JPS58132192A - Direct caustification using fluidized layer furnace - Google Patents
Direct caustification using fluidized layer furnaceInfo
- Publication number
- JPS58132192A JPS58132192A JP1014982A JP1014982A JPS58132192A JP S58132192 A JPS58132192 A JP S58132192A JP 1014982 A JP1014982 A JP 1014982A JP 1014982 A JP1014982 A JP 1014982A JP S58132192 A JPS58132192 A JP S58132192A
- Authority
- JP
- Japan
- Prior art keywords
- black liquor
- fluidized bed
- furnace
- bed furnace
- iron oxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 51
- 238000000034 method Methods 0.000 claims description 19
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 17
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 14
- 238000002485 combustion reaction Methods 0.000 claims description 14
- 239000000843 powder Substances 0.000 claims description 12
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 9
- 239000011734 sodium Substances 0.000 claims description 9
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 229910052708 sodium Inorganic materials 0.000 claims description 5
- 238000009993 causticizing Methods 0.000 claims description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 2
- 229910044991 metal oxide Inorganic materials 0.000 claims 1
- 150000004706 metal oxides Chemical class 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 10
- 229910021311 NaFeO2 Inorganic materials 0.000 description 9
- 229910001868 water Inorganic materials 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical class [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 229920005610 lignin Polymers 0.000 description 4
- 238000010411 cooking Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 235000017550 sodium carbonate Nutrition 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- 229920003043 Cellulose fiber Polymers 0.000 description 1
- 229910021260 NaFe Inorganic materials 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
Landscapes
- Compounds Of Iron (AREA)
- Paper (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
この発明はパルプ製造工程で生じる黒液と称する廃液中
から苛性ソーダを中心とする薬品を回収する方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for recovering chemicals, mainly caustic soda, from a waste liquid called black liquor produced in a pulp manufacturing process.
製紙工場においてパルプ製造工程では木材成分のセルロ
ーズ（繊維）とリグニン（樹脂）を分離してセルローズ
のみを取り出すため苛性ソーダ（ＮａＯＨ）を中心とし
た薬品を用いる。蒸解工程を経た溶解リグニンとＮａ叶
を含有する溶液は黒液と称する廃液として排出されるが
、この黒液を燃焼させることにより熱回収を行ない、か
つ同時にＮａＯＨを回収して再使用する方法が従来から
実施されている。しかしこの方法は黒液燃焼装置を精密
に制御することにより同装置内で黒液を燃焼させてＮ
ａ ２ ＣＯ３を反応生成させ、このＮａ２ＣＯ３を別
の工程で生成した消石灰（Ｃａ （ＯＨ）２ ）と反応
させることによりＮａＯＨを回収するものであり、反応
過程が複雑で太きな設備を必要とし、かつＮａＯＨ生成
の際に生じたＯ ａ ００３を消和工程を経てＯａ （
ＯＨ） ２に戻すために多大なエネルギーを消費すると
いう問題がある。このため設備の簡略化、エネルギー消
費の減少を図って直接苛性化法と称するＮａＯＨ回収方
法が提案されている。第１図を用いてこの直接苛性化法
の概略を説明すると、木材チップは蒸解工程１において
ＮａＯＨによりリグニンが分離され、リグニンおよびＮ
ａｅを含有する黒液は燃焼過程２において酸化鉄粉とし
てＦｅ２０３を添加することにより次式の反応を行なう
。In the pulp manufacturing process at paper mills, chemicals such as caustic soda (NaOH) are used to separate the wood components cellulose (fiber) and lignin (resin) and extract only the cellulose. The solution containing dissolved lignin and Na leaves after the cooking process is discharged as a waste liquid called black liquor, but there is a method that recovers heat by burning this black liquor and at the same time recovers and reuses NaOH. This has been practiced for a long time. However, this method requires precise control of the black liquor combustion device to burn the black liquor in the same device and produce nitrogen.
NaOH is recovered by reacting a2CO3 and reacting this Na2CO3 with slaked lime (Ca(OH)2) produced in another process, and the reaction process is complicated and requires large equipment. , and Oa (
OH) There is a problem that a large amount of energy is consumed to return to 2. For this reason, an NaOH recovery method called a direct causticization method has been proposed to simplify equipment and reduce energy consumption. To explain the outline of this direct causticizing method using Fig. 1, lignin is separated from wood chips using NaOH in cooking step 1, and lignin and N
Black liquor containing ae undergoes the following reaction by adding Fe203 as iron oxide powder in combustion process 2.
