或壓縮的多變膨脹或壓縮。 在無氣體密度改變之下（亦即在從一個積蓄器的氣體 -30 - 201132851 排出率與至另一個積蓄器內的氣體吸取率相等之下）的通 過熱交換器（較熱的熱交換器10或較冷的熱交換器U) 的氣體傳遞會實施氣體溫度的等體積改變（分別爲加熱或 冷卻）。 在膨脹之下（亦即在氣體貯器7及8的合計氣體體積 增加之下）從一個積蓄器經由較熱的熱交換器10至另一 個積蓄器的氣體傳遞會實施帶有加熱的氣體膨脹，例如等 壓。以類似方式，帶有冷卻的氣體壓縮（例如等壓）是以 在壓縮之下從一個積蓄器經由較冷的熱交換器U至另一 個積蓄器的氣體傳遞而被實施。 所提出的將熱轉換成爲流體動力的方法不限於具有上 述的理想化階段的循環，而可應用於其中氣體膨脹功超過 氣體壓縮功的所有循環。 在根據圖1的裝置實施例中所實施的將熱轉換成流體 動力的循環的例子包含四個階段，亦即在第一積蓄器的氣 體貯器中的多變氣體壓縮的第一階段；在氣體經由較熱的 熱交換器10傳遞至另一積蓄器的期間的對氣體的熱供應 及氣體加熱的第二階段；在另一積蓄器的氣體貯器中的多 變氣體膨脹的第三階段；及在氣體經由較冷的熱交換器11 傳遞回至第一積蓄器的期間的從氣體移除熱及氣體冷卻的 第四階段。於第一階段的開始處，氣體從積蓄器2的氣體 貯器8以最大的程度被排出通過較冷的熱交換器11而至 積蓄器1的氣體貯器7內。結果，初始氣體溫度接近較冷 的熱交換器11的溫度。以液體供應及吸取機構14泵啷工 -31 - 201132851 作流體至積蓄器1的液體貯器3內，多變氣體壓縮會在氣 體壓力及溫度的增加之下於氣體貯器7內被實施。多變氣 體壓縮結束於小於較熱的熱交換器10的溫度的氣體溫度 。在第二階段期間，在將工作液體泵啷至液體貯器3內且 將工作液體從液體貯器4排出之下，藉著將氣體從氣體貯 器7經由閥13及較熱的熱交換器10而傳遞至氣體貯器8 內，熱被供應至經壓縮的氣體。熱的供應是在氣體的加熱 及膨脹之下被實施，亦即在氣體貯器7及8中的合計氣體 體積的增加之下被實施。從積蓄器2的液體貯器4被排出 至液體供應及吸取機構14內的工作流體的量大於從液體 供應及吸取機構14被泵啷至積蓄器1的液體貯器3內的 工作流體的量。較佳地，氣體傳遞被實施直到從積蓄器1 的氣體貯器7排出的爲氣體的最大排出量。於第三階段， 在液體從積蓄器2的液體貯器4被排出至液體供應及吸取 機構14內之下，進一步的氣體膨脹在積蓄器2的氣體貯 器8中被實施。此時，氣體的壓力及溫度減小。多變氣體 膨脹結束於比較熱的熱交換器10的溫度高的氣體溫度。 在第四階段期間，在將工作液體泵唧至液體貯器4內且將 工作液體從液體貯器3排出之下，藉著將氣體從氣體貯器 8經由較冷的熱交換器11及閥13而傳遞至氣體貯器7內 ，熱從膨脹的氣體被移除。熱的移除是在氣體的冷卻及壓 縮之下被實施，亦即在氣體貯器8及7內的合計氣體體積 的減小之下被實施。從積蓄器1的液體貯器3排出至液體 供應及吸取機構1 4內的工作流體的量小於從液體供應及 -32- 201132851 吸取機構14被泵啷至積蓄器2的液體貯器4內的工作流 體的量。於第二及第三階段的膨脹期間的氣體的平均溫度 及平均壓力比在第一及第四階段的壓縮期間高。因此，氣 體膨脹功超過氣體壓縮功。在第二及第三階段期間，液體 供應及吸取機構1 4以從積蓄器排出的液體所得到的流體 動力比在第一及第四階段期間用來將工作流體泵唧至積蓄 器內所費的流體動力多。結果，熱的一些部份被轉換成額 外的流體動力，其被液體供應及吸取機構1 4使用於例如 負載 '液壓馬達、或液壓缸筒中的機械工作。液體供應及 吸取機構14可有各種不同的實施例，包括分開的泵及液 壓馬達以及液壓變換器（hydraulic transformer)。 以上所述的本發明的主要原理係使用根據圖2的裝置 實施例中所包含的改良而以更高的效率被實施。 在根據圖2的裝置中，加熱及冷卻機構9包含止回閥 22，其被安裝成使得氣體被傳遞通過較冷的熱交換器11 而只至積蓄器1的氣體貯器7內，因而氣體貯器7的壁部 被保持較冷。較熱的熱交換器10被安裝成使得氣體從氣 體貯器7被傳遞通過熱交換器10而至氣體貯器8內，且 從熱交換器10被傳遞至第三積蓄器24的氣體貯器23內 ，因而將氣體貯器8及23的壁部保持較熱。 在具有三個或更多的積蓄器的其他實施例中，加熱及 壁些 的這 器在 貯而 體器 氣換 的交 器熱 蓄體 積氣 個的 兩冷 少較 至由 將經 可體 成氣。 構將遞 建且傳 被’間 可冷之 構較器 機持貯 卻保體 冷部氣 -33- 201132851 加熱及冷卻機構9也包含液體流熱交換器25及止回 閥26。熱交換器25是由來自外部熱源的熱加熱，例如藉 著熱的熱傳遞媒質》被引入積蓄器2的液體貯器4或積蓄 器24的液體貯器27、28的工作液體通過經加熱的液體熱 交換器25，因而將這些液體貯器的壁部及其內的工作液體 保持較熱。此時，積蓄器1的液體貯器3的壁部及其內的 液體保持較冷。如此，積蓄器2及24整體而言被保持較 熱，而整個積蓄器1被保持較冷。 其他實施例可包含冷卻液體熱交換器，以使工作液體 在被泵啷至具有較冷的氣體貯器壁部的積蓄器（例如圖1 、圖2中的積蓄器1)的液體貯器時被傳遞通過此冷卻液 體熱交換器。其他實施例也可包含設置有用來直接加熱或 冷卻積蓄器壁部的熱交換器的積蓄器。 在根據圖2的裝置中，液體供應及吸取機構14包含 液體再生熱交換器29及熱絕緣緩衝器（heat-insulating buffer ) 30。在其他實施例中，可只使用液體再生熱交換 器或只使用熱絕緣緩衝器。液體再生熱交換器29與兩個 較熱的積蓄器的液體貯器4、27、及28連接，而可在液體 從這些積蓄器被排出通過液體再生熱交換器29而至熱絕 緣緩衝器30內的期間將熱從液體移除，並且在液體從緩 衝器30被反向傳遞至這些積蓄器內時將移除的熱供應至 液體。工作液體在從較熱的積蓄器2或24被引導通過熱 交換器29時由於將熱從液體傳遞至熱交換器29而被冷卻 。於相反方向被引導通過同一熱交換器29而至較熱的積 -34- 201132851 蓄器2或24內的工作液體由於從熱交換器29傳遞至液體 的熱而被加熱。如此，被引至包含由可移動的熱絕緣體33 隔開的兩個可變體積的液體貯器31及32的熱絕緣液體緩 衝器3 0的工作液體的溫度被降低》高溫工作液體（例如 有機或有機-矽（organic-silicon)工作液體）的使用容許 將其溫度升高至3〇〇°C及更高的溫度。 對於在冷及熱積蓄器中使用不同的工作液體，可應用 分開的液體緩衝器，其包含由可移動的分隔件隔開的兩個 可變體積的貯器。或是，液體緩衝器30可被建構成具有 液密的可移動的熱絕緣分隔件33。 液體再生熱交換器29可有各種不同的實施例，包括 被安裝在強固外殼的內部的再生元件，以及製成爲具有高 熱容量且從其較熱部份至較冷部份有低的熱傳遞的單一元 件形式者（例如成爲長管的形式）。在根據圖4的整合實 施例中’圖2的液體再生熱交換器29與液體熱絕緣緩衝 器30在共同的強固外殻34內被實施，而強固外殼34在 其凸緣上具有液體通口 35及36。強固外殼34的內部有薄 壁狀金屬套筒37，而成爲長的中空活塞38的形式的可移 動的熱絕緣體33被可滑動地安裝在套筒37內，以分隔高 溫與低溫的可變體積的貯器3 1及3 2。在強固外殻3 4與金 屬套筒37之間的空間39中，放置有塡料40 (例如礦渣棉 (mineral wool )或發泡聚合物（foained polymer ))，以 防止充塡該空間的具有低的熱傳導係數的高溫液體的對流 。中空活塞38內部的空腔41也含有塡料40及具有低的 -35- 201132851 熱傳導係數的高溫液體。在此情況中，此液體爲經由套筒 37的孔42及中空活塞38的壁部的孔43而充塡的工作液 體。此液體提供薄套筒37及活塞38的薄壁的液體靜壓卸 載（hydrostatic unloading)。在其他實施例中，可使用由 具有低的熱傳導係數（較佳的爲小於lW/mK)的高溫材料 製成的固體隔熱插入物，例如由高溫塑膠（例如聚亞胺等 )製成者，以取代薄壁狀金屬套筒37及由金屬套筒37沿 著強固外殼34隔開的隔熱液體層。可移動的熱絕緣體33 也可由類似的具有低的熱傳導係數的固體材料製成。 高溫的可變體積的貯器32與充塡有再生元件45的液 體再生熱交換器29的流動部份44連通。在此情況中，再 生元件45的實施例爲由具有高的熱傳導係數的金屬（例 如鋁）製成的球件的形式。爲減小尺寸，再生元件45可 含有在與經過的液體熱交換的期間進行相的轉變（例如， 在從液體移除熱的期間熔化，而在熱供應至液體的期間結 晶）的材料。 在根據圖2的實施例中，氣體熱交換器10被建構成 分開的元件且被安裝在積蓄器2與積蓄器24之間，而可 將氣體從積蓄器2的較小的氣體貯器8傳遞通過熱交換器 10而至積蓄器24的較大的氣體貯器23內，因而使氣體膨 脹過程較爲趨近等溫膨脹過程。爲確保小型化及氣體傳遞 期間的壓力損失較低，根據圖5的實施例被提出，其中氣 體熱交換器10與積蓄器2被建構在同一殼體內成爲此積 蓄器的氣體通口而具有增加的熱交換表面面積。熱交換器 -36- 201132851 ίο包含供加熱的熱傳遞媒質用的外部通道21、與積蓄器2 共用的強固外殻46、及由具有高的熱傳導係數的金屬（較 佳地爲銅或鋁）製成的內部熱交換區段47。於內部熱交換 區段47中，形成有從軸向通道16徑向發散的內部槽溝型 氣體通道15，而軸向通道16除了收集器部份17外的大部 份是由插塞18阻塞。在如根據圖2的具有兩個較熱的積 蓄器的實施例中，在氣體從較冷的積蓄器1傳遞至較熱的 積蓄器2的期間，以及在氣體從較小的較熱的積蓄器2傳 遞至較大的較熱的積蓄器24的期間，氣體均被傳遞通過 此較熱的熱交換器1〇。 類似地，在其他實施例中，較冷的氣體熱交換器1 1 可與較冷的積蓄器1 一起在同一殻體內被實施。 根據圖2的加熱及冷卻機構9包含氣體鼓風機48，其 被安裝成可在較冷的積蓄器1的氣體貯器7中產生強制對 流。氣體貯器7經由至少兩個氣體管線49及50而與加熱 及冷卻機構9連通，因而可藉著氣體鼓風機48經由氣體 管線49而將氣體從氣體貯器7移去，將移去的氣體傳遞 通過較冷的流動氣體熱交換器11，及使氣體經由另一氣體 管線50而返回至同一個氣體貯器7。在具有外部熱交換器 的其他實施例中，氣體鼓風機可被放置在積蓄器的殻體內 ，並且可在沒有氣體傳遞通過外部熱交換器之下產生強制 對流，因而只由於與氣體貯器的壁部熱交換而使氣體壓縮 或膨脹較爲接近等溫過程。 根據圖2的液體供應及吸取機構1 4包含藉著軸件52 -37- 201132851 而與氣體鼓風機48在運動學上（kinematically )連接的液 壓馬達51。在其他實施例中，液壓馬達與氣體鼓風機的運 動學連接可包含供氣體鼓風機的旋轉速率增加用的齒輪箱 。液壓馬達51經由閥103而與液體管線67連接，因而可 被在液壓馬達與積蓄器1的液體貯器3之間的液體流致動 〇 在根據圖6的整合實施例中，流動氣體熱交換器11 與離心氣體鼓風機48二者均與積蓄器1 一起在同一個殼 體內被實施》氣體鼓風機48藉著軸件52而與液壓馬達51 連接。止回閥22 (圖2)未顯示在圖6中。止回閥中的一 個可被實施成爲被安裝在內部熱交換區段47的表面處的 圓盤閥（disc valve)，因而可閉鎖熱交換槽溝通道15。 另一個止回閥可被安裝在軸向通道16中。此整合實施例 增進小型化且不需氣體管線，因而降低總氣體動態阻力（ dynamic resistance ) ° 當工作液體被泵啷至積蓄器1的液體貯器3內時，工 作液體致動液壓馬達51及在運動學上與液壓馬達51連接 的氣體鼓風機48»離心氣體鼓風機48 (圖6)經由軸向通 道16從氣體貯器7吸取氣體，並且將氣體泵唧至熱交換 器11的槽溝型通道15內，而氣體從槽溝型通道15返回 至氣體貯器7內而在氣體貯器7產生強制對流。氣體與氣 體貯器7的壁部及槽溝型通道15的表面的強化的熱交換 使得此氣體貯器內的氣體壓縮過程較爲趨近等溫過程。 致動液壓馬達51的液體與由氣體鼓風機48泵嘟的氣 -38- 201132851 體具有接近的壓力及接近的溫度，此促進軸件52的密封 件的良好的操作情況。 在其他實施例中，氣體鼓風機可被安裝成可在較熱的 積蓄器的氣體貯器內產生強制對流。並且，在其他實施例 中，氣體鼓風機可在運動學上與位在較佳地充塡有液體的 高壓空腔中的電馬達連接。 根據圖2的裝置包含再生流動氣體熱交換器53，而當 氣體被傳遞通過再生熱交換器53至較冷的積蓄器1時， 熱從氣體被移去至再生熱交換器53，並且當氣體於相反方 向（亦即從較冷的積蓄器1至較熱的積蓄器2)被傳遞通 過再生熱交換器53時，從氣體移去的熱從再生熱交換器 S3被供應回至氣體。如此，氣體從較冷的積蓄器1進入再 生熱交換器53的部份變得較冷，而氣體從較熱的積蓄器2 或24進入的相反部份變得較熱。於冷卻階段，來自氣體 的熱被供應至再生熱交換器53，且然後經由較冷的熱交換 器11而被供應至冷卻熱傳遞媒質。於加熱階段，熱首先 從再生熱交換器53被供應至氣體，且然後從外部熱源經 由較熱的熱交換器10而被供應至氣體。 較佳的是再生熱交換器53內的合計氣體體積不應超 過積蓄器的氣體貯器內的最大合計氣體體積的10%。再:生 熱交換器53的熱容量超過氣體的最大合計熱容量（較佳 地不小於兩倍）。再生熱交換器的組態（長度、縱向截面 、及橫向截面）及再生熱交換器的材料的熱傳導係數被選 擇成使得從其較熱部份至其較冷部份的熱傳遞應小於從氣 -39- 201132851 體至較冷的熱交換器11中的冷卻熱傳遞媒質的熱傳遞 較佳地，小於後者熱傳遞的30% )。再生熱交換器53 有各種不同的實施例，包括安裝在強固的氣密密封外殼 內部的再生元件，以及以具有小的內部體積、高的熱容 、及低的從較熱部份至較冷部份的熱傳遞的單一元件的 式實施者。在根據圖7的特定實施例中，再生氣體熱交 器53包含強固外殻54，其具有熱絕緣插入物55，而再 元件56以螺旋狀薄片57的形式被放置在熱絕緣插入物 的內部，其中以墊片5 8決定螺旋狀薄片層之間的間隙 氣體在流動通過這些間隙時與再生元件的表面交換熱， 而取決於傳遞方向變得較冷或較熱。在此實施例中，使 金屬薄片（較佳地是由具有低的熱傳導係數的金屬製成 例如不銹鋼）。爲減小縱向熱傳導係數，金屬薄片57 有穿孔5 9，以將再生元件分開成數個區段，而在各區段 間於穿孔5 9的區域具有增大的熱阻。在其他實施例中 再生元件可由不具有穿孔的高溫塑膠製成。由高溫塑膠 陶瓷製成的隔熱或熱絕緣插入物55減少強固外殼54的 熱及冷卻的熱損失。在其他實施例中，可使用熱絕緣液 層來取代隔熱插入物55，其中液體是藉著薄金屬套筒而 再生元件內的氣體部份隔開（類似於根據圖4的液體再 熱交換器29中的隔熱液體層）。 在其他實施例中，熱交換器1 〇 (或1 1 )的一部份 被使用成爲氣體再生熱交換器53。爲此目的，額外的氣 通口形成於此種熱交換器成爲可將氣體引入熱交換器， 可 的 量 形 換 生 55 〇 因 用 > 具 之 或 加 體 與 生 可 體 而 -40- 201132851 加熱及冷卻機構包含將上述的額外氣體通口與氣體貯器23 (或氣體貯器7)連接至少一個通道，並且包含安裝成爲 可閉鎖此通道的閥。 與使壓縮及膨脹較爲趨近等溫過程結合的熱再生在液 體從積蓄器排出的期間提供將熱轉換成由氣體所實施的功 的高熱力學效率（thermodynamic efficiency )。 根據圖2的液體供應及吸取機構14包含液壓變換器 60及閥61、62、及63，而液壓變換器60及閥61、62、 及63與液體管線64至67 —起形成積蓄器間液體傳遞機 構，其可在積蓄器1、2、及24的液體貯器之間產生液體 流。 液壓變換器60具有三個液體通口 68、69、及70 *通 口 68經由閥63及103而與積蓄器1的液體貯器3連接， 而通口 69經由閥62、26、及61，液體熱絕緣緩衝器30 ’ 及再生液體熱交換器29而與積蓄器2的液體貯器4或與 積蓄器24的液體貯器27及28連接。液壓變換器60的第 三通口 70與液體管線71連接。當液體流動通過此第三通 口 70時，液體流產生在液壓變換器60的通口 68與通口 69之間，且因此而產生在與這些通口連通的積蓄器的液體 貯器之間。 根據圖2的積蓄器24如同美國專利第5,971，〇27號般 地被實施，並且結合液氣積蓄器與液壓變換器的功能。積 蓄器24具有三個通口（氣體通口 72及液體通口 73及74 )，並且包含藉著一個共同的活塞分隔件75而與一個氣 -41 - 201132851 體貯器23隔開的兩個液體貯器27及28。積蓄器間液體傳 遞機構包含閥61及管線64及65，以在積蓄器24的液體 貯器27與積蓄器2的液體貯器4之間產生液體流。液體 貯器27及28彼此隔開，此容許在二者中保持不同的壓力 ，使得在分隔件75上的液體壓力的合計力與在分隔件75 上的氣體壓力的力平衡。當氣體從積蓄器2的氣體貯器8 傳遞至氣體貯器23內時，逆向的液體流從液體貯器27產 生至積蓄器2的液體貯器4內，因而將液體貯器4內的壓 力保持成爲比氣體貯器23內的壓力高。如此，在經由閥 62 (及經由再生熱交換器29及熱絕緣緩衝器30 )而與液 壓變換器76連接的另一液體貯器28內的壓力被保持於比 在氣體貯器23中低的位準。藉著改變通過液壓變換器76 的通口 7 7、7 8、及7 9的流量之間的比，流動通過與液體 貯器28連接的通口 77的液體的壓力被改變。因此，藉著 液壓變換器76，液體貯器28中的壓力相對於氣體貯器23 中的氣體壓力被保持爲較低。由於上述的作用在分隔件75 上的力的平衡，.液體貯器27中的壓力變成相對於氣體貯 器23中的氣體壓力增加。在積蓄器2與積蓄器24之間的 相互氣體及液體傳遞率穩定之下，液體貯器27中的液體 壓力高於氣體貯器 23中的氣體壓力的此相對超額（ relative excess)的値相應於由摩擦所造成的在分隔件75 及6上的壓力降及由氣體傳遞及液體逆向傳遞發生時所經 過的氣體-液體迴路的阻抗所造成的合計壓力降的値。上 述迴路包含積蓄器1、2、及24的氣體及液體通口、氣體 -42- 201132851 熱交換器10、以及閥及管線。因爲該迴路 積蓄器2與積蓄器24之間相互氣體及液 而增大，所以對於傳遞率增大，液體貯器 體貯器23中的壓力的上述壓力超額的値 傳遞率減小，上述壓力超額的値減小。 在其他實施例中，此種具有數個液體 被使用成爲第二個較冷的積蓄器（或是例 的積蓄器2成爲唯一的較熱的積蓄器）。 氣體從此積蓄器傳遞回至較小的積蓄器內 圖1的積蓄器1內）的期間，產生從較小 貯器至此種積蓄器的一個（或數個）液體 流，以將液體貯器內的壓力保持於比氣體 此積蓄器的另一個液體貯器（或其他數個 壓力也例如藉著液壓變換器而被保持於比 氣體壓力高。結合積蓄器及液壓變換器的 液體貯器的此種整合的積蓄器實施例減少 遞的損失，並且增進裝置的小型化。在其 中，積蓄器可在一個殼體內容納數個液體 貯器。從本發明的觀點而言，此種整合實 數目等於在氣體貯器與液體貯器之間的獨 件的數目。 在氣體在熱供應自再生熱交換器53 器1〇之下在積蓄器2與積蓄器1之間傳 變換器60及閥62、63被用來在積蓄器2 上的壓力降隨著 體傳遞率的增大 2 7中相對於氣 增大，並且對於 貯器的積蓄器可 如取代根據圖1 在此情況中，在 (例如回至根據 的積蓄器的液體 貯器的逆向液體 壓力低。此時， 液體貯器）內的 其氣體貯器內的 功能的具有兩個 積蓄器間液體傳 他的整合實施例 貯器及數個氣體 施例中積蓄器的 立地移動的分隔 及較熱的熱交換 遞的期間，液壓 與積蓄器1之間 -43- 201132851 產生液體流，並且在熱從氣體被移去至再生熱交換器53 及較冷的熱交換器11之下在積蓄器24與積蓄器1之間傳 遞的期間，液壓變換器60及閥62、63被用來在積蓄器24 的液體貯器27、28與積蓄器1的液體貯器3之間產生液 體流。在氣體從氣體貯器7傳遞至氣體貯器8的期間，液 體貯器3連接於通口 68 (經由閥103、63 )，而液體貯器 4連接於通口 69 (經由閥61、26、及62、液體再生熱交 換器29、及液體熱絕緣緩衝器30)。藉著液壓變換器60 將液體貯器3內的液體壓力保持於比氣體貯器7內的氣體 壓力高的値，氣體從積蓄器1被排出至積蓄器2，並且在 差動液體流被排出通過液壓變換器60的第三通口 70、管 線7 1、及止回閥97至管線90之下，逆向液體流通過液壓 變換器60的通口 68、69而產生在積蓄器2與積蓄器1之 間。 當氣體從氣體貯器23傳遞至積蓄器1的氣體貯器7 內時，液體貯器27及28二者均與液壓變換器60的通口 69連接（經由閥61及62、液體再生熱交換器29、及液體 熱絕緣緩衝器30)。在液壓變換器60將這些液體貯器內 的液體壓力保持於比氣體貯器23內的氣體壓力高的値之 下，氣體從積蓄器24排出至積蓄器1，並且在差動液體流 從管線89被傳送通過液壓變換器60的第三通口 70、管線 71、及止回閥97之下，產生從積蓄器1的液體貯器3通 過液壓變換器60的通口 68、69而至液體貯器27及28內 的逆向液體流。因此，在兩種情況中，液壓變換器60均 -44- 201132851 容許克服導因於包含積蓄器1、2、24的氣體及液體通口 、氣體及液體熱交換器、液體緩衝器、閥、及管線的氣 體-液體迴路的阻抗的合計壓力降以及另外的導因於分隔 件的由摩擦所造成的壓力降。 在根據圖2的實施例中，液壓變換器60被建構成可 變的液壓變換器，其可改變通過其通口 68、69、70的液 體流量之間的比，且然後可保持這些液體流中液體壓力之 間的不同比。在其他實施例中，被用於積蓄器間液體的傳 遞的液壓變換器60可被建構成不可調整的液壓變換器， 亦即通過其通口的液體流量之間具有恆定的比，例如如同 積蓄器24包含由一個分隔件隔開的三個液體貯器。圖8 顯示與熱絕緣液體緩衝器結合的此種液壓變換器的整合實 施例。此液壓變換器的兩個液體貯器80及81是藉著一個 共同的熱絕緣活塞分隔件82而與較大的液體貯器83隔開 。熱絕緣活塞分隔件82沿著安裝在強固外殼85的內部的 熱絕緣插入物84滑動。在積蓄器間的氣體及液體傳遞期 間，貯器81及83被用於與彼此之間正有液體被傳遞的積 蓄器的液體貯器進行液體交換。較大的貯器83連接於較 熱的積蓄器（例如圖2的積蓄器2或24)並且與其交換較 熱的液體。較小的貯器81連接於較冷的積蓄器（例如圖2 的積蓄器1)並且與其交換較冷的液體。貯器83及81的 截面面積的比等於在氣體經由熱交換器在較冷與較熱積蓄 器之間傳遞的階段中氣體體積改變的程度。第三貯器80 的截面面積等於貯器83及81的截面面積之間的差。因此 -45- 87 201132851 ’通過液體通口 86的液體流等於通過通口 88與通口 的液體流之間的差。第三貯器80被用來在壓縮之下的 體傳遞期間吸取差動液體流，以及在膨脹之下的氣體傳 期間排出差動液體流。熱絕緣活塞分隔件82及插入物 是由熱絕緣材料（例如聚亞胺或其他高溫塑膠）製成， 減少在貯器83內的較熱液體與貯器80及81內的較冷 體之間通過分隔件及插入物的熱傳遞。活塞分隔件82 插入物84之間的長的滑動接觸減少導因於與貯器83內 較熱液體接觸的熱絕緣插入物84的表面的部份的循環 加熱及冷卻的熱損失。至於使用此種整合實施例成爲熱 緣緩衝器’只有較小的液體貯器80及81二者被互連。 種整合實施例導致整體流體動力阻抗的減小以及較佳的 置小型化。 在以上所述的所有產生積蓄器間液體流的情況中， 蓄器之間的氣體及液體的相互交換率是藉著例如藉由調 各別液壓變換器或其他液壓機械機構以改變各別積蓄器 液體貯器內高於同一積蓄器的氣體貯器內的氣體壓力的 力超額而被改變。上述的相互交換率也可藉著在氣體傳 期間改變氣體溫度改變的程度（例如藉由改變熱交換器 或1 1的溫度）而被改變。積蓄器間液體流的流量被選 成使得積蓄器內液體的任何部份之間的壓力差（由上述 迴路的阻抗及液壓變換器的密封的摩擦所造成者）不超 數巴（bar)，較佳地不超過1巴。因爲積蓄器內的氣 及液體的工作壓力爲數十及數百巴，所以此液體流內的 氣 遞 84 以 液 與 的 性 絕 此 裝 積 節 的 壓 遞 10 擇 的 過 體 液 -46- 201132851 體的任何部份之間的壓力差不超過液體被泵唧所至的液體 貯器內的液體壓力的30%，較佳地此壓力差不超過該液體 壓力的5 %。 根據圖2的液體供應及吸取機構14包含配備有積蓄 器91及92的第一管線89及第二管線90、及可在這些管 線中保持不同壓力（於管線89中-在第一指定範圍中的第 一壓力改變，且於管線90中-在第二指定範圍中的第二壓 力改變）的具有閥94及95的補充栗（replenishment pump) 93，並且包含具有三個通口 77' 78、及79的液壓變換器 76。兩個通口 78及79連接於管線89及90。第三通口 77 經由閥63、62、及61而與積蓄器1的液體貯器3及與積 蓄器24的液體貯器27及28連接。液壓變換器76被實施 成爲可變的液壓變換器，因而可改變（連續式地或步進式 地）通過液壓變換器的通口的液體流量之間的比，且然後 改變這些通口內的壓力之間的比。因此，在氣體壓力改變 的階段中，液壓變換器7 6確保在與管線8 9、9 0中的給定 的第一及第二壓力不同的壓力之下，兩個管線89、90與 積蓄器1、2、或24的液體貯器之間有液體交換的可能性 〇 管線89、90中的第一及第二壓力均被保持於高的値 (較佳地爲數十或數百巴），而第二壓力比第一壓力高。 爲穩定管線89、90中的壓力，所利用的是具有比積蓄器1 、2、及24的合計工作體積大的工作體積的積蓄器91、92 。當裝置被帶至其初始狀態時，補充泵93從箱槽96經由 -47- 201132851 閥94、95而傳送液體至積蓄器91、92內’直到第一及第 二管線89、90內的壓力被分別設定在指定的第一及第二 範圍內。 轉換是成爲一循環被實施，而此循環包含在具有較冷 的氣體貯器7的積蓄器1內的氣體壓縮階段、氣體從積蓄 器1經由較熱的熱交換器10被傳遞至積蓄器2內的氣體 傳遞階段、氣體在積蓄器2及24的較熱的氣體貯器8及 23內膨脹之下從積蓄器2傳遞至積蓄器24內的氣體傳遞 階段、及氣體從積蓄器24經由較冷的熱交換器11被傳遞 至積蓄器1內的氣體傳遞階段。 藉著利用由從管線90通過液壓變換器76的通口 79 的液體流致動的液壓變換器76將工作流體泵啷至積蓄器1 的液體貯器3內，積蓄器1內的氣體從在管線89內的壓 力以下的壓力被壓縮至在管線90內的壓力以上的壓力。 在氣體壓縮期間，積蓄器1的液體貯器3內的液體壓力藉 著液壓變換器76的調節而被升高，亦即藉著提高從管線 90經由通口 79被傳送至液體變換器76內的液體的流量對 於從液體變換器76經由通口 77被排出至積蓄器1的液體 的流量的比而被升高。液壓馬達51致動氣體鼓風機48, 其泵啷氣體通過熱交換器11，而此導致熱從氣體被移去， 並且使氣體壓縮過程較爲接近等溫過程。 在液體貯器3內的液體壓力已被升高至第二壓力（第 二管線90中的壓力）以上的壓力之後，閥62及63被切 換至氣體從積蓄器1被傳遞至積蓄器2內的氣體傳遞階段 -48 - 201132851 ’而此係於積蓄器內的工作液體壓力超過第二壓力的情 中被實施。從積蓄器2的液體貯器4至管線90的工作 體流致動液壓變換器60，其產生從積蓄器2至積蓄器1 工作液體流。結果，氣體從氣體貯器7被排出至氣體貯 8內。在此情況中，氣體被傳遞通過止回閥22、再生氣 熱交換器53、及較熱的熱交換器1〇。由於熱從再生熱 換器53及較熱的熱交換器1〇供應至氣體，因此氣體加 繼續，並且膨脹趨近等壓過程。 藉著將工作液體從液體貯器28排出通過液壓變換 76而至管線89以致動液壓變換器76及產生從液壓變換 76至管線90的工作液體流，氣體在具有較熱的氣體貯 8、23的積蓄器2、24內從超過管線90內的壓力的壓力 脹至在第一管線89內的壓力以下的壓力。在氣體膨脹 間，積蓄器24及2的液體貯器28、27、4內的液體壓 藉著液壓變換器76的調節而被降低，亦即藉著提高從 蓄器24的液體貯器28經由通口 77被傳送至液壓變換 76內的液體的流量對於從液壓變換器76經由通口 79被 出至管線90的液體的流量的比而被降低。從液體貯器 流動通過液壓變換器76的通口 77的液體的壓力被保持 比氣體貯器23內的氣體壓力低。同時，同一積蓄器24 另一液體貯器27在液體正從積蓄器24的液體貯器27 傳遞至積蓄器2的液體貯器4之下產生比氣體壓力高的 力。在氣體傳遞通過熱交換器1 〇的期間供應至氣體的 將氣體膨脹過程帶至較爲接近等溫過程。 況 液 的 器 體 交 熱 器 器 器 膨 期 力 積 器 排 28 於 的 被 壓 熱 -49- 201132851 在液體貯器3內的液體壓力已被降低至第一壓力（第 一管線89中的壓力）以下的壓力之後，閥61、62及63 被切換至氣體從具有較熱的氣體貯器23的積蓄器24被傳 遞至具有較冷的氣體貯器7的積蓄器1內的氣體傳遞階段 ，而此係於積蓄器內的工作液體壓力係在第一壓力以下的 情況中被實施。從管線89 (經由各別止回閥97 )至積蓄 器24的液體貯器27、28的工作液體流致動液壓變換器60 ，其產生從積蓄器1至積蓄器24的工作液體流。因此， 氣體從氣體貯器23被排出至氣體貯器7內。在此情況中 ，氣體被傳遞通過再生氣體熱交換器53、較冷的熱交換器 11、及各別止回閥22。由於熱從氣體被移去至再生熱交換 器53及較冷的熱交換器11，因此氣體被冷卻及壓縮，並 且過程趨近等壓過程。 由於每一轉換循環的結果，工作液體的一些部份從具 有第一壓力的管線89被傳遞至具有較高的第二壓力的管 線90。壓縮及膨脹的趨近等溫過程以及等壓壓縮階段與等 壓膨賬階段之間的氣體熱再生將氣體循環帶至接近第二型 的愛力克生循環（Ericsson cycle of the second type)( 兩個等溫階段及兩個等壓階段，而兩個等壓階段之間有熱 再生）。氣體壓縮及膨脹越接近等溫且熱再生率越接近 1 00%，此種循環的熱力學效率就越接近熱力學極限，亦即 越接近卡諾（Carnot)循環效率。 液壓變換器60及76的滑動密封（以及積蓄器24的 分隔件75的密封）係於差壓而非於全壓力操作，此減小 -50- 201132851 導因於滲漏及摩擦的損失，並且增大轉換的液壓機械 〇 根據圖2的液體供應及吸取機構14也包含具有 通口 99、100、101、102的液壓變換器98。兩個通[ 及100與第一及第二管線89、90連接，而另外兩個 101及102與兩個輸出管線104及105連接。液壓變 98被實施成爲被調節的液壓變換器，其可將輸出管線 、105內的壓力保持成與第一及第二管線89、90內的 不同。上述的將熱轉換成流體動力的循環的過程包含 的將液體從第一及第二管線89、90供應至積蓄器1 的階段及將液體從積蓄器2 ' 24吸取至管線89、90 階段。因此，這些管線內的壓力承受在指定的第一及 壓力範圍內的循環性改變。液壓變換器內壓力變換率 制確保傳遞至負載106的動力與這些循環性的壓力變 關。當第一或第二壓力由於液壓變換器76或98的滲 超出指定範圍時，這些壓力是藉著補充泵93及閥94, 而恢復。因此，壓力被隔離（isolated)，以藉著管I 、90內的給定的第一及第二壓力的選擇而將氣體循環 率最佳化，以及藉著管線1〇4、105內的高及低輸出 的選擇而將負載106的情況最佳化。 結果，從熱源以微小損失被傳遞至氣體的熱以高 力學效率被轉換成氣體功（gas work)，而氣體功以 液壓機械效率被轉變成被傳遞至負載的流體動力。 因此，所提出的將熱轉換成流體動力的方法及其 效率 四個 ]99 通口 換器 1 04 壓力 交替 、2 4 內的 第二 的控 動無 漏而 "5 I 89 的效 壓力 的熱 高的 實施 -51 - 201132851 裝置提供： -高的熱利用率，因爲經由熱交換器的積蓄器間的氣 體傳遞消除龐大元件的循環性加熱及冷卻的熱損失，特別 是與消除與積蓄器的壁部熱交換的氣體熱損失結合，以及 與藉著工作液體的熱的保存或再生而消除與液體熱交換的 氣體熱損失結合； -高的將供應至氣體的熱轉換成由氣體所實施的功的 氣體循環的熱力學效率，特別是與氣體熱再生結合，以及 與趨近等溫過程的氣體壓縮或膨脹過程結合； -高的將氣體功轉換成流體動力的液壓機械效率，因 爲積蓄器間的液體傳遞藉著液壓變換器而具有小的壓力差 ，特別是與液體在積蓄器與管線之間於小的壓力差等壓交 換結合，以及與於氣體壓縮或膨脹分別使用液壓變換器於 液體供應或吸取結合； -高的將熱轉換成被傳遞至負載的流體動力的槪括效 率，因爲有以上所述的要素的結合，特別是與使用液壓變 換器以確保將與積蓄器交換液體的管線內的壓力轉變成與 負載交換液體的管線內的壓力的結合； -高的功率密度（power density)，因爲有高的氣體 及液體壓力以及高的變換效率； -增加的可靠性’因爲元件在高壓下的循環性加熱及 冷卻被消除； -將熱積蓄在龐大的熱交換器內且在熱源功率的暫時 性停止運轉或降低期間使用積蓄的熱以轉換成流體動力的 -52- 201132851 可能性。 熟習此項技術者可瞭解此詳細敘述只是給予一個例子 ，並且在本發明的範圍內的許多其他的變化可被提出，包 括例如（但是不限於）未在此處被詳細敘述並且氣體循環 的類型不同、工作液體及氣體的選擇不同、以及外部熱源 及冷卻熱傳遞媒質的類型及與其熱接觸的特定特徵不同的 方法的實施；及積蓄器、氣體及液體熱交換器、氣體鼓風 機、包括液壓變換器及緩衝器的液體供應及吸取機構、及 裝置的其他組件的數目及實施例不同的裝置實施例；以及 未在以上被敘述的裝置的組件的整合實施例的變化》 【圖式簡單說明】 圖1顯示具有兩個積蓄器及兩個熱交換器的裝置。 圖2顯示具有三個積蓄器、氣體鼓風機、氣體再生熱 交換器、液體熱交換器、及液體熱絕緣緩衝器且具有液壓 變換器的裝置。 圖3顯示氣體流熱交換器。 圖4顯示液體再生熱交換器與液體熱絕緣緩衝器的整 合實施例。 圖5顯示積蓄器與氣體流熱交換器的整合實施例。 圖6顯示積蓄器、氣體流熱交換器、與由液壓馬達致 動的氣體鼓風機的整合實施例。 圖7顯示氣體再生熱交換器。 圖8顯示不可調整的液壓變換器與液體熱絕緣緩衝器 -53- 201132851 的整合實施例。 