CN103212271B - Gas separating system and method for separating gas by using system thereof - Google Patents
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Abstract
本发明公开了一种气体分离系统以及使用该系统分离气体的方法，所述系统包括至少一个吸附塔和至少一个吸附-脱附塔，二者经管道相连通，吸附-脱附介质在吸附塔和吸附-脱附塔之间循环，其中所述吸附-脱附介质在达到吸附饱和前，吸附-脱附塔作为吸附塔对吸附气体进行吸附；而在所述吸附-脱附介质达到吸附饱和或接近饱和后，吸附-脱附塔作为脱附塔对吸附的气体进行脱附。本发明分离系统有效地延长了吸附-脱附介质的吸附时间，缩短了其脱附时间，从而大大地提高了吸附和脱附效率。
The invention discloses a gas separation system and a method for separating gas using the system. The system includes at least one adsorption tower and at least one adsorption-desorption tower. Circulation between the adsorption-desorption tower, wherein the adsorption-desorption tower acts as an adsorption tower to adsorb the adsorbed gas before the adsorption-desorption medium reaches adsorption saturation; and when the adsorption-desorption medium reaches adsorption saturation Or near saturation, the adsorption-desorption tower acts as a desorption tower to desorb the adsorbed gas. The separation system of the present invention effectively prolongs the adsorption time of the adsorption-desorption medium and shortens the desorption time, thus greatly improving the adsorption and desorption efficiency.
Description
技术领域technical field
本发明涉及一种气体分离系统以及使用该系统分离气体的方法，特别是，涉及一种吸附和脱附特定气体的分离系统以及使用该系统从废气或气体混合物中分离上述特定气体的方法。The present invention relates to a gas separation system and a gas separation method using the system, in particular, to a separation system for adsorbing and desorbing a specific gas and a method for separating the above specific gas from waste gas or a gas mixture using the system.
背景技术Background technique
随着在工业、生活领域中广泛使用石油、天然气、煤等燃料，这些燃料在燃烧过程中产生的废气排放问题作为全球规模的环境问题长期受到关注。上述废气中含有大量二氧化碳，而地球温室化的一个主要原因是由于大气中二氧化碳浓度增加。又如，许多工业上排放的废气中还可能包含除二氧化碳之外的成分、例如硫氧化物(SOX)，而硫氧化物有助于酸雨的形成。由于今后对上述燃料的需求仍然可观，因此怎样处理产生的废气或混合气中的二氧化碳或其他有毒气体将是一个严峻的问题。With the widespread use of fuels such as oil, natural gas, and coal in the industrial and living fields, the problem of exhaust emissions generated during the combustion of these fuels has long been concerned as a global environmental problem. The above exhaust gas contains a large amount of carbon dioxide, and one of the main causes of global warming is due to the increase in the concentration of carbon dioxide in the atmosphere. As another example, many industrial waste gases may contain components other than carbon dioxide, such as sulfur oxides (SO x ), which contribute to the formation of acid rain. Since the demand for the above-mentioned fuels will still be considerable in the future, it will be a serious problem how to deal with the carbon dioxide or other poisonous gases in the generated waste gas or mixed gas.
实际上，废气或混合气中的某些气体在一些工业过程中是需要供给的原材料，例如CO2、CO、CH4、NH4等都可以被分离提纯后用作产品材料回收利用。比如，在碳捕获及储存(CCS)和提高原油采收(EOR)领域中二氧化碳是必不可少的原材料，为了获得高浓度二氧化碳或降低购买二氧化碳的成本，能够从混合气中便利地分离和回收二氧化碳是解决上述问题的一个重要途径。In fact, some gases in waste gas or mixed gas are raw materials that need to be supplied in some industrial processes, such as CO 2 , CO, CH 4 , NH 4 , etc., can be separated and purified and used as product materials for recycling. For example, carbon dioxide is an essential raw material in the fields of carbon capture and storage (CCS) and enhanced oil recovery (EOR). In order to obtain high-concentration carbon dioxide or reduce the cost of purchasing carbon dioxide, it can be conveniently separated and recovered from the mixed gas Carbon dioxide is an important way to solve the above problems.
在过去的几十年中，关于从燃烧后的废气或混合气中分离和回收一些特定的气体一直是若干研究的课题，其中变温吸附(TSA)方法是利用吸附剂的平衡吸附量随温度升高而降低的特性，采用常温吸附、升温脱附的操作方法。因为在燃料燃烧后的废气或混合气中二氧化碳的量较多，很多研究是从怎样回收利用废气中的二氧化碳开始的，这些研究早期针对的是所谓的二氧化碳的“湿”分离和回收方法，即基于用能够选择性吸附二氧化碳的合适溶液或溶剂洗涤混合气，并通过加热吸附溶液或溶剂来回收所吸附的二氧化碳的方法。但是，此方法遇到的问题在于洗涤溶液易受到其组分氧化现象的影响，而且，废气或混合气中通常还包含硫和氮氧化物(SOX和NOX)，与洗涤溶液中的某些组分反应，会产生稳定的盐和难以清除和处理的其他有害化合物，因此需要经常替换洗涤溶液。In the past few decades, the separation and recovery of some specific gases from the exhaust gas or mixture after combustion has been the subject of several studies, among which the temperature swing adsorption (TSA) method is to use the equilibrium adsorption capacity of the adsorbent as the temperature increases. The characteristics of high and low, adopt the operation method of normal temperature adsorption and temperature rise desorption. Because the amount of carbon dioxide in the exhaust gas or mixed gas after fuel combustion is relatively large, many studies start from how to recycle the carbon dioxide in the exhaust gas. These studies are aimed at the so-called "wet" separation and recovery method of carbon dioxide in the early stage, that is, Based on scrubbing the gas mixture with a suitable solution or solvent capable of selectively adsorbing carbon dioxide and recovering the adsorbed carbon dioxide by heating the adsorption solution or solvent. However, the problem encountered in this method is that the scrubbing solution is susceptible to the oxidation of its components, and the exhaust gas or mixed gas usually also contains sulfur and nitrogen oxides (SO x and NO x ), which are different from some of the scrubbing solution. These components react to produce stable salts and other harmful compounds that are difficult to remove and handle, requiring frequent wash solution replacements.
近年来，国内外研究主要集中在用固体吸附剂分离和回收二氧化碳的系统和方法上，例如US6，387，337公开了一种从混合气中分离二氧化碳的工艺，其中吸附反应器中使用了经脱附二氧化碳而还原成可以反复使用的碱金属或碱土金属的吸附剂，在一个双床式反应器之间移动。此工艺包括：第一反应器为填装有还原的吸附剂的吸附塔，将含有二氧化碳的混合气通入第一反应器中，从而将二氧化碳吸附在所述吸附剂上；将吸附有二氧化碳的用过的吸附剂移至第二反应器以便还原，用于脱附吸附剂上的二氧化碳的气体可包括天然气、甲烷、一氧化碳、氢气和一氧化碳与氢气的合成气；而后，将还原的吸附剂移至第一反应器，使其继续进行吸附过程。此工艺的流程和操作简单、高效，但是外源性还原气体的引入将直接导致分离后的二氧化碳纯度降低，进而需要进行额外的气体分离操作。In recent years, research at home and abroad has mainly focused on systems and methods for separating and recovering carbon dioxide with solid adsorbents. For example, US6,387,337 discloses a process for separating carbon dioxide from mixed gas, in which the adsorption reactor uses Adsorbents that desorb carbon dioxide and reduce it to reusable alkali or alkaline earth metals move between a two-bed reactor. This process includes: the first reactor is an adsorption tower filled with reduced adsorbent, and the mixed gas containing carbon dioxide is passed into the first reactor, so that carbon dioxide is adsorbed on the adsorbent; The spent sorbent is moved to a second reactor for reduction, and the gases used to desorb carbon dioxide on the sorbent may include natural gas, methane, carbon monoxide, hydrogen, and synthesis gas of carbon monoxide and hydrogen; the reduced sorbent is then moved to to the first reactor to continue the adsorption process. The process and operation of this process are simple and efficient, but the introduction of exogenous reducing gas will directly lead to a decrease in the purity of the separated carbon dioxide, which in turn requires additional gas separation operations.
US6,755,892公开了一种从废气中分离二氧化碳的系统，该系统包括：填装含胺和腈官能团的吸附剂的二氧化碳吸附床；连通含二氧化碳的废气源和所述吸附床的管道；所述吸附床的出口管道；从所述吸附塔中释放出二氧化碳的再生装置；和至少一个可以控制所述吸附床的进出气的调节阀。此系统通过上述调节阀或加设的控制装置转换系统中的气流方向，从而进行吸附过程和脱附过程。而上述用于脱附二氧化碳的再生装置为加热器，系统中利用外设加热器加热所述吸附床，以便达到脱附二氧化碳的温度。另外，此发明中也提到可用通入蒸汽的方法达到脱附二氧化碳目的。此发明系统进行二氧化碳分离和回收所需的设备复杂、昂贵、难以操作，因而意味着需要高投资和高维护费用。此外，还存在外设性热源传热效率问题、分离后二氧化碳纯度、高压热蒸汽对吸附剂的磨损等问题。US6,755,892 discloses a system for separating carbon dioxide from waste gas, the system comprising: a carbon dioxide adsorption bed filled with an adsorbent containing amine and nitrile functional groups; a pipeline connecting the carbon dioxide-containing waste gas source and the adsorption bed; The outlet pipeline of the adsorption bed; the regeneration device for releasing carbon dioxide from the adsorption tower; and at least one regulating valve capable of controlling the inlet and outlet gas of the adsorption bed. In this system, the air flow direction in the system is changed through the above-mentioned regulating valve or the additional control device, so as to carry out the adsorption process and the desorption process. The above-mentioned regenerating device for desorbing carbon dioxide is a heater, and an external heater is used in the system to heat the adsorption bed so as to reach the temperature for desorbing carbon dioxide. In addition, it is also mentioned in this invention that the method of feeding steam can be used to achieve the purpose of desorbing carbon dioxide. The equipment required for the carbon dioxide separation and recovery of the inventive system is complex, expensive and difficult to operate, thus implying high investment and maintenance costs. In addition, there are also problems such as the heat transfer efficiency of external heat sources, the purity of carbon dioxide after separation, and the wear of adsorbents by high-pressure hot steam.