２ＮａＯＨ＋ Ｃｏ２ Ｎａ２ｃｏ３＋ Ｈ２Ｏ
・（１）Ｎａ ００−１− Ｆｅ Ｏ→２ＮａＦｅＯ−
１−（！Ｏ−・・（２）２３２３
２２
このうち鉄酸ナトリウム（ＮａＦｅＯ２）は次段階の溶
解過程３において加水分解されＮａＯＨを回収する。2NaOH+ Co2 Na2co3+ H2O
・(1) Na 00-1- Fe O → 2NaFeO-
1-(!O-...(2)2323
22 Of these, sodium ferrate (NaFeO2) is hydrolyzed in the next dissolution step 3 to recover NaOH.
２ＮａＦｅＯ２＋ Ｈ２０→２ＮａＯＨ＋ Ｆｅ２０３
−（３）つまり直接苛性化法では（ＬＬ （２Ｌ （３
）の反応を行なうことによりＮａＯＨの回収を行なうこ
とができると共に、この回収に使用したＦｅ２０３を循
環再使用することができ、従来方法と比較して設備費、
エネルギー消費縁を大幅に減少させることができるとい
う利点がある。2NaFeO2+ H20→2NaOH+ Fe203
-(3) In other words, in the direct causticization method (LL (2L (3
) NaOH can be recovered by carrying out the reaction, and the Fe203 used for this recovery can be recycled and reused, reducing equipment costs and costs compared to conventional methods.
The advantage is that energy consumption can be significantly reduced.
以上の方法においてＮａＦｅＯ２は粉状で回収するとそ
の輸送、加水分解等において便利であるが、反対に燃焼
装置から粉状のＮａＦｅＯ２を回収することは困難とな
る。In the above method, collecting NaFeO2 in powder form is convenient for transportation, hydrolysis, etc., but on the other hand, it is difficult to collect NaFeO2 in powder form from a combustion device.
また黒液中から１ＪａＯＨを効率良く回収するためには
供給するＦｅ２Ｏ３と、式（１）に示す反応により生じ
たＮａ２ＣＯ３とのモル比を１以上とすること、及び黒
液とＦｅ２Ｏ３とが長幼に混合していることが条件とな
る。In addition, in order to efficiently recover 1JaOH from black liquor, the molar ratio of Fe2O3 to be supplied and Na2CO3 produced by the reaction shown in equation (1) should be 1 or more, and the black liquor and Fe2O3 should be The condition is that they are mixed.
この発明の目的は上述した技術的課題を達成しＮａＯＨ
の回収効率を大幅に向トさせることが可能な直接苛性化
方法を提供することにある。The purpose of this invention is to achieve the above-mentioned technical problems and to
The object of the present invention is to provide a direct causticization method that can greatly improve the recovery efficiency of .
要するにこの発明は黒液を燃焼させ、かつき有するＮａ
分とＦ ｅ ２０３との反応を行なう燃焼装置を流動層
炉として、反応生成したＮ ａ Ｆ（３０２を後続の集
塵装置においてほぼ完全に回収し、一方流動層炉に供給
する黒液は予混合装置において、あらかじめ定められた
モル比に基づいてＦｅ２０３等の酸化鉄粉と良好に混合
し炉内での反応を効果的に行なうようにしたものである
。In short, this invention burns black liquor and has Na
A fluidized bed furnace is used as the combustion device for the reaction between F e 203 and F e 203, and the reaction produced N a F (302) is almost completely recovered in the subsequent dust collector, while the black liquor supplied to the fluidized bed furnace is In the mixing device, the powder is well mixed with iron oxide powder such as Fe203 based on a predetermined molar ratio, and the reaction in the furnace is effectively carried out.
以丁この発明に係る方法を図面を参考に説明する。The method according to the present invention will now be explained with reference to the drawings.