【主要元件符號說明】 1 :液氣積蓄器 2 :液氣積蓄器 3 :液體貯器 4 :液體貯器 5 :可移動的分隔件 6 :可移動的分隔件 7 :氣體貯器 8 :氣體貯器 9 :加熱及冷卻機構 10 :熱交換器 1 1 :熱交換器 1 2 :氣體管線 13 :閥 14:液體供應及吸取機構 15:內部槽溝型氣體通道 16 :內部軸向通道 1 7 :收集器部份 18 :插塞 1 9 :通口 20 :凸緣 2 1 :螺旋狀外部通道 -54 201132851 22 :止回閥 23 :氣體貯器 24 :積蓄器 25 :熱交換器 26 :止回閥 27 :液體貯器 28 :液體貯器 29:液體再生熱交換器 3 〇 :熱絕緣緩衝器 3 1 :可變體積的液體貯器 3 2 :可變體積的液體貯器 3 3 :可移動的熱絕緣體，液密的可移動的熱絕緣分隔件 3 4 :強固外殼 3 5 :液體通口 3 6 :液體通口 37 :金屬套筒 38 :活塞 3 9 :空間 40 :塡料 41 :空腔 42 :孔 43 :孔 44 _·流動部份 45 :再生元件 -55- 201132851 46 :強固外殼 47 :內部熱交換區段 48 :氣體鼓風機 49 :氣體管線 5 0 :氣體管線 5 1 :液壓馬達 5 2 :軸件 53:氣體再生熱交換器 54 :強固外殼 55:熱絕緣插入物，隔熱插入物 56 :再生元件 57 :螺旋狀薄片 58 :墊片 5 9 :穿孔 60 :液壓變換器 61 :閥 6 2 :閥 6 3 :閥 64 :液體管線 6 5 :液體管線 6 6 :液體管線 67 :液體管線 6 8 :液體通口 69 :液體通口 -56- 201132851 70 ： 71 : 72 ： 73 ： 74 ： 75 ： 76 ： 77 ： 78 ： 79 ： 80 ： 81 ： 8 2 ： 8 3 ·· 8 4 ： 85 ： 86 ： 87 : 88 ： 89 ： 90 ： 91 : 92 ： 93 ： 液體通口 液體管線 氣體通口 液體通口 液體通口 活塞分隔件 液壓變換器 通口 通口 通口 液體貯器 液體貯器 熱絕緣活塞分隔件 液體貯器 熱絕緣插入物 強固外殼 液體通口 通口 通口 第一管線 第二管線 積蓄器 積蓄器 補充泵 -57 201132851 94 :閥 95 :閥 96 :箱槽 97 :止回閥 98 :液壓變換器 99 :通口 1 00 :通口 1 01 :通口 102 :通口 103 ··閥 1 0 4 :輸出管線 1 0 5 :輸出管線 106 :負載 -58-201132851 VI. Description of the Invention: TECHNICAL FIELD OF THE INVENTION The present invention relates to mechanical engineering and can be used to source various sources including the sun, internal combustion engines or external combustion engines, high temperature fuel cells, geothermal heat, and the like. The heat is efficiently converted into fluid power. [Prior technology]. US Patent 5 57, The apparatus disclosed in No. 964 can implement a method of converting heat to fluid power. The method comprises pumping a working fluid to a hydropneumatic accumulator (hereinafter referred to as an accumulator) under gas compression. The gas expansion occurs when the liquid is discharged from the accumulator. And the heat supply to the gas and the removal of heat from the gas are performed such that the average gas temperature during expansion should be higher than the average gas temperature during compression. This method is by including at least two liquid gas accumulators (referred to in the foregoing It is implemented as a device for the "first and second liquid tanks"). In each accumulator, The liquid reservoir in communication with the liquid supply and suction mechanism is separated from the gas reservoir in communication with the heating and cooling mechanism by a movable partition. The heating and cooling mechanism is constructed to form a gas that can be heated and cooled. The heating and cooling mechanism includes gas receivers (referred to as "first and second gas containers" in the foregoing case), And each of the gas receivers is in communication with a gas reservoir of each (first or second) accumulator, And the heating and cooling mechanism includes a gas heating and cooling mechanism in the receiver (referred to as "first and second heating and cooling mechanisms -5-201132851 j" in the foregoing cases), And constructed to form a control system that allows the gas to cool and heat alternately in the receiver. The liquid supply and suction mechanism includes a hydraulic pump, Hydraulic motor, And valve. Heat is supplied from the hot heat transfer medium to the gas in the receiver via the wall of the heat exchanger for heating, The heating heat exchanger is placed outside the receiver and transfers heat to the gas via the wall of the receiver. Or placed inside the receiver to transfer heat to the gas via its own strong wall. What is proposed is to use a heat transfer medium such as an exhaust gas of an internal combustion engine to become hot. The heat from the gas in the receiver is directly extracted to the external cooling heat transfer medium via the wall portion of the receiver or via the strong wall portion of the separate cooling heat exchanger placed inside the receiver. It is proposed to use ambient air or water to become a heat transfer medium for cooling. Switching from heat supply to heat removal and switching back to heat supply is by using a valve to shut off the heat of the heat transfer medium and to open the heat for cooling. The media stream is delivered and vice versa. Each accumulator is a separate converter that converts heat into fluid power with its receiver and heating and cooling mechanisms. The gas reservoirs of the different accumulators are not connected to each other and the liquid reservoir is connected to the liquid supply and suction mechanism via separate valves. To reduce the pulsation of the input and output flows into the device, Two or more such converters are used, In order to pump the liquid into the accumulator of one of the converters, the liquid is discharged from the accumulator of the other converter. In each of these converters, The foregoing method is implemented as a cyclical -6 - 201132851 process, This cyclical process consists of four consecutive phases: - after the gas is compressed and the gas is discharged from the accumulator to the receiver, And under the cooling heat transfer medium where the heat from the receiver is removed to the outside, Pumping the working fluid from the liquid supply and suction mechanism into the accumulator, - isosiconically heating the gas in the receiver by supplying heat to the gas from, for example, a hot heat transfer medium, - after the gas is discharged from the receiver into the accumulator, After the liquid is discharged from the accumulator to the liquid supply and suction mechanism, And continuing to supply heat to the gas in the receiver from, for example, a hot heat transfer medium, Perform gas expansion, - The gas is equally volume-cooled by removing heat from the gas in the receiver to the external cooling heat transfer medium. Due to the heat supply to the gas during equal volume heating and subsequent expansion stages and the removal of heat from the gas during equal volume cooling and subsequent compression stages, The average temperature (and therefore the average pressure) of the gas during expansion is higher than during compression. Therefore, the gas expansion work exceeds the gas compression work. result, Some parts of the heat are converted into additional fluid power. but, The cyclic heating and cooling of the gas takes place within the volume of the same gas receiver, This means not only cyclic heating and cooling gas, It also cyclically heats and cools the heat exchanger and the wall of the receiver. There is heat exchange between high pressure (bars) of gas and heat exchange medium of low pressure (down to several bars for exhaust gas). The heat exchanger with relevant strength 201132851 and the wall of the receiver are very large. And its thermal capacity is significantly higher (at least tens of times) the heat capacity of the gas within the receiver. The heat capacity of the heat exchanger with associated strength and the wall of the receiver is significantly higher (hundreds and thousands of times) than the heat capacity of the atmospheric air and the exhaust gas pumped through the heat exchanger per second. result, The thermal inertia of the device is high, The gas is cooled and the heating rate is low. This reduces the operating rate and the average power density of the device, And thus the first significant drawback of the proposed solution. Gas heating and cooling in the receiver occurs due to gas heat conduction and natural convection. This also reduces the heating and cooling rates and the associated specific power. In this case, Most of the heat from the external heat source is spent on the bulk of the heat exchanger and receiver that is cooled during the previous stages of heating, rather than being converted to fluid power. When the gas expansion is complete, The heat accumulated in the heat exchanger is transferred to the heat transfer medium for cooling and released. Therefore, The heat utilization efficiency is obviously low, This is the second and most substantial drawback of the proposed solution. The heat loss from the use of heat removed during cooling of one of the receivers during the cooling of one of the receivers, which is proposed in the above, allows for a reduction in heat loss of no more than 50%. Additional heat loss occurs when the heated gas stream enters the accumulator. At this time, the gas is blown through the wall portion of the gas reservoir of the accumulator to quickly impart heat to the wall portions. It should also be noted that in the proposed solution, Increasing the thermodynamic efficiency of the gas cycle is primarily incompatible with increasing the efficiency of converting the heat of the external heat source 201132851 into fluid power. In an attempt to increase the efficiency of gas circulation, It is recommended to heat the gas in the receiver until the temperature of the gas in the receiver approaches the temperature of the hot heat transfer medium. Similarly, the pre-opening case proposes to cool the gas in the receiver. Until the temperature is equal to the temperature of the surrounding air or the temperature of another cooling heat transfer medium. but, When the temperature of the heat exchanger approaches the temperature of the hot heat transfer medium, The heat removed from the heat transfer medium to the heat exchanger tends to be zero. therefore, Although the thermodynamic efficiency of the gas cycle grows, However, the efficiency of heat conversion from external heat sources to fluid power is even lower. Rate and average power are also reduced, Because the process of equalizing the temperature inside the receiver is asymptotic. Cyclic heating and cooling of the body of the receiver and heat exchanger under high pressure accelerates fatigue failure and reduces the reliability and safety of the proposed device. In addition, Switching the hot heat transfer medium flow through the valve also reduces the reliability of the device. Especially when using an internal combustion engine exhaust that combines high temperatures (up to 800 ° C to 900 ° C) and chemical aggressiveness, Failure of the valve that switches the exhaust flow may result in dangerous uncontrolled overheating of the gas within the receiver with a pressure increase that exceeds the maximum allowable level. Or in the case of a blocked exhaust duct, the malfunction of the internal combustion engine is caused. therefore, Low heat conversion to fluid power efficiency and conversion rate, Low specific power, And low reliability is the main drawback of the proposed solution. Where: Another substantial disadvantage of the gastric delivery protocol is that it is not possible to accumulate heat and generate fluid dynamics during the temporary shutdown or reduction of the hot heat transfer medium flow. SUMMARY OF THE INVENTION -9 - 201132851 The essence of the invention is to increase the efficiency and rate of conversion of heat into fluid power. Another object of the invention is to increase the power density and reliability of a device that converts heat into fluid power. Another object of the present invention is to ensure the possibility of heat storage and conversion to fluid power during temporary shutdown or reduction of heat supply power. Method The method of converting heat into fluid power for achieving these objectives comprises pumping a working fluid into a fluid reservoir of at least one liquid gas accumulator (hereinafter referred to as an accumulator), And causing gas compression to occur in the gas reservoir of the at least one accumulator, The gas expansion then occurs in the gas reservoir of the other at least one accumulator after the fluid is discharged from the fluid reservoir of the at least one accumulator. And the heat supply to the gas and the heat removal from the gas are carried out such that the average gas temperature during expansion is higher than the average gas temperature during compression. By ensuring that at least two accumulators are used, And after the gas is transferred between the different accumulators via the hotter heat exchanger and another cooler heat exchanger, Heat is supplied to the gas by passing the gas through a hotter heat exchanger. And heat is removed from the gas by passing the gas through another, cooler heat exchanger. The above purpose can be achieved. To keep the heat exchanger hot, The heat exchanger is brought into thermal contact with the heat source (by heat conduction, radiation, Or by heat transfer medium for heating -10 - 201132851 heat transfer). To keep the heat exchanger cold, This heat exchanger is brought into thermal contact with the heat transfer medium for cooling. Since this is due to the fact that the average gas temperature during expansion is higher than the average gas temperature during compression (and therefore the average gas pressure is also high), The gas expansion work exceeds the gas compression work. result, Some of the heat carried from the heat source to the heat transfer medium for cooling via the heat exchanger and gas stream is converted to additional fluid power, It can be used to perform mechanical work. To pump the working fluid and to use the extra fluid power obtained by discharging the liquid through the hotter gas, Liquid supply and suction mechanisms are used, It may include a hydraulic pump and a motor or liquid pressure transducer (hereinafter referred to as a hydraulic transformer). Due to the gas transfer between the different accumulators via the heat exchanger, Therefore, only the delivered gas, rather than the bulky heat exchanger, undergoes cyclic heating and cooling, which results in significantly lower heat loss and significantly increased heat transfer to fluid power conversion efficiency. Forced convection of the gas flowing through the heat exchanger ensures its high heating and cooling rates, This allows the heat of the external heat source to be converted to fluid power at a high slew rate and at a specific power. Eliminating the cyclic heating and cooling of heat exchangers under high pressure and other components of the heating and cooling mechanisms increases the reliability and safety of these components in converting heat into fluid power. The heat accumulated in the hotter heat exchanger is not released. It can be used to convert to fluid power during the temporary stop or decrease of the power of the external heat source. -11 - 201132851 To reduce the heat loss when the wall of the gas reservoir of the accumulator is blown through the heated or cooled gas stream, The wall of the gas reservoir of at least one accumulator is kept cold, And the gas is transferred to the gas reservoir via a cooler heat exchanger, The wall of the gas reservoir of the other accumulator is kept hot. And the gas is delivered to the gas reservoir via the hotter heat exchanger. In order to reduce the heat loss of the gas passing through