事实上，US6,755,892所公开的二氧化碳分离系统包括了至少两个二氧化碳吸附剂床，其中当一个吸附剂床在吸附时，另一个吸附剂床在脱附，但由于脱附速度通常要比吸附速度快得多，两个吸附剂床无法同时达到满负荷，因此，该分离系统的吸附效率和脱附效率并不高。In fact, the carbon dioxide separation system disclosed in US6,755,892 includes at least two carbon dioxide adsorbent beds, wherein when one adsorbent bed is adsorbing, the other adsorbent bed is desorbing, but because the desorption rate is usually faster than the adsorption The speed is much faster, and the two adsorbent beds cannot be fully loaded at the same time, so the adsorption and desorption efficiency of this separation system is not high.
US7,153,344公开了一种从燃烧的氧化物废气中分离和回收二氧化碳的方法。该方法包括：将废气通入半渗透材料中，通过气体半渗透材料从所述废气中分离包括高浓度二氧化碳的气流，其中将至少一部分包括高浓度二氧化碳的气流用作工业生产的原料入料和/或储存至少一部分包括高浓度二氧化碳的气流。US 7,153,344 discloses a method for the separation and recovery of carbon dioxide from combustion oxide off-gases. The method comprises passing waste gas through a semi-permeable material from which a gas stream comprising a high concentration of carbon dioxide is separated by means of the gas semi-permeable material, wherein at least a portion of the gas stream comprising a high concentration of carbon dioxide is used as a raw material feedstock for industrial production and and/or storing at least a portion of the gas stream comprising a high concentration of carbon dioxide.
实际上，在US7,153,344所公开的分离系统中，一部分作为产物气体的包括高浓度二氧化碳的气流经加热后作为解吸气体回流又重新进入系统中，用于加热所述半渗透材料，以使其吸附的二氧化碳脱附。In fact, in the separation system disclosed in US 7,153,344, a part of the product gas containing high-concentration carbon dioxide is heated and then re-enters the system as desorbed gas to heat the semi-permeable material so that it Adsorbed carbon dioxide is desorbed.
上述所有专利文献的公开内容在此全文引入以作参考。The disclosures of all of the above patent documents are hereby incorporated by reference in their entirety.
显然，对废气或混合气中的其它特定气体、例如CO、CH4、SOX、NOX、H2S或NH4等进行吸附-脱附处理的系统和方法与二氧化碳的吸附-脱附系统和方法的原理是相同的。毫无疑问，在变更合适的吸附剂的情况下，吸附和脱附二氧化碳的系统及其分离二氧化碳的方法同样适用于其它气体的分离或提纯。Obviously, the system and method for adsorption-desorption treatment of other specific gases in exhaust gas or mixed gas, such as CO, CH 4 , SO X , NO X , H 2 S or NH 4 , and the adsorption-desorption system of carbon dioxide The principle of the method is the same. Undoubtedly, the system for adsorbing and desorbing carbon dioxide and the method for separating carbon dioxide are also applicable to the separation or purification of other gases, provided that suitable adsorbents are changed.
尽管现有技术中公开了很多通过吸附-脱附机理分离气体的系统和方法，但普通存在由于低温吸附和高温脱附的速度不一致导致的吸附设备尺寸过大或分离效率低下的问题，如何解决这一问题以减小吸附设备尺寸或提高分离效率是气体分离与回收领域中亟待解决的问题。Although many systems and methods for separating gases through the adsorption-desorption mechanism have been disclosed in the prior art, there are generally problems of excessive size of adsorption equipment or low separation efficiency due to inconsistent speeds of low-temperature adsorption and high-temperature desorption. How to solve the problem? This problem is an urgent problem to be solved in the field of gas separation and recovery in order to reduce the size of the adsorption equipment or improve the separation efficiency.
为解决上述现有技术中所面临的问题，本发明提供一种从气体混合物中分离某些特定气体的系统和方法，系统操作简单、成本低、效率高，可在低温吸附条件下对这些特定气体进行连续性快速吸附，并且可在未引入外源性脱附气体的条件下提高脱附效果，从而可分离得到高纯度的特定气体。In order to solve the above-mentioned problems faced in the prior art, the present invention provides a system and method for separating certain specific gases from a gas mixture. The gas is continuously and rapidly adsorbed, and the desorption effect can be improved without introducing exogenous desorption gas, so that high-purity specific gases can be separated.
此外，本发明系统和方法通过巧妙的构思，在不改变吸附剂种类和分离系统结构的情况下，延长了吸附剂的吸附时间，缩短了气体脱附的时间，从而通过同时提高吸附效率和脱附效率而使得吸附设备尺寸减小和气体分离效率大大提高，进而克服了现有技术中的上述技术难题。In addition, the system and method of the present invention prolong the adsorption time of the adsorbent and shorten the time of gas desorption without changing the type of adsorbent and the structure of the separation system through ingenious conception, thereby improving the adsorption efficiency and desorption at the same time. The adsorption efficiency reduces the size of the adsorption equipment and greatly improves the gas separation efficiency, thereby overcoming the above-mentioned technical difficulties in the prior art.
发明内容Contents of the invention
根据本发明第一个方面，提供一种气体分离系统，其包括至少一个吸附塔和至少一个吸附-脱附塔，二者通过管道相连通，以使吸附-脱附介质在吸附塔和吸附-脱附塔之间循环；其区别于现有技术的特征是：所述吸附-脱附介质在达到吸附饱和前，吸附-脱附塔作为吸附塔对气体混合物中的气体进行吸附处，以便充分吸附气体提高吸附效率；而在所述吸附-脱附介质达到吸附饱和或吸附接近饱和后，吸附-脱附塔作为脱附塔对吸附的气体进行脱附，以便提高气体脱附效率。According to the first aspect of the present invention, a kind of gas separation system is provided, which comprises at least one adsorption tower and at least one adsorption-desorption tower, the two are connected through pipelines, so that the adsorption-desorption medium is in the adsorption tower and the adsorption-desorption tower Circulation between the desorption towers; its difference from the prior art is that: before the adsorption-desorption medium reaches adsorption saturation, the adsorption-desorption tower is used as an adsorption tower to adsorb the gas in the gas mixture, so that it can fully The adsorption gas improves the adsorption efficiency; and after the adsorption-desorption medium reaches adsorption saturation or the adsorption is close to saturation, the adsorption-desorption tower acts as a desorption tower to desorb the adsorbed gas, so as to improve the gas desorption efficiency.
任选地，可用直接加热或间接加热的方式对达到吸附饱和或吸附接近饱和的所述吸附-脱附介质进行加热，以使被吸附在所述吸附-脱附介质中的吸附气体脱附，直接加热指用热交换器、电加热、微波加热、和/或辐射加热等方式直接加热所述吸附-脱附介质；而间接加热指先加热解吸气体，而后将解吸气体作为热载体使之与所述吸附-脱附介质接触进行加热，其中热交换器优选地是热交换介质流经其中的盘管式热交换器，所述热交换介质例如是高压水蒸汽，氢气、二氧化碳和/或高温惰性气体等等。Optionally, the adsorption-desorption medium that has reached adsorption saturation or is close to saturation can be heated by direct heating or indirect heating, so that the adsorbed gas adsorbed in the adsorption-desorption medium is desorbed, Direct heating refers to direct heating of the adsorption-desorption medium by means of heat exchangers, electric heating, microwave heating, and/or radiation heating; while indirect heating refers to first heating the desorbed gas, and then using the desorbed gas as a heat carrier to combine with the The adsorption-desorption medium is contacted for heating, wherein the heat exchanger is preferably a coil heat exchanger through which a heat exchange medium flows, such as high-pressure steam, hydrogen, carbon dioxide and/or high-temperature inert gas and so on.
在所述吸附-脱附介质达到吸附饱和或吸附接近饱和后，吸附塔对混合物中的气体继续进行吸附，同时吸附-脱附塔作为托附塔对吸附到吸附-脱附介质中的气体进行脱附，优选地，可将在所述吸附-脱附塔中脱附的至少一部分产物气体作为解吸气体回流至吸附-脱附塔中。在对吸附气体进行上述吸附和脱附时，所述气体混合物与所述吸附-脱附介质的接触方式是任意的，例如顺流或逆流接触，同样达到吸附饱和或吸附接近饱和的所述吸附-脱附介质与解吸气体的接触方式也是任意的，例如顺流或逆流接触。After the adsorption-desorption medium reaches adsorption saturation or adsorption is close to saturation, the adsorption tower continues to adsorb the gas in the mixture, and the adsorption-desorption tower acts as a supporting tower to adsorb the gas in the adsorption-desorption medium. Desorption, preferably, at least a part of the product gas desorbed in the adsorption-desorption column can be refluxed into the adsorption-desorption column as desorption gas. When performing the above-mentioned adsorption and desorption on the adsorbed gas, the contact mode between the gas mixture and the adsorption-desorption medium is arbitrary, such as forward or countercurrent contact. - The manner of contacting the desorption medium with the desorption gas is also arbitrary, eg cocurrent or countercurrent.
上述系统包括至少一个吸附塔和至少一个吸附-脱附塔，在具备两个或两个以上吸附塔的情况下，所述吸附塔之间的连接方式可以是串联或并联；同样，在具备两个或两个以上吸附-脱附塔的情况下，所述吸附-脱附塔之间的连接方式也可以是串联或并联。The above-mentioned system includes at least one adsorption tower and at least one adsorption-desorption tower. In the case of having two or more adsorption towers, the connection mode between the adsorption towers can be in series or in parallel; In the case of one or more adsorption-desorption towers, the connection mode between the adsorption-desorption towers can also be series or parallel.