第２図において、１０は黒液燃焼装置（反応装置も兼ね
る）である流動層ボイラ（流動層炉）であり、ボイラ内
に形成した流動層１０ａ内には層内伝熱管１０ｂが配置
してあり、黒液燃焼により生じた熱を回収すると共に給
水Ｗ工の通過散を調節することにより層内温度を制御す
る。ここで、前記（ＩＬ （２）により生じるＮａＦｅ
Ｏ２の軟化点は１１００℃以−Ｌ１溶融点は１１８０’
Ｃ以上でありＮａＦｅＯ２は前述の如く粉状で回収した
いので層内温度は１１００℃以下になるよう、弁４によ
り給水Ｗ□を、弁５を調節して黒液の供給量を各々制御
する。以上の制御により生じたＮａＦｅＯ２は粒径が１
００μ以下の微細な粒子の粉状であり炉内を」−がする
燃焼排ガスと共に炉外に排出され集塵装置（図示のもの
はサイクロン） １２に至りＮａＦｅＯ２が回収され、
排ガスＧは系外に排出される。この場合、流動層炉１０
で発生したＮａＦｅＯ２の殆んどは排ガスＧと共に炉外
に流出し、かつサイクロン式集塵装置の場合、捕集可能
な最低粒径は約１０μとされているので、結局流動層炉
１０で発生したＮａＦｅＯ２の殆んど全部が集塵装置１
２で捕集されることになる。捕集されたＮ ａ Ｆ ｅ
０２はホッパ１３に至り、溶解水Ｗ２の供給ｂｔに対
応してロータリーフィーダ１４で供給ばか調節され溶解
槽１６に至る。ここで式（３）に示す加水分解が行なわ
れ、ＮａＯＨとＦ ｅ２０ψｆ生じる。この場合、溶解
槽１６内の溶液は加熱した方が反応が促進されるが、加
熱媒体としては流動層ボイラ１０で発生し、かつ管路４
０を経て供給された温水または蒸気により加熱される。In FIG. 2, 10 is a fluidized bed boiler (fluidized bed furnace) which is a black liquor combustion device (also serving as a reaction device), and an intrabed heat exchanger tube 10b is arranged in a fluidized bed 10a formed in the boiler. The temperature inside the bed is controlled by recovering the heat generated by black liquor combustion and adjusting the dissipation through the water supply W. Here, NaFe generated by the above (IL (2))
O2 softening point is 1100℃ or higher - L1 melting point is 1180'
Since NaFeO2 is desired to be recovered in powder form as described above, the water supply W□ is controlled by the valve 4, and the amount of black liquor supplied is controlled by the valve 5 so that the temperature in the bed is below 1100°C. The NaFeO2 produced by the above control has a particle size of 1
NaFeO2 is in the form of fine particles of 00μ or less, and is discharged from the furnace together with the combustion exhaust gas that flows through the furnace.
The exhaust gas G is discharged outside the system. In this case, the fluidized bed furnace 10
Most of the NaFeO2 generated in the fluidized bed furnace 10 flows out of the furnace together with the exhaust gas G, and in the case of a cyclone type dust collector, the minimum particle size that can be collected is approximately 10μ, so in the end most of the NaFeO2 generated in the fluidized bed furnace 10 flows out of the furnace together with the exhaust gas G. Almost all of the NaFeO2 was removed from the dust collector 1.
It will be collected in 2. Collected N a Fe
02 reaches the hopper 13, and is adjusted by the rotary feeder 14 in accordance with the supply bt of the dissolving water W2, and reaches the dissolving tank 16. Here, the hydrolysis shown in formula (3) is performed to produce NaOH and Fe20ψf. In this case, heating the solution in the dissolution tank 16 accelerates the reaction, but the heating medium is generated in the fluidized bed boiler 10 and in the pipe line 4.
It is heated by hot water or steam supplied through 0.
加水分解されたＮａＯＨとＦｅ２Ｏ３の混合液は管路１
７により沈降槽１９に供給され、沈降分離したＦｅ２Ｏ
３は管路３９を経て脱水機２０に供給される。The mixed solution of hydrolyzed NaOH and Fe2O3 is in pipe 1.
Fe2O is supplied to the sedimentation tank 19 by 7 and separated by sedimentation.
3 is supplied to the dehydrator 20 through a pipe line 39.
一方沈降槽１９から溢流したＮａＯＨは溢流槽２３に流
入し、さらに管路２４を経てＮａＯＨ貯槽２７に貯留さ
れ、管路２８を経て遂次蒸解１程で使用される。なお、
脱水機２０から排出された液体（ＮａＯＨ）は管路２６
を経てＮａＯＨ貯槽２７に供給される。On the other hand, NaOH overflowing from the sedimentation tank 19 flows into the overflow tank 23, passes through the pipe line 24, is stored in the NaOH storage tank 27, passes through the pipe line 28, and is used in the first stage of sequential cooking. In addition,
The liquid (NaOH) discharged from the dehydrator 20 is transferred to the pipe 26
It is supplied to the NaOH storage tank 27 through.