the accumulator partition caused by the temperature difference between the gas and the liquid in the accumulator, The wall of the liquid reservoir of at least one accumulator and the working fluid in the liquid reservoir are kept cold, And the wall portion of the liquid reservoir of at least one other accumulator and the working fluid in the liquid reservoir are kept hot. To prevent the heat loss associated with the flow of working fluid, The present invention provides thermal and thermal regeneration of liquid streams as the hot (or cooler) working fluid is pumped and discharged. For heat regeneration, The working liquid discharged from the at least one accumulator passes through the regenerative liquid heat exchanger. When the working fluid is pumped into the accumulator, The working fluid passes through the same regenerative liquid heat exchanger in the opposite direction. For thermal insulation of liquid streams, The hotter working fluid is separated from the cooler working fluid by at least one movable thermal insulator. For operations that have an increased temperature difference between the accumulators, a working fluid is used in a colder liquid reservoir, Another working fluid is used in a hotter liquid reservoir. The two different working fluids are separated by at least one movable partition. The movable partition can also be a movable thermal insulator. For example, a piston made of a material having a low heat transfer coefficient (Poly-12-201132851 or ceramic), Or an elastic spacer coated with an open-cell foamed elastomer. High temperature organic (for example based on diphenyl or diphenyloxide) or sand-organic (for example based on monomethyl dimethylsiloxane) working liquid Use allows the temperature of the hotter accumulator and the working fluid inside it to be maintained at 300 ° C to 4 ° C. The use of an inorganic working fluid, such as molten tin or other metal, allows the maximum temperature to be increased up to the temperature stress limit of the material of the wall of the accumulator. The increased temperature of the hot accumulator and the working fluid therein increases the conversion efficiency of the heat transfer to fluid power, In particular, when the heat loss associated with the liquid flow is eliminated in the manner previously described. The stable temperature condition of the strong outer casing of the accumulator under high pressure also increases the reliability and safety of the accumulator to convert heat into fluid power. In order to bring the gas compression process closer to the isothermal process, At least three accumulators are used, Whereas the wall of the gas reservoir in at least two of the at least three accumulators is kept cold, And the gas is transferred between the at least two accumulators under compression via a cooler heat exchanger. In order to make the gas expansion process approach the isothermal process, At least three accumulators are used, Whereas the wall of the gas reservoir in at least two of the at least three accumulators is kept hot, And the gas is transferred between the at least two accumulators under expansion via a hotter heat exchanger. To increase the maximum gas temperature above the maximum allowable temperature of the working fluid or separator in at least one accumulator, The wall of the gas reservoir is separated from the heated gas stream by thermal protection. In order to bring the gas compression or expansion process in the gas reservoir of at least one accumulator closer to the isothermal process and further increase the efficiency of heat conversion to fluid power, A gas circulation pump (hereinafter referred to as a gas blower for the sake of brevity) is used to generate forced gas convection. Both an external gas blower and a gas blower implemented inside the accumulator (either in its housing or in a gas reservoir) can be used. To better approach isothermality, Forced convection is produced by passing a gas through at least one heat exchanger using a gas blaster. The gas is withdrawn from the gas reservoir of at least one of the accumulators and returned to the same gas reservoir. It is preferred to reduce heating and cooling losses in the gas line, The gas from this gas reservoir should be withdrawn through a gas line. And return via another gas line. The gas blower can be electrically driven by a shaft of the drive or another kinematic link, Hydraulic motor, Or other motor actuation, The shaft member or the moving link of the drive is provided with a seal that prevents leakage of the compressed gas. In order to reduce the leakage and friction loss of the seal, The moving link of the gas blower drive is actuated by a hydraulic motor that operates at a near liquid pressure (typically no more than a few bars of gas pressure within the gas blower). Preferably, when liquid is pumped into the liquid reservoir of at least one of the accumulators via the hydraulic motor or discharged from the liquid reservoir, The hydraulic motor should be actuated by liquid flowing between the hydraulic motor and the liquid reservoir. In order to increase the thermodynamic efficiency, the conversion is performed as a cycle with gas thermal regeneration when compression or expansion approaches isothermal compression or expansion. At least one of them, Heat is removed from the gas under gas cooling' and at least at one stage, Some of the heat that is supplied to the gas under heat heating and removed from the gas during the cooling phase is used to supply to the gas during the heating phase. For this purpose, The heat is removed from the gas to the regenerative heat exchanger during the cooling phase and the heat is first supplied to the gas from the regenerative heat exchanger and then from the external heat source in the heating phase. When using a high temperature heat source such as a high temperature fuel tank, The heat of the sun, Or the heat given by another source of radiant energy, It is preferred to use a separate regenerative heat exchanger. During the gas cooling phase, The gas first passes through a separate regenerative heat exchanger in the cooling direction. Then through the cooler heat exchanger, In the gas heating stage, The gas first passes through the regenerative heat exchanger, preferably in a heating direction opposite to the cooling direction. Then pass the hotter heat exchanger. When heat is transferred from a heat source by a hot heat transfer medium (eg, exhaust) that is released after heat removal, A counterflow of a hotter heat exchanger is used to increase efficiency. The gas is passed through the countercurrent hotter heat exchanger during the heat supply in a direction opposite to the direction of the hot heat transfer medium stream. Causing heat from the heat transfer medium exiting the heat exchanger to the gas entering the heat exchanger, Heat is supplied from the heat transfer medium entering the heat exchanger to the gas leaving the heat exchanger. This ensures hot heat transfer media (for example, Higher gas heating and cooling rate of the output stream or water stream of the end product of the fuel combustion. Preferably, the same countercurrent heat exchanger (or a portion thereof) should be used as a regenerative heat exchanger. Where -15- 201132851 gas passes through the counter-flow heat exchanger (or a part thereof) in one direction during cooling, And passing through the counterflow heat exchanger (or a portion thereof) in the opposite direction during heating. For increased thermal regeneration, Contains two isothermal stages and two isobaric stages (or two other stages in the middle of the "entropy" coordinate, For example, the gas cycle of the isochoric phase approaches the generalized Carnot cycle, It allows heat to be converted to gas work with maximum thermodynamic efficiency. To reduce hydromechanical losses, The portion of the liquid that is exposed to a large pressure change during delivery through the hydromechanical device is reduced. For this purpose, The gas is transferred between the gas reservoirs of the accumulator by pumping the liquid into the liquid reservoir of the at least one accumulator and discharging the liquid from the liquid reservoir of at least one other accumulator. The liquid flow is created between the liquid reservoirs of the accumulators such that the pressure difference between any portion of the liquid within the liquid flow does not exceed 30% of the liquid pressure in the liquid reservoir to which the liquid is pumped. , Preferably, the pressure differential should not exceed 5% of the liquid pressure. In a traditional accumulator, Each gas reservoir corresponds to a liquid reservoir, The pressure difference between the two is quite small, It is only related to the friction of the piston spacer or the deformation of the elastic spacer. The flow of liquid between these accumulators is produced by a hydraulic mechanical mechanism (e.g., a liquid pump or a hydraulic transducer) that transfers liquid between the accumulators. The hydromechanical mechanism overcomes the pressure difference between -16 and 201132851 of the liquid reservoir of the accumulator in which the gas reservoir is connected via the heat exchanger. The pressure difference between different portions of the liquid flow between the liquid reservoirs through the accumulator having a gas reservoir that is in communication via the heat exchanger is by the impedance of the heat exchange and communication lines (gas and liquid lines) and by The efficiency of the hydraulic mechanism that transfers liquid between the accumulators is determined. Compared to the total pressure of the liquid in the accumulator, This pressure difference is quite small (preferably no more than a few bars). therefore, The losses associated with leakage and friction of the hydraulic mechanical mechanism for liquid transfer between the accumulators are also relatively small. The hydraulic mechanical mechanism can include a fluid pump, It is electrically driven by the shaft of the drive or another moving link, Hydraulic motor, Or other motor actuation, The shaft member or the moving link of the drive is provided with a seal that prevents liquid leakage. In order to reduce the leakage and friction loss of the seal, This liquid flow between the accumulators is preferably produced by a hydraulic transducer having at least three liquid ports. In order to generate a liquid flow between the accumulators, Two of the at least three liquid ports are connected to the liquid ports of the respective accumulators, And the hydraulic transducer is actuated by another flow of liquid flowing through at least one other port of the hydraulic transducer. Preferably, the further liquid stream is a liquid stream entering the hydromechanical mechanism from the accumulator (the gas entering the accumulator discharges liquid therefrom) and exiting the hydraulic converter to the accumulator (the liquid entering the accumulator) A differential liquid flow between the liquid streams within which the gas is discharged. Different hydraulic transformers can be used, Included are hydraulic transducers that have separate, kinematically interconnected or integrated pumps and hydraulic motors, including both rotor hydraulic motors and linear hydraulic motors. -17- 201132851 For example, a phase-regulated hydraulic converter, Each cylinder should act as a motor during one part of the cycle. In the other part, it acts as a pump. In terms of miniaturization, Preferably, at least one accumulator incorporating the functions of the liquid gas accumulator and the hydraulic converter is used. The accumulator contains at least two liquid reservoirs, The at least two liquid reservoirs are separated from a gas reservoir by a common piston partition. These liquid reservoirs have separate liquid ports and are spaced apart from each other 'this allows different pressures to be maintained within these liquid reservoirs' to balance the force of the total pressure of the liquid on the divider with the force of the gas pressure on the divider . In order to generate the aforementioned liquid flow between the accumulators, The pressure of the liquid in the at least one liquid reservoir of the accumulator is maintained above the gas pressure in the gas reservoir of the same accumulator, The pressure of the liquid in at least one other liquid reservoir of the accumulator is maintained below the gas pressure. At least one of the liquid reservoirs connected to the liquid reservoir of at least one other accumulator participates in the flow of liquid between the accumulators, At least one other liquid reservoir of the same accumulator is used to maintain the ratio of the liquid pressure depending on the direction of gas transfer. The pressure in the liquid reservoir that participates in the transfer of liquid between the accumulators is raised or lowered relative to the gas pressure by the valve to produce a liquid flow. For this purpose, The pressure in the liquid reservoir that is not involved in the transfer of liquid between the accumulators is reduced or raised by the valve in accordance with the force balance that maintains the pressure on the piston divider. When gas is delivered to the gas reservoir of the accumulator, Liquid flow is generated from at least one of the liquid reservoirs of the accumulator to another accumulator, Maintaining the pressure in the liquid reservoir at a higher pressure than the gas in the gas reservoir, At least one other -18-201132851 liquid reservoirs of the same accumulator are maintained at a lower pressure than the gas pressure. When gas is transferred from the gas reservoir of the accumulator, At least one of the liquid reservoirs from the other accumulator to the accumulator, Maintaining the pressure in the liquid reservoir at a lower pressure than the gas in the gas reservoir, The pressure in at least one other liquid reservoir of the same accumulator is maintained at a higher pressure than the gas. The present invention provides for direct flow of liquid through a hydraulic shifter and the necessary valves between liquid reservoirs of different accumulators, Or to further reduce the hydro-mechanical loss by moving the liquid buffer to the movable partition or thermal insulator via the intermediate liquid buffer. The suction of the discharged working fluid and its pumping are carried out by means of a liquid supply and suction mechanism. The liquid supply and suction mechanism includes a line having a first pressure and a line having a second pressure. The first and second pressures are both maintained at a high pressure (preferably tens or hundreds of bars), The second pressure is higher than the first pressure. The conversion is implemented as a cycle, This cycle is included in the gas compression stage in the accumulator with a cooler gas reservoir, The gas is transferred from the accumulator having the cooler gas reservoir to the gas transfer stage in the accumulator having the hotter gas reservoir via the hotter heat exchanger, In the stage of gas expansion in the accumulator with a hotter gas reservoir, And the gas is transferred from the accumulator having the hotter gas reservoir to the gas transfer stage of the accumulator having the cooler gas reservoir via the cooler heat exchanger. The gas from the accumulator having the hotter gas reservoir is delivered to the accumulator having a cooler -19-201132851 gas reservoir when the working fluid pressure in the accumulator is below the first pressure. The working fluid flow from the liquid reservoir of the accumulator of the gas reservoir to the gas reservoir having the first pressure is subjected to the aforementioned hydraulic pressure converter, The hydraulic converter produces a liquid flow from an accumulator having a reservoir to an accumulator having a hotter gas reservoir. The gas from the accumulator having a cooler gas reservoir is delivered to the accumulator having the gas reservoir above the second pressure. The working fluid flow from the liquid reservoir having the hotter gas reservoir to the pipeline having the second pressure is subjected to the aforementioned hydraulic converter, The hydraulic converter produces a liquid flow from an accumulator having a reservoir to an accumulator having a cooler gas reservoir. In an accumulator having a cooler gas reservoir (at least one body is pumped by means of a hydraulic converter that is also connected to a line having a second pressure having a first pressure) to an accumulator having a reservoir The liquid reservoir is compressed inside. This hydraulic pressure changes the flow of liquid from the line having the second pressure through the hydraulic pressure to be actuated. During gas compression, The pressure of the liquid pumped from the hydraulic converter to the device is between increasing the volumetric flow rate of the liquid flowing from the second line to the liquid and the volumetric flow rate of the liquid flowing from the device to the liquid reservoir. In contrast to an accumulator having a hotter gas reservoir (at least one body is expanded by means of an integrated reservoir having a relatively hot gas reservoir therefrom to also be connected to a line having a first pressure and having The hot gas is guided through the cold gas. The gas line in the accumulator has a hot accumulator that is guided through the hot gas. The gas line in the above work) and the cold gas converter are the converter and the liquid pressure accumulator is hydraulic. The transformation is raised. The liquid in the gas reservoir is actuated by the working fluid flow of the hydraulic transducer of the second pressure -20-201132851 force pipeline. The working fluid flow actuates the hydraulic transducer to produce a working fluid flow from the hydraulic transducer to the line having the second pressure. During gas expansion, The pressure of the liquid discharged from the liquid reservoir into the hydraulic converter is by reducing the volumetric flow rate of the liquid flowing from the hydraulic pressure converter to the second line and the volume flow rate of the liquid flowing from the liquid reservoir to the hydraulic pressure converter. The ratio between them is lowered. therefore, Due to the results of each conversion cycle, Some portions of the working fluid are transferred from a line having a first pressure to a line having a higher second pressure. The sliding seal of the hydraulic converter operates under differential pressure rather than full pressure. This reduces leakage and friction losses. The fluid power received by the aforementioned transfer of the liquid to the line having the second pressure can be used to connect the load between the line having the first pressure and the line having the second pressure. The solution proposed for expanding the use of the obtained fluid dynamics is to utilize a hydraulic transformer, Wherein the two ports of the hydraulic converter are connected to a line having a first pressure and a line having a = pressure and two additional ports are connected to a line having a high and a low output pressure. therefore, Pressure decoupling is implemented' and the efficiency of the gas cycle can be optimized by selecting the first and second pressures of the line. The load regime can be optimized by selecting high and low output pressures. The device method can be implemented by an I device that converts the heat of an external heat source into a fluid enthalpy. And the device comprises at least two liquid gas accumulators, -21 - 201132851 wherein the liquid reservoir of each of the at least two liquid-gas accumulators in communication with the liquid supply and suction mechanism is separated from the gas reservoir in communication with the heating and cooling mechanism by a movable partition 'The heating and cooling mechanism is constructed to heat and cool the incoming gas. The heating and cooling mechanism comprises at least two gas heat exchangers 'the at least two gas heat exchangers are mounted to transfer gas between the gas reservoirs of different accumulators via the at least two gas heat exchangers' Heating and cooling mechanisms are constructed to keep at least one of the heat exchangers colder, And the at least one additional heat exchanger is kept hot. At least one heat exchanger is constructed to supply heat to the gas from an external heat source. At least one heat exchanger is constructed to form a heat transfer medium that removes heat from the gas to the cooling. In the following description of the working device, The first type of heat exchanger is called a hotter heat exchanger. The second type of heat exchanger is referred to as a cooler heat exchanger. In a similar situation, A heat exchanger constructed to constitute heat that can be removed from the gas and that can supply the removed heat to the gas is referred to as a regenerating heat exchanger. In order to eliminate the heat loss of the cyclic heating and cooling of the wall portion of the gas reservoir of the accumulator, The proposed embodiment is wherein the heating and cooling mechanism is constructed to keep the wall of the gas reservoir of at least one accumulator relatively cold, And passing the gas to the gas reservoir via a cooler heat exchanger, The wall portion of the gas reservoir of at least one other accumulator can be kept hot. The gas is transferred to the gas reservoir via a hotter heat exchanger. To eliminate heat loss through the separator, The proposed embodiment is such that the heating and cooling mechanism is constructed to keep the wall of the liquid reservoir -22-201132851 of at least one accumulator and the working fluid in the liquid reservoir relatively cold, The wall portion of the liquid reservoir of at least one other accumulator and the working fluid in the liquid reservoir can be kept hot. In order to carry out the above method under the regeneration of working liquid heat, The liquid supply and suction mechanism comprises at least one liquid regenerative heat exchanger. The at least one liquid regenerative heat exchanger is coupled to the liquid reservoir of the at least one accumulator, And constructed to remove heat from the liquid during discharge of the liquid from the accumulator through the liquid regenerative heat exchanger, And the removed heat is supplied to the liquid while the liquid is pumped through the liquid regeneration heat exchanger into the accumulator. To implement the above method in order to thermally insulate the hotter portion of the working fluid from the cooler portion, The liquid supply and suction mechanism includes at least one liquid buffer, The at least one liquid buffer comprises two liquid reservoirs separated by a movable thermal insulator. To implement the above method in order to use different working fluids in different accumulators, The liquid supply and suction mechanism includes at least one liquid buffer, And at least one of the liquid buffers comprises two variable volume reservoirs separated by a movable partition. Each of the liquid reservoirs of the above liquid buffer is mounted to be in communication with a liquid reservoir of at least one accumulator. In order to reduce the mass and size of the device and the total internal volume of the gas communication line, At least one gas heat exchanger is constructed, for example, in the housing of the accumulator to become a gas port of the accumulator, Instead, heat can be supplied to the gas or removed from the gas (preferably a gas port having an increased ratio between the area and volume of the gas contact surface). Due to the removal of two intermediate passes -23- 201132851 and gas lines, Therefore, the gas dynamic loss during the passage of the gas through the heat exchanger is also reduced. In order to carry out the above method while the gas compression process is approached to an isothermal process, The proposed mounting embodiment comprises at least three accumulators, The heating and cooling mechanism is constructed to keep the wall of the gas reservoir of at least two of the accumulators relatively cold, And passing the gas between the at least two accumulators via the cooler gas heat exchanger. In order to carry out the above method under the process of making the gas expansion process closer to isothermal, The proposed device embodiment comprises at least three accumulators, The heating and cooling mechanism is constructed to keep the wall of the gas reservoir of at least two accumulators hot. And passing the gas between the at least two accumulators via the hotter gas heat exchanger. To reduce heat loss, At least one accumulator is provided with a thermal protection mechanism, This thermal insulation mechanism is constructed to separate the wall of the accumulator's gas reservoir from the incoming gas stream. When the gas is heated to below 150 ° C to 200 ° C, In order to reduce the friction loss of the separator and reduce the cost, The accumulator is constructed to have an elastic partition, The thermal insulation mechanism comprises a flexible porous thermal insulation connected to the elastic spacer, when the gas is heated to a higher temperature, The accumulator is preferably constructed to have a piston divider, The thermal insulation mechanism includes a variable length thermal screen mounted along the cylindrical side wall of the gas reservoir of the accumulator, And a hot screen mounted relative to the partition and the bottom of the gas reservoir. For temperatures above 300 °C, The above thermal screen is preferably made of metal. And • 24- 201132851 can be made from polymers at lower temperatures. For example, it can be made of an organic-antimony polymer. In order to implement the above method under a process in which the gas compression or expansion process is relatively close, The gas heating and cooling mechanism includes at least one gas circulation pump (hereinafter referred to as a gas blower for brevity), It produces forced gas convection in the gas reservoir of at least one accumulator. To improve isothermality, At least one accumulator gas reservoir is in communication with the gas heating and cooling mechanism by at least two gas lines The gas can be removed from the gas reservoir by a gas blower via one of the at least two gas lines. Passing the removed gas through at least one heat exchanger, The gas is returned to the same gas reservoir via another gas line. In an embodiment of a device that is preferred for simplicity and reliability and that includes a gas blower, The liquid supply and suction mechanism includes at least one hydraulic motor that is kinematically coupled to at least one gas blower, The hydraulic motor is mounted to be actuated by a flow of liquid between the hydraulic motor and the liquid reservoir of the at least one accumulator. To implement the conversion method by a cycle with thermal regeneration, The proposed device has at least one gas heat exchanger implemented as a regenerative gas heat exchanger, It is also possible to remove heat from the gas as it is pumped through the at least one gas heat exchanger in one direction, And the heat removed from the gas is supplied to the gas when the gas is pumped through the at least one gas heat exchanger in the opposite direction. The present invention provides for the utilization of a variety of different heat sources. Hotter heat exchange -25- 201132851 Thermal contact with the heat source is by heat conduction or heat-and-mass transfer. Including condensation heat transfer, It is implemented by radiant heat transfer and a combination of these. To ensure thermal contact with the heat source by heat and mass transfer, At least one gas heat exchanger has a passage for external heat transfer medium to pass heat from the heat transfer medium to the gas. To increase the efficiency of using hot heat transfer media, At least one heat exchanger is constructed as a counterflow heat exchanger, That is, the counterflow heat exchanger has a passage for the external heat transfer medium to pass heat from the heat transfer medium to the gas. Causing heat from the external heat transfer medium exiting the heat exchanger to the gas entering the heat exchanger, The heat from the gas leaving the heat exchanger is supplied from the external heat transfer medium entering the heat exchanger. In order to use the above heat exchanger as a regenerative heat exchanger, The heat exchanger has at least one additional port, In order to introduce the gas into the heat exchanger, The heating and cooling mechanism includes at least one passage connecting the additional gas ports described above to the accumulator and is configured to lock the passage. In order to carry out the above method under the flow of liquid between the accumulators, An apparatus embodiment is presented, Wherein the liquid supply and suction mechanism comprises a liquid transfer mechanism between the accumulators, It is embodied to produce a flow of liquid between the liquid reservoirs of at least two accumulators, The pressure difference between any portion of the liquid in the liquid stream is no more than 30% of the liquid pressure in the liquid reservoir to which the liquid is pumped, Preferably, the