上述系统中吸附和脱附的气体可以依据实际需要进行选择，所述吸附-脱附气体可为CO2、CO、CH4、SOX、NOX、H2S或NH4中的一种或多种气体。The gas for adsorption and desorption in the above system can be selected according to actual needs, and the adsorption-desorption gas can be one of CO 2 , CO, CH 4 , SO X , NO X , H 2 S or NH 4 or Various gases.
所述吸附-脱附介质在达到吸附饱和或吸附接近饱和后，吸附塔对气体混合物中的吸附气体进行吸附，同时吸附-脱附塔作为脱附塔对吸附的气体进行脱附，在此过程中，除可将一部分产物气体回流作为解吸气体外，也可从系统外部通入吸附-脱附塔所需的用于脱附吸附-脱附介质所吸附的气体的解吸气体，以便于系统对吸附的气体进行脱附。从系统外部通入吸附-脱附塔中的解吸气体可是本领域普通技术人员熟知的任何类型的解析气体，优选地，从系统外部通入吸附-脱附塔中的解吸气体是与产物气体相同的气体。After the adsorption-desorption medium reaches adsorption saturation or adsorption is close to saturation, the adsorption tower adsorbs the adsorbed gas in the gas mixture, and at the same time the adsorption-desorption tower acts as a desorption tower to desorb the adsorbed gas. In addition to refluxing a part of the product gas as the desorption gas, the desorption gas required by the adsorption-desorption tower for desorption of the gas adsorbed by the adsorption-desorption medium can also be introduced from the outside of the system, so that the system The adsorbed gas is desorbed. The desorption gas that is passed into the adsorption-desorption tower from the outside of the system can be any type of analytical gas well known to those of ordinary skill in the art. Preferably, the desorption gas that is passed into the adsorption-desorption tower from the outside of the system is the same as the product gas gas.
上述系统使用的吸附-脱附介质可按照吸附-脱附气体的类型进行选择，所述吸附-脱附介质可是选自于以下物质的一种或多种吸附剂：硅胶、活性炭、纳米碳管、沸石、硅藻土、分子筛、离子交换树脂、含金属化合物的改性材料、含胺官能基的改性材料或含腈官能基的改性材料。显然，因其自身使用周期等原因，所述系统还可包括吸附-脱附介质入料口和废且不再使用的吸附-脱附介质出料口，以便定期更换无法再生的吸附-脱附介质。The adsorption-desorption medium used in the above system can be selected according to the type of adsorption-desorption gas, and the adsorption-desorption medium can be one or more adsorbents selected from the following substances: silica gel, activated carbon, carbon nanotubes , zeolite, diatomaceous earth, molecular sieve, ion exchange resin, modified material containing metal compound, modified material containing amine functional group or modified material containing nitrile functional group. Obviously, due to reasons such as its own service cycle, the system can also include an adsorption-desorption medium inlet and a waste and no longer used adsorption-desorption medium outlet, so that the adsorption-desorption medium that cannot be regenerated can be replaced regularly. medium.
事实上，所述吸附-脱附塔是通过管道和阀实现吸附塔和脱附塔之间转变的，即当吸附-脱附塔作为吸附塔使用时，通过管道向其中输入含吸附气体的气体混合物和/或新鲜的吸附-脱附介质，而在吸附-脱附塔作为脱附塔使用时，通过阀关闭上述输入通道，同时也通过管道将吸附-脱附塔中的气体混合物移至吸附塔中并在其中继续进行气体吸附或将之移出系统之外，又将吸附塔中的达到吸附饱和或吸附接近饱和的吸附-脱附介质通过管道移至吸附-脱附塔中，并在其中实现气体脱附和再生，上述过程可彼此交叉重复进行。In fact, the adsorption-desorption tower realizes the transition between the adsorption tower and the desorption tower through pipelines and valves, that is, when the adsorption-desorption tower is used as an adsorption tower, the gas containing the adsorbed gas is input into it through the pipeline mixture and/or fresh adsorption-desorption medium, and when the adsorption-desorption tower is used as a desorption tower, the above-mentioned input passage is closed by a valve, and the gas mixture in the adsorption-desorption tower is also moved to the adsorption through a pipeline The gas adsorption is continued in the tower or removed from the system, and the adsorption-desorption medium in the adsorption tower that has reached adsorption saturation or adsorption is close to saturation is moved to the adsorption-desorption tower through the pipeline, and in it To achieve gas desorption and regeneration, the above-mentioned processes can be repeated alternately.
根据本发明第二个方面，提供一种用上述系统分离气体的方法，该方法按顺序包括以下步骤：According to a second aspect of the present invention, there is provided a method for separating gases with the above-mentioned system, the method comprising the following steps in sequence:
1)将含所述吸附气体的气体混合物通入所述吸附塔和吸附-脱附塔中，从而将所述吸附气体吸附到在吸附塔和吸附-脱附塔之间循环的吸附-脱附介质中；1) Pass the gas mixture containing the adsorption gas into the adsorption tower and the adsorption-desorption tower, thereby adsorbing the adsorption gas to the adsorption-desorption cycle between the adsorption tower and the adsorption-desorption tower medium;
2)在所述吸附-脱附介质达到吸附饱和或吸附接近饱和后，将吸附-脱附塔中的气体混合物和/或新鲜吸附-脱附介质移入吸附塔中对气体混合物中的所述吸附气体继续进行吸附，同时将吸附饱和或吸附接近饱和的吸附-脱附介质从吸附塔中移至吸附-脱附塔中，并将吸附-脱附塔中的吸附-脱附介质加热至吸附气体解吸温度以上，从而对吸附在吸附-脱附介质中的所述吸附气体进行脱附2) After the adsorption-desorption medium reaches adsorption saturation or adsorption is close to saturation, the gas mixture in the adsorption-desorption tower and/or the fresh adsorption-desorption medium are moved into the adsorption tower for the adsorption of the gas mixture. The gas continues to be adsorbed, and at the same time, the adsorption-desorption medium that is saturated or nearly saturated is moved from the adsorption tower to the adsorption-desorption tower, and the adsorption-desorption medium in the adsorption-desorption tower is heated to the adsorption gas Above the desorption temperature, thereby desorbing the adsorbed gas adsorbed in the adsorption-desorption medium
3)将脱附后的气体作为产物气体移出系统外；3) Remove the desorbed gas out of the system as product gas;
4)将经吸附分离出吸附气体的气体混合物移出系统外。4) Remove the gas mixture from which the adsorbed gas has been separated by adsorption out of the system.
优选地，对吸附-脱附介质加热是通过向吸附-脱附塔中通入解吸气体来实现的，并且至少一部分产物气体可作为解吸气体回流至所述吸附-脱附塔中，其中回流的产物气体在回流至所述吸附-脱附塔中前需被加热到解吸温度以上。Preferably, the heating of the adsorption-desorption medium is achieved by passing desorption gas into the adsorption-desorption tower, and at least a part of the product gas can be refluxed into the adsorption-desorption tower as desorption gas, wherein the refluxed The product gas needs to be heated above the desorption temperature before being refluxed into the adsorption-desorption column.
一般而言，可按照吸附-脱附介质对特定气体的吸附-脱附特性来选择解吸气体，如上所述，解吸气体可来自系统外，也可来自一部分回流的产物气体，作为解吸气体回流至所述吸附-脱附塔中的产物气体通常占在所述吸附-脱附塔中脱附产生的气体总量的10～60(体积)％。Generally speaking, the desorption gas can be selected according to the adsorption-desorption characteristics of the adsorption-desorption medium for a specific gas. As mentioned above, the desorption gas can come from outside the system, or from a part of the refluxed product gas, which is refluxed as desorption gas to The product gas in the adsorption-desorption tower usually accounts for 10-60 (volume)% of the total amount of gas desorbed in the adsorption-desorption tower.
在上述方法中，可使脱附得到的产物气体进一步通过至少一个旋风机、气体过滤器、干燥器和/或气体压缩机，从而形成纯度更高的产物气体，所述新鲜吸附-脱附介质也可是来自吸附-脱附塔中经气体解吸而再生的吸附-脱附介质，上述方法的各步骤可按顺序循环，以便实现气体的连续分离。In the above method, the product gas obtained by desorption can be further passed through at least one cyclone, gas filter, dryer and/or gas compressor, thereby forming a product gas with higher purity, and the fresh adsorption-desorption medium It can also be the adsorption-desorption medium regenerated by gas desorption in the adsorption-desorption tower, and the steps of the above method can be cycled in sequence, so as to realize the continuous separation of gases.
附图说明Description of drawings
图1为本发明气体分离系统一个实施方案的结构示意图。Fig. 1 is a schematic structural view of an embodiment of the gas separation system of the present invention.
图2为本发明气体分离系统另一个实施方案的结构示意图。Fig. 2 is a schematic structural view of another embodiment of the gas separation system of the present invention.
具体实施方式Detailed ways
通过以下参考附图的描述进一步详细解释本发明，但以下描述仅用于使本发明所属技术领域的普通技术人员能够更加清楚地理解本发明的原理和精髓，并不意味着对本发明进行任何形式的限制。附图中等同的或相对应的部件或特征用相同的标记数表示。The present invention is further explained in detail through the following description with reference to the accompanying drawings, but the following description is only used to enable those of ordinary skill in the art to which the present invention belongs to understand the principle and essence of the present invention more clearly, and does not mean that the present invention is modified in any form. limits. Identical or corresponding parts or features are denoted by the same reference numerals in the figures.