次に脱水機２０から排出されたＦ ｅ ２ Ｃ！３の脱
水ケーキはコンベヤ３０によりホッパ３１に貯留されさ
らにスクリューフィーダ３２．コンベヤ３３により混合
槽３５に供給され、供給された黒液３４と混合撹拌され
る。この場合、後続の流動層炉１０においてＦｅ２Ｏ２
とＮａ２（１！０ρモル比が１以上となるようこの混合
槽３５においてＦｅ２．．０３と黒液３４４・との混合
比率を定めておく。また黒液は燃焼し功いよう濃縮して
あり、常温では粘性が非常に高くなるので黒液を加熱し
流動化し易いようにしておく必要があるが、この場合の
加熱手段も前述の溶解槽１６の場合と同様に流動層炉１
０において発生した温水もしくは蒸気とすれば省エネル
ギー化を図ることができる。符号４１は流動層炉１ｏで
発生した温水もしくは蒸気を供給する管路である。Ｆｅ
２Ｏ３を所定量混合した黒液は管路１１を経て流動層炉
１０に供給され、燃焼およびＮａＦθ０２の生成が行な
われる。Next, F e 2 C discharged from the dehydrator 20! The dehydrated cake No. 3 is stored in a hopper 31 by a conveyor 30 and further transferred to a screw feeder 32. It is supplied to a mixing tank 35 by a conveyor 33, and is mixed and stirred with the supplied black liquor 34. In this case, in the subsequent fluidized bed furnace 10, Fe2O2
The mixing ratio of Fe2..03 and black liquor 344 is determined in this mixing tank 35 so that the molar ratio of Since the viscosity becomes very high at room temperature, it is necessary to heat the black liquor to make it easier to fluidize. In this case, the heating means is also the fluidized bed furnace 1, as in the case of the melting tank 16 described above.
If the hot water or steam generated at 0 is used, energy saving can be achieved. Reference numeral 41 is a pipe line for supplying hot water or steam generated in the fluidized bed furnace 1o. Fe
Black liquor mixed with a predetermined amount of 2O3 is supplied to the fluidized bed furnace 10 through a pipe 11, where it is combusted and NaFθ02 is generated.
この発明を実施することにより燃焼装置で発生したＮａ
Ｆθ０２を、処理のし易い粉状で、しかもほぼ全量回収
することができ、プラント全体の効率を高めることがで
きる。Na generated in the combustion device by implementing this invention
Fθ02 can be recovered in powder form, which is easy to process, and almost the entire amount can be recovered, making it possible to improve the efficiency of the entire plant.
また燃焼装置に供給する黒液と酸化鉄粉をあらかじめ定
めらたモル比でしかも良好に混合しであるので、燃焼装
置におけるＮ ａ、Ｆ ｅ Ｏ２の反応を効果的に行な
うことができる。Furthermore, since the black liquor and iron oxide powder supplied to the combustion device are well mixed at a predetermined molar ratio, the reactions of Na and FeO2 in the combustion device can be carried out effectively.