pressure difference does not exceed 5% of the liquid pressure. There may be various embodiments of the inter-accumulator fluid transfer mechanism. Including the use of a rotor and a linear liquid pump and a hydraulic motor, And a mechanism for making a hydraulic transducer that combines a pump and a motor with -26-201132851. In the latter case, The inter-accumulator liquid transfer mechanism includes at least one hydraulic transducer having at least three liquid ports, The at least one hydraulic transformer is mounted to be in communication with the liquid reservoirs of the at least two accumulators via the two ports of the hydraulic converter, And a liquid flow can be created between the at least two accumulators described above as the liquid flows through the other at least one port of the hydraulic shifter. A variety of different hydraulic transducers can be used, For example, a rotary axial-piston hydraulic converter with phase control (as in U.S. Patent No. 6, 11 6, No. 138), Each of the cylinders acts as a motor during one part of the cycle, And during the other part of the cycle it acts as a pump, Or a multi-chamber linear hydraulic transformer with digital control (as in U.S. Patent No. 7, 47 5, 5 3 8). In a more compact embodiment, At least one accumulator combines the functions of a liquid accumulator and a hydraulic converter, As in US Patent No. 5, 971, No. 027. The accumulator contains at least two liquid reservoirs, The at least two liquid reservoirs are separated from a gas reservoir by a common piston divider. The inter-accumulator liquid transfer mechanism is constructed to create a liquid flow between at least one of the liquid reservoirs of the accumulator and at least one liquid reservoir of the other accumulator. To perform the conversion method under the pipeline that transfers the liquid from the pipeline having the first high pressure to the pipeline having the second highest pressure, The liquid supply and suction mechanism comprises first and second pipelines, And a hydraulic converter having at least three ports, Wherein the first and second pipelines can maintain the first and second pressures therein, respectively And the hydraulic converter is mounted such that the pressure in the liquid reservoir of the at least one accumulator is different from the first and second pressures in the first and second lines, -27- 201132851 Liquid exchange between the first and second lines and the liquid reservoir. To implement the above method under decoupling the load pressure from the first and second pressures in the first and second lines, The liquid supply and suction mechanism comprises a hydraulic transducer having at least four ports. The hydraulic converter is mounted to connect the two ports to the first and second lines. And connect the other two ports to the two output lines. And the pressure in the two output lines can be maintained to be different from the first and second pressures in the first and second lines. The details of the present invention are shown in the following examples shown by the drawings. [Embodiment] The main principle of the present invention is shown in Fig. 1 and an improvement of the main principle is shown in Fig. 2. 3 to 8 show a specific embodiment of the main components and parts. 装置 The apparatus according to Fig. 1 comprises two liquid gas accumulators 1 and 2, The liquid reservoirs 3 and 4 are in communication with the liquid supply and suction mechanism 14. The liquid reservoirs 3 and 4 are separated from the gas reservoirs 7 and 8 by movable partitions 5 and 6. The gas reservoirs 7 and 8 are in communication with the heating and cooling mechanism 9. For heating and cooling of the gas, the heating and cooling mechanism 9 includes a flow gas heat exchanger 10 and 1 1 . It is connected to the gas reservoirs 7 and 8 and the accumulators 1 and 2 via the gas line 12 and the valve 13. The heat exchanger 1 is constructed to be in thermal contact with an external heat source and can supply heat from the heat source to the gas. The heat exchanger 11 is constructed to be in thermal contact with the cooling heat transfer medium. Heat can be removed from the gas to the cooled heat transfer medium. -28- 201132851 The present invention provides for the utilization of various heat sources, Including internal combustion engines or external combustion engines, High temperature fuel tank, sun, Geothermal source, etc. And the direct heat of the exothermic reaction that is carried out in thermal contact with the hotter heat exchanger. Thermal contact with the heat source is effected by heat transfer or heat-and-mass transfer using a hot heat transfer medium or by radiant heat transfer and combinations thereof. The hot heat transfer medium is, for example, the exhaust of an internal combustion engine (ICE) or the exhaust steam of a steam turbine. Condensation heat transfer can also be used for heat and mass transfer. For example, during the heat recovery of the exhaust steam of the steam turbine or when using a heat pipe. Figure 3 shows an embodiment of a gas heat exchanger 1 (or 11), Thermal contact with the heat exchanger is carried out by heat and mass transfer. The heat exchanger includes an internal slot-type gas passage 15 that radially diverges from the inner axial passage 16. The majority of the internal axial passage 16 except the collector part 17 is blocked by the plug 18. The input and output of the gas is carried out via the port 19 of the flange 20 (the second flange is not shown). Preferably, the heat exchanger is 1 〇, 11 internal passage 15, The total gas volume in 16 should not exceed the gas reservoir of the accumulator 7, The maximum total gas volume in 8 is 1%. For heat supplied from an external heat source, The heat exchanger according to Fig. 3 comprises a helical outer channel 21, The heated heat transfer medium circulating between the heat exchanger 10 and the external heat source is pumped through the spiral outer passage 21 via an external port (not shown). Preferably, the heat exchanger 1 should be constructed and installed as a counterflow heat exchanger. The supply of heat from the heated heat transfer medium to the gas is such that heat is supplied from the external heat transfer medium exiting the heat exchanger 10 to the -29-201132851 gas entering the heat exchanger 10, The heat to the gas leaving the heat exchanger 10 is supplied from the external heat transfer medium entering the heat exchanger 10. in this way, At the same time, a more complete utilization of the heat of the external heat source and a higher degree of gas heating are achieved. The heat exchanger that cools the heat transfer medium and is pumped through the external passage is also implemented and installed in a similar manner. The gas heat exchanger 10 is heated by an external heat source to become hot. The gas heat exchanger 11 is cooled by the cooling heat transfer medium to become cold. For converting heat from an external heat source into fluid power, Gas compression and expansion combined with heat supply and removal, The average gas temperature is made higher during expansion than during compression. The following compression and expansion mean a change in gas density (increase or decrease in density, respectively) due to a change in the volume of the gas reservoir in at least one of the accumulators. The device according to Figure 1 can be used to implement isobaric in combination, Isochric, Converting heat into fluid power under a cycle of a polytropic phase close to adiabatic, The above cycle is, for example, an Otto cycle, Brayton cycle, Diesel cycle, Or other loops. below, The actual process in the gas cycle will be through an idealized phase (eg, thermal insulation, Isothermal Isobaric, Or equal volume) is described similarly. A change in gas density (by gas expansion or compression) under the passage of no gas through the heat exchanger will effect a variable expansion or compression approaching adiabatic expansion or compression with increased expansion or compression. Through a heat exchanger (a hotter heat exchanger) without a change in gas density (ie, at a gas discharge rate from one accumulator of -30 - 201132851 equal to the gas draw rate in another accumulator) The gas transfer of 10 or the cooler heat exchanger U) carries out an equal volume change of the gas temperature (heating or cooling, respectively). The gas transfer from one accumulator via the hotter heat exchanger 10 to the other accumulator is carried out under expansion (i.e., under the increase in the combined gas volume of the gas reservoirs 7 and 8). , For example, isostatic. In a similar way, Gas compression with cooling (e. g., isobaric) is carried out by gas transfer from one accumulator via a cooler heat exchanger U to another accumulator under compression. The proposed method of converting heat into fluid power is not limited to the cycle having the above-described idealized phase. It can be applied to all cycles in which the gas expansion work exceeds the gas compression work. An example of a cycle of converting heat to fluid power implemented in the device embodiment according to Fig. 1 comprises four stages, That is, the first stage of the variable gas compression in the gas reservoir of the first accumulator; a second stage of heat supply to the gas and gas heating during the passage of the gas through the hotter heat exchanger 10 to the other accumulator; a third stage of variable gas expansion in a gas reservoir of another accumulator; And the fourth stage of heat removal from the gas and gas cooling during the passage of the gas back to the first accumulator via the cooler heat exchanger 11. At the beginning of the first phase, The gas is discharged from the gas reservoir 8 of the accumulator 2 to the greatest extent through the cooler heat exchanger 11 to the gas reservoir 7 of the accumulator 1. result, The initial gas temperature is close to the temperature of the cooler heat exchanger 11. The liquid supply and suction mechanism 14 pump is completed -31 - 201132851 as a fluid to the liquid reservoir 3 of the accumulator 1, The variable gas compression is carried out in the gas reservoir 7 under the increase of the gas pressure and temperature. The variable gas compression ends at a gas temperature that is less than the temperature of the hotter heat exchanger 10. During the second phase, Pumping the working fluid into the liquid reservoir 3 and discharging the working fluid from the liquid reservoir 4, The gas is transferred from the gas reservoir 7 to the gas reservoir 8 via the valve 13 and the hotter heat exchanger 10, Heat is supplied to the compressed gas. The supply of heat is carried out under the heating and expansion of the gas, That is, it is carried out under the increase of the total volume of the gas in the gas reservoirs 7 and 8. The amount of the working fluid discharged from the liquid reservoir 4 of the accumulator 2 to the liquid supply and suction mechanism 14 is larger than the amount of the working fluid pumped from the liquid supply and suction mechanism 14 to the liquid reservoir 3 of the accumulator 1. . Preferably, The gas transfer is carried out until the maximum discharge of the gas is discharged from the gas reservoir 7 of the accumulator 1. In the third stage, The liquid is discharged from the liquid reservoir 4 of the accumulator 2 to the liquid supply and suction mechanism 14, Further gas expansion is carried out in the gas reservoir 8 of the accumulator 2. at this time, The pressure and temperature of the gas are reduced. The variable gas expansion ends at the temperature of the gas at a relatively high temperature of the relatively hot heat exchanger 10. During the fourth phase, After the working fluid is pumped into the liquid reservoir 4 and the working liquid is discharged from the liquid reservoir 3, By transferring gas from the gas reservoir 8 to the gas reservoir 7 via the cooler heat exchanger 11 and valve 13, Heat is removed from the expanded gas. The removal of heat is carried out under the cooling and compression of the gas. That is, it is carried out under the reduction of the total gas volume in the gas reservoirs 8 and 7. The amount of working fluid discharged from the liquid reservoir 3 of the accumulator 1 to the liquid supply and suction mechanism 14 is smaller than that from the liquid supply and the pumping mechanism 14 is pumped into the liquid reservoir 4 of the accumulator 2 from -32 to 201132851 The amount of working fluid. The average temperature and average pressure of the gas during the expansion of the second and third stages are higher during the compression periods of the first and fourth stages. therefore, The gas expansion work exceeds the gas compression work. During the second and third phases, The fluid supply and suction mechanism 14 receives more fluid power than the liquid discharged from the accumulator during the first and fourth stages to pump the working fluid into the accumulator. result, Some parts of the heat are converted into additional fluid power, It is used by a liquid supply and suction mechanism 14 for example a load 'hydraulic motor, Or mechanical work in a hydraulic cylinder. The liquid supply and suction mechanism 14 can have a variety of different embodiments. These include separate pumps and hydraulic motors as well as hydraulic transformers. The main principles of the invention described above are implemented with greater efficiency using the improvements embodied in the embodiment of the apparatus of Fig. 2. In the device according to Figure 2, The heating and cooling mechanism 9 includes a check valve 22, It is installed such that gas is passed through the cooler heat exchanger 11 and only into the gas reservoir 7 of the accumulator 1 Therefore, the wall portion of the gas reservoir 7 is kept cold. The hotter heat exchanger 10 is mounted such that gas is passed from the gas reservoir 7 through the heat exchanger 10 to the gas reservoir 8, And being transferred from the heat exchanger 10 to the gas reservoir 23 of the third accumulator 24, The wall portions of the gas reservoirs 8 and 23 are thus kept relatively hot. In other embodiments having three or more accumulators, The heat and the wall of the device are stored in the heat exchanger of the gas exchange of the body and the gas is less than the gas. The heating and cooling mechanism 9 also includes a liquid flow heat exchanger 25 and a check valve 26. The heating and cooling mechanism 9 also includes a liquid flow heat exchanger 25 and a check valve 26. The heat exchanger 25 is heated by heat from