图1是本发明气体分离系统一个实施方案，其为吸附和脱附系统10a，在此实施方式中将特定气体设定为二氧化碳。系统10a在相对低温、例如低于60℃温度下从气体混合物中吸附二氧化碳，在相对高温、例如高于100℃温度下从吸附剂中脱附吸附的二氧化碳，从而达到从气体混合物中分离并回收二氧化碳的目的。图1的系统主要包括一个第一流化床(即吸附塔)20、一个第二流化床(即吸附-脱附塔)30、分离器40与第二分离器50、第一流化床20的气体混合物输送管道11、第二流化床30的混合气输送管道35、第一流化床20的输出管道23、第二流化床30的脱附气体管道33、脱附气体管道33的支路管道60和输送解吸气体的辅助管道65，其中，第一流化床20和第二流化床30中填装有能吸附二氧化碳而后又能通过脱附作用释放出二氧化碳的吸附剂，第一流化床20通过其顶部设置的分离器40与第二流化床30的下端连通，第二流化床30通过其顶部设置的第二分离器50与第一流化床20的下端连通，从而使所述吸附剂在第一流化床20和第二流化床30之间循环。在吸附剂达到吸附饱和前，第一流化床和第二流化床均对二氧化碳进行吸附处理，使其能够充分吸附二氧化碳；而在所述吸附剂达到吸附饱和或吸附接近饱和后，将第一流化床(吸附塔)中的吸附剂通过分离器40和管道34移至第二流化床(吸附-脱附塔)中，同时通过泵(未示出)将第二流化床(吸附-脱附塔)中的气体混合物移至第一流化床(吸附塔)中，并向其中加入新鲜吸附剂，以便第一流化床继续对二氧化碳进行吸附处理，同时第二流化床对吸附到吸附剂中的二氧化碳进行脱附处理，从而同时提高二氧化碳的吸附和脱附效率。图1所示系统的主要组件标记数说明参见下面表1。Fig. 1 is an embodiment of the gas separation system of the present invention, which is an adsorption and desorption system 10a, in which the specific gas is set to be carbon dioxide. The system 10a adsorbs carbon dioxide from the gas mixture at a relatively low temperature, such as below 60°C, and desorbs the adsorbed carbon dioxide from the adsorbent at a relatively high temperature, such as above 100°C, so as to achieve separation and recovery from the gas mixture purpose of carbon dioxide. The system of Fig. 1 mainly comprises a first fluidized bed (being adsorption tower) 20, a second fluidized bed (being adsorption-desorption tower) 30, separator 40 and second separator 50, first fluidized bed The gas mixture delivery pipeline 11 of 20, the mixed gas delivery pipeline 35 of the second fluidized bed 30, the output pipeline 23 of the first fluidized bed 20, the desorption gas pipeline 33 of the second fluidized bed 30, the desorption gas pipeline 33 A branch pipeline 60 and an auxiliary pipeline 65 for transporting desorption gas, wherein the first fluidized bed 20 and the second fluidized bed 30 are filled with an adsorbent capable of absorbing carbon dioxide and then releasing carbon dioxide through desorption, The first fluidized bed 20 communicates with the lower end of the second fluidized bed 30 through the separator 40 provided at its top, and the second fluidized bed 30 communicates with the lower end of the first fluidized bed 20 through the second separator 50 provided at its top. communicated so that the adsorbent circulates between the first fluidized bed 20 and the second fluidized bed 30 . Before the adsorbent reaches adsorption saturation, both the first fluidized bed and the second fluidized bed perform adsorption treatment on carbon dioxide, so that they can fully absorb carbon dioxide; The adsorbent in the first fluidized bed (adsorption tower) is moved to the second fluidized bed (adsorption-desorption tower) through separator 40 and pipeline 34, and the second fluidized bed (adsorption-desorption tower) is moved by pump (not shown) simultaneously The gas mixture in the adsorption-desorption tower) is moved to the first fluidized bed (adsorption tower), and fresh adsorbent is added to it, so that the first fluidized bed continues to adsorb carbon dioxide, while the second fluidized bed The carbon dioxide adsorbed in the adsorbent is desorbed to improve the adsorption and desorption efficiency of carbon dioxide at the same time. See Table 1 below for a description of the number of major components of the system shown in Figure 1 .
表1Table 1
在系统启动之初或在所述吸附剂达到饱和前，开启第二流化床30的气体混合物输送管道开关63，并关闭辅助解吸气体输送管道开关67和脱附气体回流的支路管道开关64，将第一流化床的气体混合物输送管道11中和第二流化床的气体混合物输送管道35中的气体混合物同时通入第一流化床20和第二流化床30中，以便于其中的所述吸附剂充分吸附气体混合物中的二氧化碳。At the beginning of system startup or before the adsorbent reaches saturation, open the gas mixture delivery pipeline switch 63 of the second fluidized bed 30, and close the auxiliary desorption gas delivery pipeline switch 67 and the desorption gas backflow branch pipeline switch 64 , the gas mixture in the gas mixture delivery pipeline 11 of the first fluidized bed and the gas mixture in the gas mixture delivery pipeline 35 of the second fluidized bed is passed in the first fluidized bed 20 and the second fluidized bed 30 simultaneously, so that The adsorbent therein fully adsorbs carbon dioxide in the gas mixture.
含二氧化碳的气体混合物沿第一流化床20的气体混合物输送管道11通过其气体混合物进口21进入第一流化床20中，在第一流化床20中含二氧化碳的气体混合物与新鲜和/或未吸附饱和的吸附剂相接触，将气体混合物中的二氧化碳逐渐吸附到所述吸附剂中，而除去至少部分、或大部分二氧化碳的气体混合物从第一流化床20的气体出口沿着其输出管道23移出系统外。同时，含二氧化碳的气体混合物同样沿第二流化床30的气体混合物输送管道35通过其气体混合物进口31进入第二流化床30中，在第二流化床30中含二氧化碳的气体混合物同样与新鲜和/或未饱和的吸附剂相接触，将气体混合物中的二氧化碳吸附到所述吸附剂中，而除去至少部分、或大部分二氧化碳的气体混合物从第二流化床30的气体出口沿着其输出管道(未示出)移出系统外。除去至少部分、或大部分二氧化碳的气体混合物可根据操作要求直接排入大气中，或作进一步处理，在本文中对此不再赘述。The gas mixture containing carbon dioxide enters the first fluidized bed 20 along the gas mixture delivery pipeline 11 of the first fluidized bed 20 through its gas mixture inlet 21, and in the first fluidized bed 20 the gas mixture containing carbon dioxide is mixed with fresh and/or or unsaturated adsorbent, the carbon dioxide in the gas mixture is gradually adsorbed in the adsorbent, and the gas mixture from the gas outlet of the first fluidized bed 20 along its The output pipe 23 moves out of the system. Simultaneously, the gas mixture containing carbon dioxide enters in the second fluidized bed 30 through its gas mixture inlet 31 along the gas mixture conveying pipeline 35 of the second fluidized bed 30, and the gas mixture containing carbon dioxide in the second fluidized bed 30 is also Contact with fresh and/or unsaturated adsorbent to adsorb carbon dioxide in the gas mixture to the adsorbent, and the gas mixture from the gas outlet of the second fluidized bed 30 with at least some, or most of the carbon dioxide removed It moves out of the system with its output pipe (not shown). The gas mixture from which at least part, or most, of the carbon dioxide has been removed can be directly discharged into the atmosphere or further processed according to operational requirements, which will not be described in detail herein.
所述第一流化床20的顶部设置有分离器40，而分离器40可为气-固分离器、例如旋风机，以将所夹带的吸附剂粉末和/或吸附剂与已除去至少部分、或大部分二氧化碳的气体混合物相分离，分离掉二氧化碳的气体混合物从分离器40的顶部沿着其输出管道23移出系统外，而吸附剂粉末与固体吸附剂则从分离器40的底部沿着第一流化床20的连通管道24移至第二流化床30中。在第二流化床30顶部设置有第二分离器50，第二分离器50也可是气-固分离器，可选择与分离器40相同的分离器、例如旋风机，或者可选择与分离器40不同的其他分离器，以将吸附剂粉末和/或吸附剂与已除去至少部分、或大部分二氧化碳的气体混合物相分离，分离掉二氧化碳的气体混合物从第二分离器50的顶部沿着其输出管道(未示出)移出系统外，而吸附剂粉末与固体吸附剂则从分离器50的底部沿着第二流化床30的连通管道34移至第一流化床20中，从而完成吸附二氧化碳期间吸附剂在第一流化床20和第二流化床30之间的循环。The top of the first fluidized bed 20 is provided with a separator 40, and the separator 40 can be a gas-solid separator, such as a cyclone, to separate the entrained adsorbent powder and/or adsorbent from at least part of the , or most of the gas mixture of carbon dioxide is separated, and the gas mixture separated from the carbon dioxide is moved out of the system from the top of the separator 40 along its output pipeline 23, while the adsorbent powder and the solid adsorbent are from the bottom of the separator 40 along the The communication pipe 24 of the first fluidized bed 20 is moved into the second fluidized bed 30 . A second separator 50 is arranged on the top of the second fluidized bed 30, and the second separator 50 can also be a gas-solid separator, and the same separator as the separator 40, such as a cyclone, can be selected, or it can be selected from the same separator as the separator. 40 different other separators to separate the adsorbent powder and/or adsorbent from the gas mixture from which at least part, or most, of the carbon dioxide has been removed, the gas mixture from which the carbon dioxide has been separated passes from the top of the second separator 50 along its The output pipeline (not shown) moves out of the system, while the adsorbent powder and solid adsorbent move from the bottom of the separator 50 to the first fluidized bed 20 along the communication pipeline 34 of the second fluidized bed 30, thereby completing Circulation of the adsorbent between the first fluidized bed 20 and the second fluidized bed 30 during the adsorption of carbon dioxide.
在第一流化床20和第二流化床30中填装的吸附剂是经气体脱附后可再生的吸附剂，所述吸附剂可是本领域普通技术人员熟知的可再生吸附剂，可选自于活性炭、纳米碳管、沸石、硅藻土、分子筛、离子交换树脂、含金属化合物的改性材料、含胺官能基的改性材料、含腈官能基的改性材料，以及它们的混合物。需要处理的气体混合物在第一流化床20和第二流化床30中的停留时间和操作温度，取决于吸附剂的吸附和脱附性质。The adsorbent packed in the first fluidized bed 20 and the second fluidized bed 30 is a regenerable adsorbent after gas desorption, and the adsorbent can be a regenerable adsorbent well known to those of ordinary skill in the art, and can be Selected from activated carbon, carbon nanotubes, zeolites, diatomaceous earth, molecular sieves, ion exchange resins, modified materials containing metal compounds, modified materials containing amine functional groups, modified materials containing nitrile functional groups, and their mixture. The residence time and operating temperature of the gas mixture to be treated in the first fluidized bed 20 and the second fluidized bed 30 depend on the adsorption and desorption properties of the adsorbent.