第１図は直接苛性化法の概略を示す系統図、第２図はこ
の発明に係る方法を実施するプラントの系統図である。
１０・・・・・・流動層炉
１０ａ・・・・・・流動層
１２・・・・・・集塵装置
３４・・・・・・黒液
３５・・・・・・混合槽FIG. 1 is a system diagram showing an outline of the direct causticizing method, and FIG. 2 is a system diagram of a plant implementing the method according to the present invention. 10... Fluidized bed furnace 10a... Fluidized bed 12... Dust collector 34... Black liquor 35... Mixing tank
Claims (1)
用いて回収する方法において、黒液と酸化鉄粉とをあら
かじめ混合し、この黒液を流動層炉で燃焼し、黒液燃焼
により生じた鉄酸ナトリウムが粉状であるよう炉内の燃
焼温度を制御し、燃焼排ガスと共に炉外に排出された粉
状鉄酸ナトリウムを集塵装置により捕集し、捕集した鉄
酸ナトリウムを苛性ソーダと酸化鉄に加水分解してこれ
ら苛性ソーダと酸化鉄を各々再使用することを特徴とす
る流動層炉を用いた直接苛性化方法。 ２、前記酸化鉄粉をＦｅ２Ｏ３とし、流動層炉内のＦｅ
２Ｏ３と炉内の燃焼で発生したＮａ２００３とのモル比
が１以上となるよう、黒液を流動層炉に供給する前工程
においてＦｅ２Ｏ３をこの黒液に対し予混合することを
特徴とする特徴とする特許請求の範囲第１項記載の流動
層炉を用いた直接苛性化方法。[Claims] 1. In a method for recovering the sodium component contained in black liquor using metal oxide powder, black liquor and iron oxide powder are mixed in advance, and the black liquor is combusted in a fluidized bed furnace. The combustion temperature inside the furnace is controlled so that the sodium ferrate produced by black liquor combustion is in powder form, and the powdered sodium ferrate discharged from the furnace together with the combustion exhaust gas is collected by a dust collector. A direct causticizing method using a fluidized bed furnace, characterized in that sodium ferrate is hydrolyzed into caustic soda and iron oxide, and these caustic soda and iron oxide are respectively reused. 2. The iron oxide powder is Fe2O3, and Fe in the fluidized bed furnace is
A feature characterized in that Fe2O3 is premixed with the black liquor in a pre-process of supplying the black liquor to the fluidized bed furnace so that the molar ratio of 2O3 and Na2003 generated by combustion in the furnace is 1 or more. A direct causticizing method using a fluidized bed furnace according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1014982A JPS58132192A (en) | 1982-01-27 | 1982-01-27 | Direct caustification using fluidized layer furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1014982A JPS58132192A (en) | 1982-01-27 | 1982-01-27 | Direct caustification using fluidized layer furnace |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS58132192A true JPS58132192A (en) | 1983-08-06 |
Family
ID=11742215
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1014982A Pending JPS58132192A (en) | 1982-01-27 | 1982-01-27 | Direct caustification using fluidized layer furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58132192A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59162128A (en) * | 1983-02-28 | 1984-09-13 | Kawasaki Heavy Ind Ltd | Recovery of sodium hydroxide from pulp waste |
| JPS6059190A (en) * | 1983-09-12 | 1985-04-05 | 川崎重工業株式会社 | Recovery of caustic soda from pulp waste liquid |
| JPS60181392A (en) * | 1984-02-06 | 1985-09-17 | 製紙技術研究組合 | Direct causticizing method using fluidized bed |
| JPS62268883A (en) * | 1986-05-16 | 1987-11-21 | 川崎重工業株式会社 | Soda recovery method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5112724A (en) * | 1974-07-23 | 1976-01-31 | Nippon Electric Co | |
| JPS53109899A (en) * | 1977-03-09 | 1978-09-26 | Toyo Pulp Co Ltd | Method of obtaining caustic soda from alkalline organic material |
| JPS54145396A (en) * | 1978-04-20 | 1979-11-13 | Australian Paper Manufacturers | Recovery of oxide or hydroxide of alkali or alkali earth metal |
| JPS5560020A (en) * | 1978-10-27 | 1980-05-06 | Toyo Pulp Kk | Alkaline waste liquor treating method |
-
1982
- 1982-01-27 JP JP1014982A patent/JPS58132192A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5112724A (en) * | 1974-07-23 | 1976-01-31 | Nippon Electric Co | |
| JPS53109899A (en) * | 1977-03-09 | 1978-09-26 | Toyo Pulp Co Ltd | Method of obtaining caustic soda from alkalline organic material |
| JPS54145396A (en) * | 1978-04-20 | 1979-11-13 | Australian Paper Manufacturers | Recovery of oxide or hydroxide of alkali or alkali earth metal |
| JPS5560020A (en) * | 1978-10-27 | 1980-05-06 | Toyo Pulp Kk | Alkaline waste liquor treating method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59162128A (en) * | 1983-02-28 | 1984-09-13 | Kawasaki Heavy Ind Ltd | Recovery of sodium hydroxide from pulp waste |
| JPS6059190A (en) * | 1983-09-12 | 1985-04-05 | 川崎重工業株式会社 | Recovery of caustic soda from pulp waste liquid |
| JPS60181392A (en) * | 1984-02-06 | 1985-09-17 | 製紙技術研究組合 | Direct causticizing method using fluidized bed |
| JPS62268883A (en) * | 1986-05-16 | 1987-11-21 | 川崎重工業株式会社 | Soda recovery method |
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