an external heat source. For example, by means of a hot heat transfer medium, the liquid reservoir 4 of the accumulator 2 or the liquid reservoir 27 of the accumulator 24 is introduced, The working liquid of 28 passes through the heated liquid heat exchanger 25, The walls of these liquid reservoirs and the working fluid therein are thus kept hot. at this time, The wall portion of the liquid reservoir 3 of the accumulator 1 and the liquid therein are kept cold. in this way, The accumulators 2 and 24 are kept hot as a whole, The entire accumulator 1 is kept cold. Other embodiments may include a cooling liquid heat exchanger, So that the working fluid is pumped to the accumulator with the cooler gas reservoir wall (eg Figure 1, The liquid reservoir of the accumulator 1) of Figure 2 is passed through the coolant heat exchanger. Other embodiments may also include an accumulator provided with a heat exchanger for directly heating or cooling the wall of the accumulator. In the device according to Figure 2, The liquid supply and suction mechanism 14 includes a liquid regenerative heat exchanger 29 and a heat-insulating buffer 30. In other embodiments, It is possible to use only liquid regenerative heat exchangers or only thermal insulation buffers. a liquid regenerative heat exchanger 29 and a liquid reservoir 4 of two hotter accumulators, 27. And 28 connections, Heat may be removed from the liquid during the passage of liquid from the accumulator through the liquid regenerative heat exchanger 29 to the thermal insulation buffer 30. And the removed heat is supplied to the liquid as it is reversely transferred from the buffer 30 to the accumulators. The working fluid is cooled as it is transferred from the liquid to the heat exchanger 29 as it is directed from the hotter accumulator 2 or 24 through the heat exchanger 29. The opposite direction is directed through the same heat exchanger 29 to the hotter product -34 - 201132851 The working liquid in the accumulator 2 or 24 is heated by the heat transferred from the heat exchanger 29 to the liquid. in this way, The temperature of the working liquid introduced to the thermally insulating liquid buffer 30 containing the two variable volume liquid reservoirs 31 and 32 separated by the movable thermal insulator 33 is lowered. "High temperature working liquid (for example organic or organic) The use of an organic-silicon working liquid allows the temperature to be raised to a temperature of 3 ° C and higher. For the use of different working fluids in cold and heat accumulators, Separate liquid buffers can be applied, It contains two variable volume reservoirs separated by a movable partition. Or, The liquid damper 30 can be constructed to have a liquid-tight movable thermal insulation partition 33. The liquid regenerative heat exchanger 29 can have a variety of different embodiments. Including a regenerative component that is mounted inside the rugged enclosure, And in the form of a single element (e.g., in the form of a long tube) that is made to have a high heat capacity and has a low heat transfer from its hotter portion to the cooler portion. In the integrated embodiment according to Fig. 4, the liquid regenerative heat exchanger 29 of Fig. 2 and the liquid thermal insulation buffer 30 are implemented in a common strong outer casing 34, The strong outer casing 34 has liquid ports 35 and 36 on its flange. The inside of the strong outer casing 34 has a thin-walled metal sleeve 37, The movable thermal insulator 33 in the form of a long hollow piston 38 is slidably mounted in the sleeve 37. The variable volume reservoirs 3 1 and 3 2 are separated by high temperature and low temperature. In the space 39 between the strong outer casing 34 and the metal sleeve 37, Placed with a dip 40 (such as mineral wool or foained polymer), To prevent convection of a high temperature liquid having a low heat transfer coefficient that fills the space. The cavity 41 inside the hollow piston 38 also contains a crucible 40 and a high temperature liquid having a low heat transfer coefficient of -35 to 201132851. In this case, This liquid is a working liquid that is filled through the hole 42 of the sleeve 37 and the hole 43 of the wall portion of the hollow piston 38. This liquid provides a thin walled hydrostatic unloading of the thin sleeve 37 and the piston 38. In other embodiments, A solid thermal insulation insert made of a high temperature material having a low heat transfer coefficient (preferably less than 1 W/mK) can be used. For example, made of high temperature plastic (such as polyimide), Instead of the thin-walled metal sleeve 37 and the insulating liquid layer separated by the metal sleeve 37 along the strong outer casing 34. The movable thermal insulator 33 can also be made of a similar solid material having a low heat transfer coefficient. The high temperature variable volume reservoir 32 is in communication with the flow portion 44 of the liquid regeneration heat exchanger 29 that is filled with the regeneration element 45. In this case, An embodiment of the regenerative element 45 is in the form of a ball member made of a metal having a high thermal conductivity, such as aluminum. To reduce the size, The regeneration element 45 can contain a phase transition during heat exchange with the passing liquid (e.g., Melting during the removal of heat from the liquid, The material that crystallizes during the supply of heat to the liquid. In the embodiment according to Fig. 2, The gas heat exchanger 10 is constructed as a separate component and is installed between the accumulator 2 and the accumulator 24, Gas can be transferred from the smaller gas reservoir 8 of the accumulator 2 through the heat exchanger 10 to the larger gas reservoir 23 of the accumulator 24. Therefore, the gas expansion process is closer to the isothermal expansion process. To ensure low pressure loss during miniaturization and gas transfer, According to the embodiment of Fig. 5, The gas heat exchanger 10 and the accumulator 2 are constructed in the same casing to become the gas ports of the accumulator and have an increased heat exchange surface area. Heat exchanger -36- 201132851 ίο an external passage 21 for the heat transfer medium for heating, a strong outer casing 46 shared with the accumulator 2, And an internal heat exchange section 47 made of a metal having a high heat transfer coefficient, preferably copper or aluminum. In the internal heat exchange section 47, An internal groove type gas passage 15 radially diverging from the axial passage 16 is formed, The majority of the axial passage 16 except the collector portion 17 is blocked by the plug 18. In an embodiment with two hotter accumulators according to Figure 2, During the transfer of gas from the cooler accumulator 1 to the hotter accumulator 2, And during the passage of gas from the smaller, hotter accumulator 2 to the larger, hotter accumulator 24, The gas is passed through this hotter heat exchanger 1〇. Similarly, In other embodiments, The cooler gas heat exchanger 1 1 can be implemented in the same housing together with the cooler accumulator 1 . The heating and cooling mechanism 9 according to Fig. 2 comprises a gas blower 48, It is installed to generate forced convection in the gas reservoir 7 of the cooler accumulator 1. The gas reservoir 7 is in communication with the heating and cooling mechanism 9 via at least two gas lines 49 and 50, The gas can thus be removed from the gas reservoir 7 via the gas line 49 by means of a gas blower 48, Passing the removed gas through the cooler flowing gas heat exchanger 11, And returning the gas to the same gas reservoir 7 via another gas line 50. In other embodiments having an external heat exchanger, The gas blower can be placed in the housing of the accumulator, And can generate forced convection without gas transfer through the external heat exchanger, Therefore, the gas is compressed or expanded closer to the isothermal process only due to heat exchange with the wall portion of the gas reservoir. The liquid supply and suction mechanism 14 according to Fig. 2 comprises a hydraulic motor 51 which is kinematically connected to the gas blower 48 by means of a shaft member 52-37-201132851. In other embodiments, The kinematic connection of the hydraulic motor to the gas blower may include a gearbox for increasing the rate of rotation of the gas blower. The hydraulic motor 51 is connected to the liquid line 67 via the valve 103. Thus, the liquid flow between the hydraulic motor and the liquid reservoir 3 of the accumulator 1 can be actuated. In the integrated embodiment according to Fig. 6, Both the flowing gas heat exchanger 11 and the centrifugal gas blower 48 are implemented in the same casing together with the accumulator 1". The gas blower 48 is connected to the hydraulic motor 51 by the shaft member 52. Check valve 22 (Fig. 2) is not shown in Fig. 6. One of the check valves can be implemented as a disc valve installed at the surface of the internal heat exchange section 47, Thus, the heat exchange tank communication path 15 can be blocked. Another check valve can be installed in the axial passage 16. This integrated embodiment enhances miniaturization and eliminates the need for gas lines. Therefore, the total gas dynamic resistance is lowered. When the working fluid is pumped into the liquid reservoir 3 of the accumulator 1, A working fluid actuated hydraulic motor 51 and a gas blower 48» centrifugal gas blower 48 (Fig. 6) that is kinematically coupled to the hydraulic motor 51 draws gas from the gas reservoir 7 via the axial passage 16. And pumping the gas into the groove type passage 15 of the heat exchanger 11, The gas is returned from the groove-type passage 15 to the gas reservoir 7 to generate forced convection in the gas reservoir 7. The enhanced heat exchange between the gas and the wall of the gas reservoir 7 and the surface of the channel-type passage 15 causes the gas compression process within the gas reservoir to approach the isothermal process. The liquid actuating the hydraulic motor 51 has a close pressure and a close temperature to the gas pumped by the gas blower 48. This promotes good operation of the seal of the shaft member 52. In other embodiments, The gas blower can be mounted to create forced convection in the gas reservoir of the hotter accumulator. and, In other embodiments, The gas blower can be kinematically coupled to an electric motor located in a high pressure cavity that is preferably filled with liquid. The device according to Fig. 2 comprises a regenerative flowing gas heat exchanger 53, And when the gas is passed through the regenerative heat exchanger 53 to the cooler accumulator 1, Heat is removed from the gas to the regenerative heat exchanger 53, And when the gas is passed through the regenerative heat exchanger 53 in the opposite direction (i.e., from the cooler accumulator 1 to the hotter accumulator 2), The heat removed from the gas is supplied back to the gas from the regenerative heat exchanger S3. in this way, The portion of the gas that has entered the regenerative heat exchanger 53 from the cooler accumulator 1 becomes colder. The opposite portion of the gas entering from the hotter accumulator 2 or 24 becomes hotter. During the cooling phase, Heat from the gas is supplied to the regenerative heat exchanger 53, And then supplied to the cooling heat transfer medium via the cooler heat exchanger 11. During the heating phase, The heat is first supplied from the regenerative heat exchanger 53 to the gas, It is then supplied to the gas from an external heat source via the hotter heat exchanger 10. Preferably, the total volume of gas in the regenerative heat exchanger 53 should not exceed 10% of the maximum total gas volume in the gas reservoir of the accumulator. again: The heat capacity of the raw heat exchanger 53 exceeds the maximum combined heat capacity of the gas (preferably not less than twice). Configuration of the regenerative heat exchanger (length, Longitudinal section And the transverse cross section) and the heat transfer coefficient of the material of the regenerative heat exchanger are selected such that heat transfer from its hotter portion to its cooler portion is less than from gas-39-201132851 to cooler heat exchanger 11 Preferably, the heat transfer of the cooling heat transfer medium is Less than 30% of the latter heat transfer). The regenerative heat exchanger 53 has various different embodiments. Includes regenerative components mounted inside a strong hermetic seal housing, And with a small internal volume, High heat capacity, And a simple implementer of a single component that transfers heat from the hotter portion to the cooler portion. In a particular embodiment according to Figure 7, The regeneration gas heat exchanger 53 includes a strong outer casing 54, It has a thermally insulating insert 55, The re-elements 56 are placed inside the thermally insulating insert in the form of a spiral sheet 57. Wherein the gap between the spiral sheet layers is determined by the spacers 58. The gas exchanges heat with the surface of the regenerative element as it flows through the gaps. And depending on the direction of the transfer it becomes colder or hotter. In this embodiment, The metal foil (preferably made of a metal having a low heat transfer coefficient such as stainless steel). To reduce the longitudinal heat transfer coefficient, Sheet 57 has perforations 5 9, To separate the regenerative elements into several segments, There is an increased thermal resistance in the region of the perforations 59 between the segments. In other embodiments the regenerative element can be made of a high temperature plastic that does not have perforations. An insulating or thermally insulating insert 55 made of a high temperature plastic ceramic reduces the heat loss of the heat and cooling of the strong outer casing 54. In other embodiments, A thermal insulation fluid layer can be used in place of the thermal insulation insert 55, The liquid is partially separated by a gas in the regenerative element by means of a thin metal sleeve (similar to the layer of insulating liquid in the liquid reheat exchanger 29 according to Figure 4). In other embodiments, A part of the heat exchanger 1 〇 (or 1 1 ) is used as the gas regenerative heat exchanger 53. For this purpose, Additional gas ports are formed in such a heat exchanger to introduce gas into the heat exchanger. The amount of change can be changed 55 〇 by > -40- 201132851 The heating and cooling mechanism comprises connecting the above additional gas port to the gas reservoir 23 (or the gas reservoir 7) at least one passage, It also includes a valve that is installed to lock this passage. The thermal regeneration combined with the relatively similar isothermal process of compressing and expanding provides a thermodynamic efficiency that converts heat into work performed by the gas during discharge of the liquid from the accumulator. The liquid supply and suction mechanism 14 according to Fig. 2 includes a hydraulic converter 60 and a valve 61, 62. And 63, The hydraulic converter 60 and the valve 61, 62. And 63 together with the liquid lines 64 to 67 form an inter-accumulator liquid transfer mechanism, It can be in the accumulator 1, 2, A liquid flow is created between the liquid reservoirs of 24 and 24 . The hydraulic converter 60 has three liquid ports 68, 69. And 70* port 68 is connected to the liquid reservoir 3 of the accumulator 1 via valves 63 and 103. The port 69 is via the valve 62, 26. And 61, The liquid thermal insulation buffer 30' and the regenerative liquid heat exchanger 29 are connected to the liquid reservoir 4 of the accumulator 2 or to the liquid reservoirs 27 and 28 of the accumulator 24. The third port 70 of the hydraulic transformer 60 is connected to the liquid line 71. When liquid flows through the third port 70, The liquid flow is generated between the port 68 of the hydraulic transformer 60 and the port 69. And thus between the liquid reservoirs of the accumulator communicating with the ports. The accumulator 24 according to Fig. 2 is like U.S. Patent No. 5, 971, It was implemented on the 27th, And combined with the function of the liquid gas accumulator and the hydraulic converter. The accumulator 24 has three ports (a gas port 72 and liquid ports 73 and 74). Also included are two liquid reservoirs 27 and 28 separated from a gas-41 - 201132851 body reservoir 23 by a common piston divider 75. The inter-accumulator liquid transfer mechanism includes a valve 61 and lines 64 and 65, A liquid flow is generated between the liquid reservoir 27 of the accumulator 24 and the liquid reservoir 4 of the accumulator 2. The liquid reservoirs 27 and 28 are spaced apart from each other. This allows for different pressures in the two, The total force of the liquid pressure on the partition 75 is balanced with the force of the gas pressure on the partition 75. When gas is transferred from the gas reservoir 8 of the accumulator 2 to the gas reservoir 23, The reverse flow of liquid is generated from the liquid reservoir 27 into the liquid reservoir 4 of the accumulator 2, Therefore, the pressure in the liquid reservoir 4 is maintained higher than the pressure in the gas reservoir 23. in this way, The pressure in the other liquid reservoir 28 connected to the hydraulic pressure converter 76 via the valve 62 (and via the regenerative heat exchanger 29 and the thermal insulation buffer 30) is maintained at a lower level than in the gas reservoir 23. . By changing the port through the hydraulic converter 76 7 7 8. And the ratio between the traffic of 79, The pressure of the liquid flowing through the port 77 connected to the liquid reservoir 28 is changed. therefore, By the hydraulic converter 76, The pressure in the liquid reservoir 28 is kept low relative to the gas pressure in the gas reservoir 23. Due to the above-described balance of forces acting on the spacer 75, . The pressure in the liquid reservoir 27 becomes increased relative to the pressure of the gas in the gas reservoir 23. Under the mutual gas and liquid transfer rate between the accumulator 2 and the accumulator 24, the liquid pressure in the liquid reservoir 27 is higher than the relative excess of the gas pressure in the gas reservoir 23. The pressure drop on the partitions 75 and 6 caused by the friction and the total pressure drop caused by the impedance of the gas-liquid circuit passing through the gas transfer and the reverse flow of the liquid. The circuit includes gas and liquid ports for accumulators 1, 2, and 24, gas - 42 - 201132851 heat exchanger 10, and valves and lines. Since the circuit accumulator 2 and the accumulator 24 are mutually increased in gas and liquid, the above-described pressure excess of the pressure in the liquid reservoir body reservoir 23 is reduced as the transmission rate is increased, and the above pressure is reduced. The excess 値 is reduced. In other embodiments, such a plurality of liquids are used as the second, cooler accumulator (or the accumulator 2 of the example is the only hot accumulator). During the passage of gas from the accumulator back into the accumulator 1 of Figure 1 in the smaller accumulator, one (or several) streams of liquid from the smaller reservoir to the accumulator are generated to be placed in the liquid reservoir. The pressure is maintained at another liquid reservoir of the accumulator than the gas (or several other pressures are also maintained at a higher pressure than the gas by, for example, a hydraulic transducer. This is combined with the liquid reservoir of the accumulator and the hydraulic transducer) An integrated accumulator embodiment reduces the loss of delivery and increases the miniaturization of the device. The accumulator can house a plurality of liquid reservoirs in a housing. From the perspective of the present invention, the actual number of such integrations is equal to The number of individual pieces between the gas reservoir and the liquid reservoir. The gas is transferred from the accumulator 2 and the accumulator 1 between the accumulator 2 and the accumulator 1 under the heat supply from the regenerative heat exchanger 53. 63 is used to increase the pressure drop on the accumulator 2 with the increase of the body transfer rate in relation to the gas, and the accumulator for the reservoir can be replaced as in Fig. 1 in this case, for example ( Return to the liquid of the accumulator according to The reverse liquid pressure of the body reservoir is low. At this time, the function in the gas reservoir in the liquid reservoir has two integrated reservoirs for accumulating liquid between the accumulators and accumulators in several gas embodiments. During the separation of the site movement and the hotter heat exchange period, between the hydraulic pressure and the accumulator 1 -43- 201132851 generates a liquid flow, and the heat is removed from the gas to the regenerative heat exchanger 53 and the cold heat exchange During the transfer between the accumulator 24 and the accumulator 1, the hydraulic pressure converter 60 and the valves 62, 63 are used in the liquid reservoirs 27, 28 of the accumulator 24 and the liquid reservoir 3 of the accumulator 1. A liquid flow is created between. During the transfer of gas from the gas reservoir 7 to the gas reservoir 8, the liquid reservoir 3 is connected to the port 68 (via valves 103, 63) and the liquid reservoir 4 is connected to the port 69 ( The liquid pressure in the liquid reservoir 3 is maintained in the gas reservoir 7 by the hydraulic pressure converter 60 via the valves 61, 26, and 62, the liquid regenerative heat exchanger 29, and the liquid thermal insulation buffer 30). The high pressure helium, the gas is discharged from the accumulator 1 to the accumulator 2, and The moving liquid stream is discharged through the third port 70 of the hydraulic converter 60, the line 71, and the check valve 97 to below the line 90, and the reverse liquid flow is generated through the ports 68, 69 of the hydraulic converter 60 to generate savings. Between the device 2 and the accumulator 1. When gas is transferred from the gas reservoir 23 to the gas reservoir 7 of the accumulator 1, both of the liquid reservoirs 27 and 28 are connected to the port 69 of the hydraulic converter 60 (via Valves 61 and 62, liquid regenerative heat exchanger 29, and liquid thermal insulation damper 30). The hydraulic pressure converter 60 maintains the liquid pressure in these liquid reservoirs at a higher pressure than the gas pressure in the gas reservoir 23. Next, the gas is discharged from the accumulator 24 to the accumulator 1, and the differential liquid flow is transmitted from the line 89 through the third port 70 of the hydraulic pressure converter 60, the line 71, and the check valve 97, resulting in savings from the accumulation. The liquid reservoir 3 of the device 1 passes through the ports 68, 69 of the hydraulic transducer 60 to the reverse liquid flow in the liquid reservoirs 27 and 28. Therefore, in both cases, the hydraulic converter 60 is -44-201132851 to allow for overcoming the gas and liquid ports, gas and liquid heat exchangers, liquid dampers, valves, including the accumulators 1, 2, 24. And the total pressure drop of the impedance of the gas-liquid circuit of the pipeline and the additional pressure drop caused by the friction of the separator. In the embodiment according to Fig. 2, the hydraulic transducer 60 is constructed as a variable hydraulic transducer that varies the ratio between the flow of liquid through its ports 68, 69, 70 and can then maintain these liquid flows The difference between the liquid pressures. In other embodiments, the hydraulic transducer 60 used for the transfer of liquid between the accumulators can be constructed as a non-adjustable hydraulic transducer, i.e., having a constant ratio of liquid flow through its ports, such as, for example, savings The device 24 includes three liquid reservoirs separated by a divider. Figure 8 shows an integrated embodiment of such a hydraulic transducer in combination with a thermally insulating liquid damper. The two liquid reservoirs 80 and 81 of the hydraulic converter are separated from the larger liquid reservoir 83 by a common thermally insulated piston divider 82. The thermally insulating piston spacer 82 slides along a thermally insulating insert 84 mounted inside the strong outer casing 85. During the transfer of gas and liquid between the accumulators, the reservoirs 81 and 83 are used to exchange liquid with the liquid reservoirs of the accumulators in which the liquid is being transferred. The larger reservoir 83 is connected to a hotter accumulator (e.g., accumulator 2 or 24 of Figure 2) and exchanges hotter liquid therewith. The smaller reservoir 81 is connected to a cooler accumulator (e.g., accumulator 1 of Figure 2) and exchanges cooler liquid therewith. The ratio of the cross-sectional areas of the reservoirs 83 and 81 is equal to the extent to which the gas volume changes during the phase in which the gas is transferred between the cooler and hotter accumulators via the heat exchanger. The cross-sectional area of the third reservoir 80 is equal to the difference between the cross-sectional areas of the reservoirs 83 and 81. Thus -45- 87 201132851 'The liquid flow through the liquid port 86 is equal to the difference between the liquid flow through the port 88 and the port. The third reservoir 80 is used to draw a differential liquid stream during body transfer under compression and to discharge a differential liquid stream during gas transfer under expansion. The thermally insulating piston spacer 82 and the insert are made of a thermally insulating material (e.g., polyimide or other high temperature plastic) to reduce the amount of hot liquid within the reservoir 83 and the cooler within the reservoirs 80 and 81. Heat transfer through the separator and the insert. The long sliding contact between the piston divider 82 inserts 84 reduces the heat loss from the cyclic heating and cooling of the portion of the surface of the thermally insulating insert 84 that is in contact with the hotter liquid within the reservoir 83. As for the use of such an integrated embodiment as a thermal rim buffer, only the smaller liquid reservoirs 80 and 81 are interconnected. The integrated embodiment results in a reduction in overall hydrodynamic impedance and better miniaturization. In the case of all of the above-described liquid flow generation between accumulators, the mutual exchange rate of gas and liquid between the accumulators is changed by, for example, by adjusting individual hydraulic converters or other hydraulic mechanical mechanisms to change the respective savings. The force in the liquid reservoir above the gas pressure in the gas reservoir of the same accumulator is excessively altered. The above mutual exchange rate can also be changed by changing the degree of change in gas temperature during gas transfer (e.g., by changing the temperature of the heat exchanger or 11.). The flow rate of the liquid flow between the accumulators is selected such that the pressure difference between any portion of the liquid in the accumulator (caused by the impedance of the above-described circuit and the friction of the seal of the hydraulic converter) does not exceed a few bars. Preferably no more than 1 bar. Because the working pressure of the gas and liquid in the accumulator is tens and hundreds of bars, the gas delivery in the liquid flow is liquid and the excess of the body fluid of the accumulating section -46-201132851 The pressure difference between any portion of the body does not exceed 30% of the liquid pressure in the liquid reservoir to which the liquid is pumped, preferably the pressure difference does not exceed 5% of the liquid pressure. The liquid supply and suction mechanism 14 according to Fig. 2 comprises a first line 89 and a second line 90 equipped with accumulators 91 and 92, and can maintain different pressures in these lines (in line 89 - in the first specified range) a first pressure change, and a replenishment pump 93 having valves 94 and 95 in line 90 - a second pressure change in the second specified range, and including three ports 77' 78, And hydraulic converter 76 of 79. Two ports 78 and 79 are connected to lines 89 and 90. The third port 77 is connected to the liquid reservoir 3 of the accumulator 1 and the liquid reservoirs 27 and 28 of the accumulator 24 via valves 63, 62, and 61. The hydraulic transformer 76 is implemented as a variable hydraulic pressure converter so that the ratio between the liquid flows through the ports of the hydraulic converter (continuously or stepwise) can be varied and then changed within the ports The ratio between the pressures. Thus, during the phase of gas pressure change, the hydraulic converter 76 ensures that the two lines 89, 90 and the accumulator are at a different pressure than the given first and second pressures in lines 89, 90. The possibility of liquid exchange between the liquid reservoirs 1, 2, or 24, the first and second pressures in the lines 89, 90 are all maintained at high enthalpy (preferably tens or hundreds