在所述吸附剂达到吸附饱和或吸附接近饱和后，所述系统10a可在几种不同状态下运行，如在第一种运行状态下，关闭辅助解吸气体输送管道开关67并开启第二流化床的气体混合物输送管道开关63和脱附气体回流的支路管道开关64，以使支路管道60中的脱附气体和第二流化床的气体混合物输送管道35中的气体混合物经过加热后通入所述第二流化床30中脱附被吸附剂吸附的二氧化碳。在第二种运行状态下，关闭第二流化床的气体混合物输送管道开关63并开启辅助解吸气体输送管道开关67和脱附气体回流的支路管道开关64，以使脱附气体回流的支路管道60中的二氧化碳和辅助解吸气体输送管道65中的二氧化碳经过加热后通入所述第二流化床30中脱附被吸附剂吸附的二氧化碳。在第三种运行状态下，关闭辅助解吸气体输送管道开关67和第二流化床的气体混合物输送管道开关63并开启脱附气体回流的支路管道开关64，以使脱附气体回流的支路管道60中的二氧化碳经过加热后通入所述第二流化床30中脱附被吸附剂吸附的二氧化碳。After the adsorbent reaches adsorption saturation or adsorption is close to saturation, the system 10a can operate in several different states, such as in the first operating state, close the auxiliary desorption gas delivery pipeline switch 67 and open the second fluidization The gas mixture delivery pipeline switch 63 of the bed and the branch pipeline switch 64 of desorption gas reflux, so that the desorption gas in the branch pipeline 60 and the gas mixture in the gas mixture delivery pipeline 35 of the second fluidized bed are heated The carbon dioxide adsorbed by the adsorbent is desorbed through the second fluidized bed 30 . In the second operating state, close the gas mixture delivery pipeline switch 63 of the second fluidized bed and open the auxiliary desorption gas delivery pipeline switch 67 and the branch pipeline switch 64 of the desorption gas reflux, so that the branch pipeline switch 64 of the desorption gas reflux The carbon dioxide in the pipeline 60 and the carbon dioxide in the auxiliary desorption gas delivery pipeline 65 are heated and passed into the second fluidized bed 30 to desorb the carbon dioxide adsorbed by the adsorbent. In the third operating state, close the auxiliary desorption gas delivery pipeline switch 67 and the gas mixture delivery pipeline switch 63 of the second fluidized bed and open the branch pipeline switch 64 of the desorption gas backflow, so that the branch pipeline switch 64 of the desorption gas backflow The carbon dioxide in the pipeline 60 is heated and passed into the second fluidized bed 30 to desorb the carbon dioxide adsorbed by the adsorbent.
所述系统10a中，当在第二流化床30中脱附得到的二氧化碳产物总量经加热后不足以脱附吸附剂在第一流化床20和/或第二流化床30中吸附的二氧化碳时，可选择所述系统在第一种状态或第二种状态下运行。当在第二流化床30中脱附得到的二氧化碳总量经加热后足以脱附吸附剂在第一流化床20和/或第二流化床30中吸附的二氧化碳时，可选择所述系统在第三种状态下运行。In the system 10a, when the total amount of carbon dioxide product desorbed in the second fluidized bed 30 is heated, it is not enough for the desorption adsorbent to be adsorbed in the first fluidized bed 20 and/or the second fluidized bed 30 The system can be selected to operate in the first state or the second state when the carbon dioxide is present. When the total amount of carbon dioxide desorbed in the second fluidized bed 30 is heated enough to desorb the carbon dioxide adsorbed by the adsorbent in the first fluidized bed 20 and/or the second fluidized bed 30, the described The system operates in the third state.
如上所述，在第一种运行状态下，将辅助解吸气体输送管道开关67关闭，而将第二流化床的气体混合物输送管道开关63和脱附气体回流的支路管道开关64开启。As mentioned above, in the first operating state, the auxiliary desorption gas delivery pipeline switch 67 is closed, and the gas mixture delivery pipeline switch 63 of the second fluidized bed and the desorption gas backflow branch pipeline switch 64 are turned on.
含有二氧化碳的气体混合物沿着第一流化床20的气体混合物输送管道11通过其气体进口21进入第一流化床20中，在第一流化床20中含二氧化碳的气体混合物与吸附剂相接触，将气体混合物中的二氧化碳吸附到所述吸附剂上，除去至少部分、或大部分二氧化碳的气体混合物从第一流化床20的上部其气体出口沿着其输出管道23移出系统外。The gas mixture containing carbon dioxide enters the first fluidized bed 20 along the gas mixture delivery pipe 11 of the first fluidized bed 20 through its gas inlet 21, and the gas mixture containing carbon dioxide is mixed with the adsorbent in the first fluidized bed 20 Contacting, absorbing the carbon dioxide in the gas mixture onto the adsorbent, and removing at least part or most of the carbon dioxide from the gas mixture from the upper part of the first fluidized bed 20 and its gas outlet along its output pipe 23 to move out of the system.
如上所述，第一流化床20的顶部设置有气-固分离器40，从而将吸附剂粉末和/或固体吸附剂与已除去至少部分、或大部分二氧化碳的气体混合物相分离，气体混合物随后从分离器40的顶部沿着其输出管道23移出系统外，而吸附二氧化碳的吸附剂或吸附二氧化碳已达饱和或接近饱和的吸附剂从第一流化床20中通过气-固分离器40和连通管道24移至第二流化床30的下端，在第二流化床30中来自第一流化床20的吸附剂和吸附二氧化碳也已达饱和或接近饱和的第二流化床30中的吸附剂被加热至脱附温度以上，例如与从第二流化床30的气体进口31通入的热解吸气体相接触，使其达到二氧化碳解吸温度后放出二氧化碳，被脱附出来的二氧化碳随后通过第二流化床30的脱附气体管道33移出系统之外。As mentioned above, the top of the first fluidized bed 20 is provided with a gas-solid separator 40 to separate the adsorbent powder and/or solid adsorbent from the gas mixture from which at least part, or most of the carbon dioxide has been removed, the gas mixture Then move out of the system from the top of the separator 40 along its output pipeline 23, and the adsorbent for adsorbing carbon dioxide or the adsorbent for adsorbing carbon dioxide that has reached saturation or near saturation passes through the gas-solid separator 40 from the first fluidized bed 20 And the communication pipe 24 is moved to the lower end of the second fluidized bed 30, and in the second fluidized bed 30, the adsorbent and the adsorbed carbon dioxide from the first fluidized bed 20 have also reached the second fluidized bed 30 saturated or nearly saturated The adsorbent in the fluidized bed is heated above the desorption temperature, for example, it is in contact with the thermal desorption gas introduced from the gas inlet 31 of the second fluidized bed 30, and after reaching the carbon dioxide desorption temperature, carbon dioxide is released and desorbed. The carbon dioxide is then removed from the system through the desorption gas pipeline 33 of the second fluidized bed 30 .
这里需要注意的是：由气体进口31通入的热气体即解吸气体包括：沿着第二流化床的气体混合物输送管道35通入第二流化床30中的气体混合物，以及沿着脱附气体回流的支路管道60通入第二流化床30中的产物气体，以及沿着辅助解吸气体输送管道65通入第二流化床30中的来自系统外的解吸气体。因此，通过第二流化床30脱附气体管道33的气体不仅包括了上述吸附剂脱附的二氧化碳，而且还包括用于脱附二氧化碳的解吸气体。若由第二流化床30的脱附气体管道移出系统外的二氧化碳的纯度或浓度未达到要求，可将脱附气体管道33中的一部分产物气体放出系统外不做回收处理，而脱附气体管道33中的另一部分产物气体则沿着脱附气体回流的支路管道60通入第二流化床30中作为解吸气体使用。同时，沿第二流化床30的气体混合物输送管道35以及沿脱附气体回流的支路管道60通入第二流化床30中的气体流量由气体混合物输送管道35的调节阀37和脱附气体回流的支路管道60的调节阀61控制，而沿第二流化床30的气体混合输送管道35以及沿脱附气体回流的支路管道60通入第二流化床30的气体的温度则由气体混合物输送管道35的加热装置36和脱附气体回流的支路管道60的加热装置62控制。It should be noted here that the hot gas introduced by the gas inlet 31, that is, the desorption gas, includes: the gas mixture passed into the second fluidized bed 30 along the gas mixture delivery pipeline 35 of the second fluidized bed, and the gas mixture along the desorption The branch pipeline 60 for gas return leads to the product gas in the second fluidized bed 30 , and the desorption gas from outside the system passes into the second fluidized bed 30 along the auxiliary desorption gas delivery pipeline 65 . Therefore, the gas passing through the desorption gas pipeline 33 of the second fluidized bed 30 includes not only the carbon dioxide desorbed by the above-mentioned adsorbent, but also the desorption gas used for desorbing carbon dioxide. If the purity or concentration of the carbon dioxide removed from the system by the desorption gas pipeline of the second fluidized bed 30 does not meet the requirements, a part of the product gas in the desorption gas pipeline 33 can be released outside the system without recovery treatment, and the desorption gas Another part of the product gas in the pipeline 33 is passed into the second fluidized bed 30 along the branch pipeline 60 where the desorption gas returns and used as the desorption gas. Simultaneously, the gas flow that passes into the second fluidized bed 30 along the gas mixture delivery pipeline 35 of the second fluidized bed 30 and the branch pipeline 60 of desorption gas reflux is controlled by the regulating valve 37 and the desorption gas mixture delivery pipeline 35. The regulating valve 61 of the branch pipeline 60 with gas reflux is controlled, and the gas mixing and conveying pipeline 35 along the second fluidized bed 30 and the gas passing into the second fluidized bed 30 along the desorption gas reflux branch pipeline 60 The temperature is controlled by the heating device 36 of the gas mixture delivery pipeline 35 and the heating device 62 of the branch pipeline 60 for desorbed gas return.