of bars) And the second pressure is higher than the first pressure. In order to stabilize the pressure in the lines 89, 90, accumulators 91, 92 having a working volume larger than the total working volume of the accumulators 1, 2, and 24 are utilized. When the device is brought to its initial state, the supplemental pump 93 delivers liquid from the tank 96 via the -47-201132851 valves 94, 95 to the accumulators 91, 92 'up to the pressures in the first and second lines 89, 90 They are set in the specified first and second ranges, respectively. The conversion is carried out as a cycle which is contained in a gas compression stage in the accumulator 1 having a cooler gas reservoir 7, and the gas is transferred from the accumulator 1 via the hotter heat exchanger 10 to the accumulator 2 The gas transfer phase in the gas, the gas transfer phase from the accumulator 2 to the accumulator 24, and the gas from the accumulator 24 via the gas expansion in the hot gas reservoirs 8 and 23 of the accumulators 2 and 24 The cold heat exchanger 11 is transferred to the gas transfer stage in the accumulator 1. The working fluid is pumped into the liquid reservoir 3 of the accumulator 1 by means of a hydraulic transducer 76 actuated by the flow of liquid from the line 90 through the port 79 of the hydraulic transducer 76, the gas in the accumulator 1 being The pressure below the pressure in line 89 is compressed to a pressure above the pressure in line 90. During gas compression, the pressure of the liquid in the liquid reservoir 3 of the accumulator 1 is raised by the adjustment of the hydraulic transducer 76, i.e., by the passage from the line 90 to the liquid transducer 76 via the port 79. The flow rate of the liquid is increased for the ratio of the flow rate of the liquid discharged from the liquid transformer 76 to the accumulator 1 via the port 77. The hydraulic motor 51 actuates the gas blower 48, which pumps the gas through the heat exchanger 11, which causes heat to be removed from the gas and brings the gas compression process closer to the isothermal process. After the liquid pressure in the liquid reservoir 3 has been raised to a pressure above the second pressure (pressure in the second line 90), the valves 62 and 63 are switched to the gas being transferred from the accumulator 1 to the accumulator 2 The gas transfer phase -48 - 201132851 'and this is carried out in the case where the working fluid pressure in the accumulator exceeds the second pressure. The working fluid flow from the liquid reservoir 4 of the accumulator 2 to the line 90 actuates the hydraulic converter 60, which produces a working fluid flow from the accumulator 2 to the accumulator 1. As a result, the gas is discharged from the gas reservoir 7 into the gas reservoir 8. In this case, the gas is passed through the check valve 22, the regeneration gas heat exchanger 53, and the hotter heat exchanger 1A. Since heat is supplied from the regenerative heat exchanger 53 and the hotter heat exchanger 1 to the gas, the gas is continued and the expansion approaches the isobaric process. The gas is discharged from the liquid reservoir 28 through the hydraulic shift 76 to the line 89 to actuate the hydraulic converter 76 and to produce a flow of working liquid from the hydraulic shift 76 to the line 90, the gas having a hotter gas reservoir 8, 23 The accumulators 2, 24 expand from a pressure exceeding the pressure in the line 90 to a pressure below the pressure in the first line 89. During gas expansion, the liquid pressure in the liquid reservoirs 28, 27, 4 of the accumulators 24 and 2 is reduced by the adjustment of the hydraulic transducer 76, i.e., by increasing the liquid reservoir 28 of the accumulator 24. The flow rate of the liquid that is delivered to the hydraulic pressure conversion 76 by the port 77 is reduced by the ratio of the flow rate of the liquid that is discharged from the hydraulic pressure converter 76 to the line 90 via the port 79. The pressure of the liquid flowing from the liquid reservoir through the port 77 of the hydraulic transformer 76 is kept lower than the pressure of the gas in the gas reservoir 23. At the same time, the other accumulator 24, another liquid reservoir 27, generates a force higher than the gas pressure as the liquid is being transferred from the liquid reservoir 27 of the accumulator 24 to the liquid reservoir 4 of the accumulator 2. The supply of gas to the gas during the passage of the gas through the heat exchanger 1 brings the gas expansion process closer to the isothermal process. The liquid pressure of the liquid body of the expansion device is increased to 49. The pressure in the liquid reservoir 3 has been reduced to the first pressure (the pressure in the first line 89). After the following pressures, the valves 61, 62 and 63 are switched to a gas transfer stage in which the gas is transferred from the accumulator 24 having the hotter gas reservoir 23 to the accumulator 1 having the cooler gas reservoir 7. This is done in the case where the working fluid pressure in the accumulator is below the first pressure. The working fluid flow from line 89 (via respective check valves 97) to the liquid reservoirs 27, 28 of accumulator 24 actuates hydraulic output 60, which produces a flow of working fluid from accumulator 1 to accumulator 24. Therefore, the gas is discharged from the gas reservoir 23 into the gas reservoir 7. In this case, the gas is passed through the regeneration gas heat exchanger 53, the cooler heat exchanger 11, and the respective check valves 22. Since heat is removed from the gas to the regenerative heat exchanger 53 and the cooler heat exchanger 11, the gas is cooled and compressed, and the process approaches the isobaric process. As a result of each conversion cycle, portions of the working fluid are transferred from line 89 having a first pressure to line 90 having a second, higher pressure. The approaching isothermal process of compression and expansion and the gas thermal regeneration between the isobaric compression stage and the isostatic expansion stage bring the gas cycle to an Ericsson cycle of the second type (two One isothermal phase and two isobaric phases, and there is thermal regeneration between the two isobaric phases). The closer the gas compression and expansion is to isothermal and the closer the thermal regeneration rate is to 100%, the closer the thermodynamic efficiency of this cycle is to the thermodynamic limit, ie the closer to the Carnot cycle efficiency. The sliding seals of the hydraulic transducers 60 and 76 (and the seal of the separator 75 of the accumulator 24) are operated at a differential pressure rather than a full pressure, which is reduced by the leakage of -5032 to 201132851 due to leakage and friction, and The hydrostatic machine that increases the conversion 〇 The liquid supply and suction mechanism 14 according to Fig. 2 also includes a hydraulic transducer 98 having ports 99, 100, 101, 102. The two passes [and 100 are connected to the first and second lines 89, 90, while the other two 101 and 102 are connected to the two output lines 104 and 105. The hydraulic variable 98 is implemented as a regulated hydraulic transducer that maintains the pressure within the output line, 105, as different from within the first and second lines 89,90. The above-described process of converting heat to fluid power includes a stage of supplying liquid from the first and second lines 89, 90 to the accumulator 1 and drawing the liquid from the accumulator 2' 24 to the stages 89, 90. Therefore, the pressure within these lines is subject to cyclical changes within the specified first and pressure ranges. The pressure conversion rate within the hydraulic converter ensures that the power delivered to the load 106 is related to these cyclical pressures. When the first or second pressure is exceeded by the hydraulic strainer 76 or 98 beyond the specified range, these pressures are recovered by the supplemental pump 93 and the valve 94. Therefore, the pressure is isolated to optimize the gas circulation rate by the selection of the given first and second pressures in tubes I, 90, and by the highs in lines 1〇4, 105. The selection of the low output optimizes the load 106. As a result, the heat transferred from the heat source to the gas with a small loss is converted into gas work with high mechanical efficiency, and the gas work is converted into fluid power transmitted to the load with hydraulic mechanical efficiency. Therefore, the proposed method of converting heat into fluid power and its efficiency are four] 99 port changer 10 04 pressure alternating, second control within 2 4 without leakage and "5 I 89 effective pressure The implementation of the high heat -51 - 201132851 The device provides: - high heat utilization, because the gas transfer between the accumulators via the heat exchanger eliminates the heat loss of the cyclic heating and cooling of the bulky components, especially with the elimination and accumulator The heat exchange of the heat exchange of the walls is combined with the heat loss of the gas exchanged with the liquid by the heat preservation or regeneration of the working liquid; - the high heat supplied to the gas is converted into a gas The thermodynamic efficiency of the gas cycle of the work, in particular in combination with the thermal regeneration of the gas, and in combination with the gas compression or expansion process approaching the isothermal process; - the high hydromechanical efficiency of converting gas work into fluid power, because of the accumulator The liquid transfer between the two has a small pressure difference by means of a hydraulic converter, in particular with a small pressure difference between the accumulator and the line. In combination with gas compression or expansion, respectively, using a hydraulic transducer for liquid supply or suction; - high conversion of heat into the efficiency of the fluid power delivered to the load, because of the combination of the elements described above, especially with A hydraulic transducer is used to ensure that the pressure in the line that exchanges the liquid with the accumulator is converted into a pressure in the line that exchanges the liquid with the load; - high power density due to high gas and liquid pressure and High conversion efficiency; - Increased reliability 'because cyclic heating and cooling of components under high pressure are eliminated; - Accumulation of heat in bulky heat exchangers and use of savings during temporary shutdown or deactivation of heat source power The heat is converted to a hydrodynamic -52-201132851 possibility. It will be appreciated by those skilled in the art that this detailed description is only an example, and many other variations that are within the scope of the invention may be presented, including, for example, but not limited to, the types of gas cycles not specifically recited herein. Implementation of different methods, different choices of working fluids and gases, and different types of external heat sources and cooling heat transfer media and specific characteristics of their thermal contact; and accumulators, gas and liquid heat exchangers, gas blowers, including hydraulic shifts The liquid supply and suction mechanism of the device and the damper, and the number of other components of the device and the device embodiments different from the embodiment; and the variation of the integrated embodiment of the components of the device not described above. [Simplified illustration] Figure 1 shows a device with two accumulators and two heat exchangers. Figure 2 shows a device with three accumulators, a gas blower, a gas regenerative heat exchanger, a liquid heat exchanger, and a liquid thermal insulation buffer with a hydraulic transducer. Figure 3 shows a gas flow heat exchanger. Figure 4 shows an integrated embodiment of a liquid regenerative heat exchanger and a liquid thermal insulation buffer. Figure 5 shows an integrated embodiment of an accumulator and a gas flow heat exchanger. Figure 6 shows an integrated embodiment of an accumulator, a gas flow heat exchanger, and a gas blower actuated by a hydraulic motor. Figure 7 shows a gas regeneration heat exchanger. Figure 8 shows an integrated embodiment of a non-adjustable hydraulic transducer and a liquid thermal insulation buffer -53-201132851. [Main component symbol description] 1 : Liquid gas accumulator 2 : Liquid gas accumulator 3 : Liquid reservoir 4 : Liquid reservoir 5 : Movable partition 6 : Movable partition 7 : Gas reservoir 8 : Gas Reservoir 9: heating and cooling mechanism 10: heat exchanger 1 1 : heat exchanger 1 2 : gas line 13 : valve 14 : liquid supply and suction mechanism 15 : internal groove type gas passage 16 : internal axial passage 1 7 : Collector part 18: Plug 1 9 : Port 20 : Flange 2 1 : Spiral external passage - 54 201132851 22 : Check valve 23 : Gas reservoir 24 : Accumulator 25 : Heat exchanger 26 : Stop Return valve 27: liquid reservoir 28: liquid reservoir 29: liquid regenerative heat exchanger 3 〇: thermal insulation buffer 3 1 : variable volume liquid reservoir 3 2 : variable volume liquid reservoir 3 3 : Moving thermal insulator, liquid-tight movable thermal insulation partition 3 4 : Strong outer casing 3 5 : liquid port 3 6 : liquid port 37 : metal sleeve 38 : piston 3 9 : space 40 : dip 41 : Cavity 42: hole 43: hole 44_·flow portion 45: regenerative element -55- 201132851 46: strong outer casing 47: internal heat exchange section 48: gas blower 49 : gas line 50 : gas line 5 1 : hydraulic motor 5 2 : shaft member 53 : gas regenerative heat exchanger 54 : strong outer casing 55 : heat insulating insert, heat insulating insert 56 : regenerative element 57 : spiral sheet 58 : spacer 5 9 : perforation 60 : hydraulic converter 61 : valve 6 2 : valve 6 3 : valve 64 : liquid line 6 5 : liquid line 6 6 : liquid line 67 : liquid line 6 8 : liquid port 69 : liquid口口-56- 201132851 70 : 71 : 72 : 73 : 74 : 75 : 76 : 77 : 78 : 79 : 80 : 81 : 8 2 : 8 3 ·· 8 4 : 85 : 86 : 87 : 88 : 89 : 90 : 91 : 92 : 93 : Liquid port liquid line gas port liquid port liquid port piston partition hydraulic converter port port port liquid reservoir liquid reservoir thermal insulation piston partition liquid reservoir thermal insulation Insert strong outer casing liquid port port port first line second line accumulator accumulator replenishment pump -57 201132851 94 : valve 95 : valve 96 : tank 97 : check valve 98 : hydraulic converter 99 : port 1 00 : port 1 01 : port 102 : port 103 · · valve 1 0 4 : output line 1 0 5 : Output line 106: load -58-