在第二流化床30中，吸附二氧化碳达到饱和或接近饱和的吸附剂与上述热解吸气体相接触使吸附剂的温度升高达到解吸温度以上，从而脱附出二氧化碳，结果得到新鲜或再生的吸附剂。所述第二流化床30的顶部设置有第二气-固分离器50，从而将新鲜或再生的吸附剂与产物气体相分离，产物气体从分离器50的顶部沿着脱附气体管道33移出系统外，而新鲜或再生的吸附剂则从分离器50的底部沿着第二流化床30的连通管道34移至第一流化床20中，从而完成吸附剂在第一流化床20和第二流化床30之间的脱附循环。In the second fluidized bed 30, the adsorbent that has adsorbed carbon dioxide to be saturated or nearly saturated is in contact with the above-mentioned thermal desorption gas, so that the temperature of the adsorbent rises above the desorption temperature, thereby desorbing carbon dioxide, resulting in fresh or regenerated sorbent. The top of the second fluidized bed 30 is provided with a second gas-solid separator 50, thereby separating the fresh or regenerated adsorbent from the product gas, and the product gas is removed from the top of the separator 50 along the desorption gas pipeline 33 outside the system, while the fresh or regenerated adsorbent moves from the bottom of the separator 50 to the first fluidized bed 20 along the communication pipe 34 of the second fluidized bed 30, thereby completing the adsorption of the adsorbent in the first fluidized bed 20 and the desorption cycle between the second fluidized bed 30.
一般而言，一部分反复使用过的吸附剂需要定期被更换。因此，在系统10a中，第一流化床20下端设有吸附剂进口22,在第二流化床30的第二分离器50下端设有废吸附剂出口32，以便在需要补充新鲜吸附剂时通过吸附剂进口22添加适量的吸附剂，同时也可通过废吸附剂出口32移除适量的废吸附剂。In general, some adsorbents that are used repeatedly need to be replaced periodically. Therefore, in the system 10a, the lower end of the first fluidized bed 20 is provided with an adsorbent inlet 22, and the lower end of the second separator 50 of the second fluidized bed 30 is provided with a waste adsorbent outlet 32, so as to supplement fresh adsorbent when needed At the same time, an appropriate amount of adsorbent can be added through the adsorbent inlet 22, and an appropriate amount of spent adsorbent can also be removed through the spent adsorbent outlet 32.
需要注意的是：在未启动第二流化床30的加热装置36的情况下，第一流化床20中的吸附剂和第二流化床30中的吸附剂同时在吸附二氧化碳；而在启动第二流化床30的加热装置36后，第一流化床20中的吸附剂继续在吸附二氧化碳，而第二流化床30中的吸附剂在热解吸气体的热作用下在脱附二氧化碳。It should be noted that: without starting the heating device 36 of the second fluidized bed 30, the adsorbent in the first fluidized bed 20 and the adsorbent in the second fluidized bed 30 are simultaneously adsorbing carbon dioxide; After starting the heating device 36 of the second fluidized bed 30, the adsorbent in the first fluidized bed 20 continues to adsorb carbon dioxide, while the adsorbent in the second fluidized bed 30 is desorbed under the thermal action of the thermal desorption gas. Desorption of carbon dioxide.
在第二种运行状态下，当第二流化床30进行解吸时，将第二流化床30的气体混合物输送管道35的开关63关闭，而将辅助解吸气体输送管道65的开关67和脱附气体回流的支路管道60的开关64开启。In the second operating state, when the second fluidized bed 30 is desorbing, the switch 63 of the gas mixture delivery pipeline 35 of the second fluidized bed 30 is closed, and the switch 67 and the desorption gas delivery pipeline 65 of the auxiliary desorption gas are turned off. The switch 64 of the branch pipeline 60 with gas return is opened.
含二氧化碳的气体混合物沿第一流化床的气体混合物输送管道11通过其气体进口21进入第一流化床20中，在第一流化床20中含二氧化碳的气体混合物与吸附剂相接触，将气体混合雾中的二氧化碳逐渐吸附到所述吸附剂中。除去至少部分、或大部分二氧化碳的气体混合物从第一流化床20的气体混合物出口沿着分离器40顶部的输出管道23被移出系统外，而吸附二氧化碳的吸附剂或吸附二氧化碳达到饱和或接近饱和的吸附剂从第一流化床20中通过分离器40和连通管道24移至第二流化床30的下端，在第二流化床30中来自第一流化床20的吸附剂和吸附二氧化碳也已达到饱和或接近饱和的在第二流化床30中的吸附剂被加热至解吸温度以上，例如与从第二流化床30的气体进口31通入的热解吸气体相接触，使其达到二氧化碳解吸温度后放出二氧化碳，被脱附出来的二氧化碳通过第二流化床30的脱附气体管道33被移出系统。The gas mixture containing carbon dioxide enters the first fluidized bed 20 along the gas mixture delivery pipeline 11 of the first fluidized bed through its gas inlet 21, and the gas mixture containing carbon dioxide contacts the adsorbent in the first fluidized bed 20, The carbon dioxide in the gas mixture mist is gradually adsorbed into the adsorbent. The gas mixture from which at least part or most of the carbon dioxide has been removed is removed from the gas mixture outlet of the first fluidized bed 20 along the outlet pipe 23 at the top of the separator 40, and the adsorbent or adsorbed carbon dioxide reaches saturation or is close to The saturated adsorbent moves from the first fluidized bed 20 to the lower end of the second fluidized bed 30 through the separator 40 and the communication pipe 24, and in the second fluidized bed 30, the adsorbent from the first fluidized bed 20 and The adsorbent in the second fluidized bed 30 which is also saturated or nearly saturated with adsorbed carbon dioxide is heated above the desorption temperature, e.g. Contact, release carbon dioxide after reaching the carbon dioxide desorption temperature, and the desorbed carbon dioxide is removed from the system through the desorption gas pipeline 33 of the second fluidized bed 30 .
在此运行状态下，由气体进口31通入的热解吸气体包括：沿着脱附气体回流的支路管道60通入第二流化床30中的产物二氧化碳，以及沿着辅助解吸气体输送管道65通入第二流化床30中的系统外的二氧化碳。选择此运行状态的原因是：由第二流化床30的脱附气体回流支路管道60回流的产物二氧化碳总量未能达到足以脱附吸附剂在第一流化床20和/或第二流化床30中吸附的所有二氧化碳，在此运行状态下，脱附二氧化碳的解吸气体是加热后的二氧化碳，未加入二氧化碳以外的其它气体，所以从第二流化床的脱附气体管道33移出系统的二氧化碳纯度较高。同时，沿辅助解吸气体输送管道65以及沿脱附气体回流支路管道60通入第二流化床30中的解吸气体流量是由辅助解吸气体输送管道65的调节阀(未标出)和脱附气体回流支路管道60的调节阀61控制，而沿辅助解吸气体输送管道65以及沿脱附气体回流支路管道60通入第二流化床30中的解吸气体的温度由辅助解吸气体输送管道65的加热装置66和脱附气体回流的支路管道60的加热装置62控制。In this operating state, the thermal desorption gas introduced by the gas inlet 31 includes: the product carbon dioxide passed into the second fluidized bed 30 along the branch pipeline 60 of desorption gas return, and the product carbon dioxide transported along the auxiliary desorption gas Pipe 65 leads to carbon dioxide outside the system in second fluidized bed 30 . The reason for selecting this operating state is: the total amount of product carbon dioxide returned by the desorption gas reflux branch pipeline 60 of the second fluidized bed 30 fails to reach enough desorption adsorbent in the first fluidized bed 20 and/or the second fluidized bed. All the carbon dioxide adsorbed in the fluidized bed 30, in this operating state, the desorption gas for desorbing carbon dioxide is heated carbon dioxide, and no other gas other than carbon dioxide has been added, so it is removed from the desorption gas pipeline 33 of the second fluidized bed The carbon dioxide purity of the system is high. Simultaneously, the desorption gas flow rate that passes into the second fluidized bed 30 along the auxiliary desorption gas delivery pipeline 65 and along the desorption gas reflux branch pipeline 60 is controlled by the regulating valve (not marked) and the desorption gas delivery pipeline 65 of the auxiliary desorption gas. The regulating valve 61 of the attached gas reflux branch pipeline 60 is controlled, and the temperature of the desorption gas passed into the second fluidized bed 30 along the auxiliary desorption gas delivery pipeline 65 and along the desorption gas reflux branch pipeline 60 is transported by the auxiliary desorption gas The heating device 66 of the pipeline 65 and the heating device 62 of the branch pipeline 60 for desorbed gas reflux are controlled.
在第二流化床30中，在解吸或脱附时，吸附二氧化碳达到饱和或接近饱和的吸附剂与上述热解吸气体相接触而使自身温度升高至解吸温度以上，从而脱附二氧化碳，结果得到新鲜或再生的吸附剂。将新鲜或再生的吸附剂从第二流化床30顶部的第二分离器50底部沿第二流化床30的连通管道34移至第一流化床20中，从而完成吸附剂在第一流化床20和第二流化床30之间的脱附循环。脱附得到的产物二氧化碳从第二分离器50的顶部沿第二流化床30的脱附气体输送管道33移出系统。In the second fluidized bed 30, when desorbing or desorbing, the adsorbent that has adsorbed carbon dioxide to reach saturation or close to saturation is in contact with the above-mentioned thermal desorption gas to raise its own temperature above the desorption temperature, thereby desorbing carbon dioxide , resulting in fresh or regenerated adsorbent. The fresh or regenerated adsorbent is moved from the bottom of the second separator 50 at the top of the second fluidized bed 30 to the first fluidized bed 20 along the communication pipe 34 of the second fluidized bed 30, thereby completing the adsorption of the adsorbent in the first fluidized bed. The desorption cycle between the fluidized bed 20 and the second fluidized bed 30 . The product carbon dioxide obtained by desorption is removed from the system from the top of the second separator 50 along the desorption gas delivery pipeline 33 of the second fluidized bed 30 .
如上所述，在第三种运行状态下，当第二流化床30进行解吸时，将第二流化床30的气体混合物输送管道35的开关63和辅助解吸气体输送管道65的开关67关闭，而将脱附气体、即产物气体回流支路管道60的开关64开启。As mentioned above, in the third operating state, when the second fluidized bed 30 is desorbing, the switch 63 of the gas mixture delivery pipeline 35 of the second fluidized bed 30 and the switch 67 of the auxiliary desorption gas delivery pipeline 65 are closed , and the switch 64 of the desorption gas, that is, the product gas return branch pipeline 60 is turned on.
二氧化碳在第三种运行状态下的吸附过程与在第二种运行状态下的吸附过程相同，去除至少部分、或大部分二氧化碳的气体混合物从第一流化床20的其气体出口沿着分离器40顶部的输出管道23移出系统外，而吸附二氧化碳的吸附剂或吸附二氧化碳达到饱和或接近饱和的吸附剂从分离器40底部沿着第一流化床20的连通管道24移至第二流化床30中。The adsorption process of carbon dioxide in the third operating state is the same as that in the second operating state, the gas mixture with at least part or most of the carbon dioxide removed from the gas outlet of the first fluidized bed 20 along the separator The output pipe 23 at the top of 40 moves out of the system, and the adsorbent for adsorbing carbon dioxide or the adsorbent for adsorbing carbon dioxide that is saturated or nearly saturated moves from the bottom of the separator 40 to the second fluidized bed along the communication pipe 24 of the first fluidized bed 20 Bed 30 in.
将吸附二氧化碳的吸附剂或吸附二氧化碳达到饱和或接近饱和的吸附剂从第一流化床20中通过分离器40和连通管道24移至第二流化床30的下端，在第二流化床30中吸附二氧化碳达到饱和或接近饱和的吸附剂与从第二流化床30的气体进口31通入的热解吸气体相接触，使其达到二氧化碳解吸温度后放出二氧化碳，被脱附出来的二氧化碳通过第二流化床30的脱附气体管道33移出系统。在此运行状态下，在解吸或脱附时，由气体进口31通入的热解吸气体为沿脱附气体回流支路管道60通入第二流化床30中的产物二氧化碳。由第二流化床30的脱附气体输出管道33移出系统的至少一部分二氧化碳沿着脱附气体回流支路管道60通入第二流化床30中，用于脱附吸附剂在第一流化床20和/或第二流化床30中吸附的二氧化碳，优选地，通过所述脱附气体回流支路管道60用于脱附被吸附剂吸附的二氧化碳的产物二氧化碳数量占所述系统产生的总二氧化碳数量的10～60(体积)％。在此运行状态下，解吸气体是加热后的产物二氧化碳，未加入二氧化碳以外的其它气体，所以从第二流化床30的脱附气体输出管道33移出系统的二氧化碳纯度较高。沿脱附气体回流支路管道60通入第二流化床30中的产物气体流量由脱附气体回流支路管道60的调节阀61控制，而回流产物气体温度由脱附气体回流支路管道60的加热装置62控制。The adsorbent for adsorbing carbon dioxide or the adsorbent for adsorbing carbon dioxide reaching saturation or near saturation is moved from the first fluidized bed 20 to the lower end of the second fluidized bed 30 through the separator 40 and the communication pipe 24, and the second fluidized bed The adsorbent in 30 that has adsorbed carbon dioxide reaching saturation or close to saturation is in contact with the thermal desorption gas introduced from the gas inlet 31 of the second fluidized bed 30, so that it reaches the carbon dioxide desorption temperature and releases carbon dioxide, which is desorbed Carbon dioxide is removed from the system through desorption gas line 33 of second fluidized bed 30 . In this operating state, during desorption or desorption, the thermal desorption gas introduced through the gas inlet 31 is the product carbon dioxide which is introduced into the second fluidized bed 30 along the desorption gas return branch pipeline 60 . At least a part of the carbon dioxide that is removed from the system by the desorption gas output pipeline 33 of the second fluidized bed 30 passes into the second fluidized bed 30 along the desorption gas return branch pipeline 60, and is used for the desorption of the adsorbent in the first fluidized bed. The carbon dioxide adsorbed in the bed 20 and/or the second fluidized bed 30, preferably, the amount of carbon dioxide produced by the desorbed gas reflux branch pipeline 60 for desorbing the carbon dioxide adsorbed by the adsorbent accounted for by the system 10-60 (volume)% of the total carbon dioxide. In this operating state, the desorption gas is the heated product carbon dioxide, and no gas other than carbon dioxide is added, so the purity of the carbon dioxide removed from the system from the desorption gas output pipe 33 of the second fluidized bed 30 is relatively high. The product gas flow rate passed into the second fluidized bed 30 along the desorption gas return branch pipeline 60 is controlled by the regulating valve 61 of the desorption gas return branch pipeline 60, and the temperature of the backflow product gas is controlled by the desorption gas return branch pipeline. 60 heating device 62 control.
在第二流化床30中，吸附二氧化碳达到饱和或接近饱和的吸附剂与上述热解吸气体相接触而使自身温度升高至解吸温度以上，从而脱附二氧化碳，结果得到新鲜或再生的吸附剂。将新鲜或再生的吸附剂从第二流化床30顶部的第二分离器50底部沿着第二流化床30的连通管道34移至第一流化床20中，从而完成吸附剂在第一流化床20和第二流化床30之间的脱附循环。脱附得到的二氧化碳则从第二分离器50顶部沿着第二流化床30的脱附气体管道33移出系统。In the second fluidized bed 30, the adsorbent that has adsorbed carbon dioxide to be saturated or nearly saturated is in contact with the above-mentioned thermal desorption gas to increase its own temperature above the desorption temperature, thereby desorbing carbon dioxide, resulting in fresh or regenerated Adsorbent. The fresh or regenerated adsorbent is moved from the bottom of the second separator 50 at the top of the second fluidized bed 30 to the first fluidized bed 20 along the communication pipe 34 of the second fluidized bed 30, thereby completing the first fluidized bed 20 of the adsorbent. The desorption cycle between the first fluidized bed 20 and the second fluidized bed 30. The desorbed carbon dioxide is then removed from the top of the second separator 50 along the desorbed gas pipeline 33 of the second fluidized bed 30 out of the system.
在以上三种运行状态下，脱附得到的二氧化碳产物从第二流化床30中移出系统后，按照需求也可作进一步处理，产物气体或脱附气体从第二分离器50顶部沿第二流化床30的脱附气体管道33移出系统后，可使其通过各种气、固、液分离器，例如气体过滤器70和干燥器80，之后沿气态二氧化碳产物输送管道81输出经处理后得到的气态高纯二氧化碳产物。或者，再使其进一步通过气体压缩机90，经压缩后沿液态二氧化碳输送管道91输出液态高纯二氧化碳产物。In the above three operating states, after the carbon dioxide product obtained by desorption is removed from the second fluidized bed 30, it can be further processed according to requirements. The product gas or desorbed gas is passed from the top of the second separator 50 along the second After the desorption gas pipeline 33 of the fluidized bed 30 is removed from the system, it can pass through various gas, solid and liquid separators, such as a gas filter 70 and a dryer 80, and then output the treated gas along the gaseous carbon dioxide product delivery pipeline 81. The resulting gaseous high-purity carbon dioxide product. Or, make it further pass through the gas compressor 90, and output the liquid high-purity carbon dioxide product along the liquid carbon dioxide delivery pipeline 91 after being compressed.
图2是本发明气体分离系统另一个实施方案，其为吸附和脱附气体的系统10b，其特定的吸附气体仍为二氧化碳，系统10b的运行原理与系统10a相同，不同的是系统10b与系统10a相比省去了第二流化床30设置于其顶部的第二分离器50。主要组件标记数说明亦参见表1。系统10b主要包括一个第一流化床(吸附塔)20、一个第二流化床(吸附-脱附塔)30、气-固分离器40、第一流化床20的气体混合物输送管道11、第二流化床30的气体混合物输送管道35、第一流化床20的气体输出管道23、第二流化床30的脱附气体输出管道33、脱附气体管道33的脱附气体回流支路管道60和输送来自系统外的解吸气体的辅助解吸气体输送管道65，其中，第一流化床20和第二流化床30中装有可再生吸附剂，第一流化床20通过其顶部设置的分离器40与第二流化床30连通，第二流化床30的上端与第一流化床20的下端连通，从而使所述吸附剂在第一流化床20和第二流化床30之间循环。Fig. 2 is another embodiment of the gas separation system of the present invention, and it is the system 10b of adsorption and desorption gas, and its specific adsorption gas is still carbon dioxide, and the operating principle of system 10b is identical with system 10a, and difference is that system 10b is different from system 10a omits the second separator 50 at the top of which the second fluidized bed 30 is arranged. See also Table 1 for the description of the marking numbers of the main components. The system 10b mainly includes a first fluidized bed (adsorption tower) 20, a second fluidized bed (adsorption-desorption tower) 30, a gas-solid separator 40, and a gas mixture delivery pipeline 11 for the first fluidized bed 20 , the gas mixture delivery pipeline 35 of the second fluidized bed 30, the gas output pipeline 23 of the first fluidized bed 20, the desorption gas output pipeline 33 of the second fluidized bed 30, the desorption gas reflux of the desorption gas pipeline 33 The branch pipeline 60 and the auxiliary desorption gas delivery pipeline 65 for transporting the desorption gas from outside the system, wherein, the first fluidized bed 20 and the second fluidized bed 30 are equipped with a regenerable adsorbent, and the first fluidized bed 20 passes through The separator 40 arranged at its top communicates with the second fluidized bed 30, and the upper end of the second fluidized bed 30 communicates with the lower end of the first fluidized bed 20, so that the adsorbent is in the first fluidized bed 20 and the second fluidized bed. Circulation between the two fluidized beds 30.
应注意的是：如图1和2所示，在系统10a中，二氧化碳与吸附剂进行接触的方式都是顺流接触，而在系统10b中，二氧化碳在第一流化床中与吸附剂进行接触的方式是顺流接触，二氧化碳在第二流化床中与吸附剂进行接触的方式也是顺流接触。It should be noted that: as shown in Figures 1 and 2, in the system 10a, the carbon dioxide and the adsorbent are contacted in a down-flow manner, while in the system 10b, the carbon dioxide is contacted with the adsorbent in the first fluidized bed. The way of contact is down-current contact, and the way of contacting the carbon dioxide with the adsorbent in the second fluidized bed is also down-current contact.
上述三种运行方式以及图1和图2所示的实施方式仅是列举和示范，并未穷尽本发明气体分离系统的所用运行方式和实施方式，本发明不排除符合本发明实质和原理的其它运行方式和实施方式。The above three modes of operation and the implementations shown in Figures 1 and 2 are merely enumerations and demonstrations, and do not exhaust the operating modes and implementations of the gas separation system of the present invention, and the present invention does not exclude other that conform to the essence and principles of the present invention mode of operation and implementation.
实施例Example
实施例1Example 1
用图1所示的本发明气体分离系统从煤燃烧后的气体混合物中分离二氧化碳，该分离系统为实验室规模的分离装置，气体混合物原料的化学成分组成如表1所示：Use the gas separation system of the present invention shown in Figure 1 to separate carbon dioxide from the gas mixture after coal combustion, this separation system is a laboratory-scale separation device, and the chemical composition of the gas mixture raw material is as shown in Table 1:
表1Table 1
在该气体分离系统中，选择的吸附-脱附介质、即吸附剂为固态胺二氧化碳吸附剂(重量比为1：1的DEA-MCM-41，商购自美国FISHER或UOP公司)，其颗粒直径为60-80微米，含水量小于1重量％，二氧化碳的吸附和解吸特性如表2所示：In this gas separation system, the selected adsorption-desorption medium, that is, the adsorbent is a solid amine carbon dioxide adsorbent (DEA-MCM-41 with a weight ratio of 1:1, commercially available from FISHER or UOP in the United States), and its particles The diameter is 60-80 microns, and the water content is less than 1% by weight. The adsorption and desorption characteristics of carbon dioxide are shown in Table 2:
表2Table 2
采取上述第三种运行状态，即解吸气体完全是回流的二氧化碳产物气体，在系统启动并运行正常后，流化床20的工作压力是0.133MPa，工作温度是40-51℃；而流化床30的工作压力也是0.133MPa，其吸附时工作温度是40-51℃；脱附时工作温度为113℃，系统的其它各工艺参数如表3所示：Take the above-mentioned third operating state, that is, the desorption gas is completely refluxed carbon dioxide product gas. After the system starts and operates normally, the working pressure of the fluidized bed 20 is 0.133MPa, and the working temperature is 40-51°C; while the fluidized bed The working pressure of 30 is also 0.133MPa, and its working temperature is 40-51°C during adsorption; and 113°C during desorption. Other process parameters of the system are shown in Table 3:
表3table 3
流化床30在吸附和脱附时工作温度是不同的，为了迅速实现其吸附塔和脱附塔之间的转变，可在流化床30的内部设置热交换器(未示出)或在吸附开始时通入温度较低的气体混合物原料，使新鲜或再生吸附剂和气体混合物原料接触后温度达到40-43℃左右，而从分离器50流入管道24中的新鲜或再生吸附剂温度也较高，也可在管道24中或流化床20的内部设置热交换器(未示出)或在吸附开始时向流化床20中也通入温度较低的气体混合物原料，使其中新鲜或再生吸附剂和气体混合物原料接触后温度也达到40-43℃左右。The working temperature of the fluidized bed 30 is different during adsorption and desorption, in order to quickly realize the transition between the adsorption tower and the desorption tower, a heat exchanger (not shown) can be set inside the fluidized bed 30 or in When the adsorption starts, the gas mixture raw material with a lower temperature is introduced, so that the temperature of the fresh or regenerated adsorbent and the gas mixture raw material reaches about 40-43° C., and the temperature of the fresh or regenerated adsorbent flowing into the pipeline 24 from the separator 50 is also high. Higher, a heat exchanger (not shown) can also be set in the pipeline 24 or the inside of the fluidized bed 20, or the gas mixture raw material with a lower temperature can be introduced into the fluidized bed 20 when the adsorption starts, so that fresh Or the temperature of the regenerated adsorbent and the raw material of the gas mixture also reaches about 40-43°C.
如表2所示，吸附剂的脱附速度是其吸附速度的7.1倍，因此，吸附剂在流化床20和30中停留7次后，在流化床30中进行一次解吸或脱附，从而完成一个吸附和脱附的总的循环。As shown in Table 2, the desorption rate of the adsorbent is 7.1 times of its adsorption rate, therefore, after the adsorbent stays in the fluidized bed 20 and 30 for 7 times, desorption or desorption is performed once in the fluidized bed 30, Thereby completing a total cycle of adsorption and desorption.
脱附或分离二氧化碳后的气体混合物的化学成分组成如表4所示：The chemical composition of the gas mixture after desorption or separation of carbon dioxide is shown in Table 4:
表4Table 4
二氧化碳重量吸附率为：(25.67-2.68×(100-25.67)/(100-2.68))/25.67＝92％；而二氧化碳的体积吸附率为：(17.65-1.68×(100-17.68)/(100-1.68))/17.65＝92％。Carbon dioxide weight adsorption rate: (25.67-2.68×(100-25.67)/(100-2.68))/25.67=92%; and carbon dioxide volume adsorption rate: (17.65-1.68×(100-17.68)/(100 -1.68))/17.65=92%.
从本发明实施例1中可看出：本发明利用吸附-脱附介质吸附速度和脱附速度的差异改进了现有的吸附-脱附气体分离系统，使得吸附设备尺寸变小，并同时增加了吸附和脱附效率，从而最终大大改善了气体分离的效率和设备的可操作性。As can be seen from Example 1 of the present invention: the present invention improves the existing adsorption-desorption gas separation system by utilizing the difference between the adsorption-desorption medium adsorption speed and the desorption speed, so that the size of the adsorption equipment becomes smaller and increases simultaneously. The efficiency of adsorption and desorption is improved, and finally the efficiency of gas separation and the operability of equipment are greatly improved.
本说明书所用的术语和表述方式仅被用作描述性、而非限制性的术语和表述方式，在使用这些术语和表述方式时无意将已表示和描述的特征或其组成部分的任何等同物排斥在外。The terms and expressions used in this specification are used only as descriptive, not restrictive terms and expressions, and when using these terms and expressions, it is not intended to exclude any equivalents of the features shown and described or their components outer.
尽管已表示和描述了本发明的几个实施方式，但本发明不被限制为所描述的实施方式。相反，本领域普通技术人员应当意识到在不脱离本发明原则和精神的情况下可对这些实施方式进行任何变通和改进，本发明的保护范围由所附的权利要求及其等同物所确定。While several embodiments of the invention have been shown and described, the invention is not limited to the described embodiments. On the contrary, those skilled in the art should realize that any modifications and improvements can be made to these embodiments without departing from the principle and spirit of the present invention, and the protection scope of the present invention is determined by the appended claims and their equivalents.
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| CN106118777A (en) * | 2016-08-24 | 2016-11-16 | 深圳前海中盛环保科技有限公司 | A kind of marsh gas purifying purifies the method for methane |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57107218A (en) * | 1980-12-26 | 1982-07-03 | Mitsubishi Heavy Ind Ltd | Method for adsorption and separation of gaseous mixture |
| JPH11179139A (en) * | 1997-12-24 | 1999-07-06 | Mitsubishi Heavy Ind Ltd | Organic gas treating equipment |
| US6755892B2 (en) * | 2000-08-17 | 2004-06-29 | Hamilton Sundstrand | Carbon dioxide scrubber for fuel and gas emissions |
| CN101443275A (en) * | 2006-03-31 | 2009-05-27 | 西班牙高等科研理事会 | Precalcination method with production of pure or easily purified CO2 originating from the decomposition of carbonates |
| CN101549241A (en) * | 2009-05-01 | 2009-10-07 | 宇星科技发展(深圳)有限公司 | Pressure swing adsorption recovery unit of organic exhaust gas and method thereof |
| CN102292138A (en) * | 2009-01-22 | 2011-12-21 | 通用电气公司 | Fluidized bed system for removing multiple pollutants from a fuel gas stream |
-
2012
- 2012-01-20 CN CN201210019373.4A patent/CN103212271B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57107218A (en) * | 1980-12-26 | 1982-07-03 | Mitsubishi Heavy Ind Ltd | Method for adsorption and separation of gaseous mixture |
| JPH11179139A (en) * | 1997-12-24 | 1999-07-06 | Mitsubishi Heavy Ind Ltd | Organic gas treating equipment |
| US6755892B2 (en) * | 2000-08-17 | 2004-06-29 | Hamilton Sundstrand | Carbon dioxide scrubber for fuel and gas emissions |
| CN101443275A (en) * | 2006-03-31 | 2009-05-27 | 西班牙高等科研理事会 | Precalcination method with production of pure or easily purified CO2 originating from the decomposition of carbonates |
| CN102292138A (en) * | 2009-01-22 | 2011-12-21 | 通用电气公司 | Fluidized bed system for removing multiple pollutants from a fuel gas stream |
| CN101549241A (en) * | 2009-05-01 | 2009-10-07 | 宇星科技发展(深圳)有限公司 | Pressure swing adsorption recovery unit of organic exhaust gas and method thereof |
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