JPS6332726B2 - - Google Patents
Info
- Publication number
- JPS6332726B2 JPS6332726B2 JP55009714A JP971480A JPS6332726B2 JP S6332726 B2 JPS6332726 B2 JP S6332726B2 JP 55009714 A JP55009714 A JP 55009714A JP 971480 A JP971480 A JP 971480A JP S6332726 B2 JPS6332726 B2 JP S6332726B2
- Authority
- JP
- Japan
- Prior art keywords
- caustic soda
- heat exchange
- soda solution
- vapor
- evaporator
- 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.)
- Expired
Links
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 156
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 52
- 239000000243 solution Substances 0.000 claims description 50
- 239000012267 brine Substances 0.000 claims description 21
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 21
- 238000005868 electrolysis reaction Methods 0.000 claims description 12
- 239000003014 ion exchange membrane Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000007788 liquid Substances 0.000 description 12
- 239000000463 material Substances 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明はイオン交換膜法電解により得られる苛
性ソーダ溶液を効率よくかつ低コストにて濃縮す
ることを可能ならしめる苛性ソーダの濃縮法に関
する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for concentrating caustic soda that makes it possible to efficiently and at low cost concentrate a caustic soda solution obtained by ion exchange membrane electrolysis.
［従来の技術］
イオン交換膜法電解は、イオン交換膜を挾んで
陰極と陽極を配置した電解槽で、塩化アルカリ水
溶液（ブライン）を電解することにより陰極室側
で苛性ソーダ溶液を製造する。[Prior Art] Ion-exchange membrane electrolysis produces a caustic soda solution on the cathode chamber side by electrolyzing an aqueous alkali chloride solution (brine) in an electrolytic cell in which a cathode and an anode are arranged with an ion-exchange membrane sandwiched between them.
イオン交換膜電解により製造される苛性ソーダ
溶液は、直接実用濃度45〜50％の濃厚なものは得
られないが、食塩含有量が0.1％以下できわめて
低いのが特徴である。このイオン交換膜電解で得
られた苛性ソーダ溶液を濃縮する場合、熱源とし
て電解槽における電解による余剰熱を利用して省
エネルギーを計るのが合理的である。従来の苛性
ソーダ濃縮装置は第１図に示すように、熱源とし
て電解槽陽極室側の80〜120℃のブライン１０２
を利用し、電解槽陰極室側からの苛性ソーダ溶液
１０１と液―液熱交換を行わせる方法をとつてい
る。すなわち、イオン交換膜電解で得られた苛性
ソーダ溶液１０１を多段直列（図では４段直列）
の最終段の熱交換器に供給し、第３段の熱交換
から送られてきたブライン１０２と熱交換した
のち、蒸発缶Ｂに入り、そこでフラツシユして気
液分離し、発生した蒸気はこれを引き出してコン
デンサー１０３に送つて凝縮水とし、一方濃縮さ
れた苛性ソーダ溶液は第３段の熱交換器に入
り、そこで第２段の熱交換器からのブライン１
０２と同じく熱交換したのち、蒸発缶Ｂに入り、
そこでフラツシユしてさらに濃縮度を高め、以下
同様の熱交換とフラツシユとを繰返し、蒸発缶Ａ
より濃縮苛性ソーダ溶液１０１ａとして取り出さ
れる。 Although the caustic soda solution produced by ion-exchange membrane electrolysis cannot be directly obtained in a concentrated solution with a practical concentration of 45-50%, it is characterized by an extremely low salt content of 0.1% or less. When concentrating the caustic soda solution obtained by this ion-exchange membrane electrolysis, it is reasonable to save energy by using surplus heat from electrolysis in the electrolytic cell as a heat source. As shown in Figure 1, a conventional caustic soda concentrator uses a brine 102 at 80 to 120°C on the anode chamber side of the electrolytic cell as a heat source.
A method is used to perform liquid-liquid heat exchange with the caustic soda solution 101 from the cathode chamber side of the electrolytic cell. That is, the caustic soda solution 101 obtained by ion-exchange membrane electrolysis is placed in series in multiple stages (four stages in series in the figure).
After exchanging heat with the brine 102 sent from the third stage heat exchanger, it enters the evaporator B where it is flashed and separated into gas and liquid, and the generated steam is is drawn off and sent to condenser 103 as condensate water, while the concentrated caustic soda solution enters the third stage heat exchanger where it is combined with brine 1 from the second stage heat exchanger.
After exchanging heat as in 02, it enters evaporator B.
Then, the concentration level is further increased by flashing, and the same heat exchange and flashing are repeated, and the evaporator A
A more concentrated caustic soda solution 101a is taken out.
［発明が解決しようとする問題点］
しかしながら、上記熱交換は液―液熱交換であ
るので、伝熱係数が小さく設備が大型となるのは
もちろんであり、NaOHやブラインに対して耐
蝕性を有する材質が必要となり、工作上において
もまたコスト的にも高価なものとなるという欠点
がある。[Problems to be Solved by the Invention] However, since the above heat exchange is a liquid-liquid heat exchange, the heat transfer coefficient is small and the equipment becomes large. The disadvantage is that the material is expensive in terms of workmanship and cost.
本発明者らは上記の従来方法の欠点を解決し、
イオン交換膜法電解により得られる苛性ソーダ溶
液を効率よくかつ低コストにて濃縮することを可
能ならしめる苛性ソーダ溶液の濃縮法を提供する
ことを目的とする。 The present inventors solved the drawbacks of the above conventional methods,
An object of the present invention is to provide a method for concentrating a caustic soda solution, which makes it possible to efficiently concentrate a caustic soda solution obtained by ion-exchange membrane electrolysis at low cost.
（問題点を解決するための手段）
本発明は、上記の目的を達成するためにイオン
交換膜法電解によつて得られる苛性ソーダ溶液の
濃縮法において、上部に熱交換部、下部にフラツ
シユ部を一体に連結した濃縮用蒸発缶を多段に直
列に接続し、他方電解槽の陽極室側からのブライ
ンを減圧下でフラツシユさせ、その発生ベーパー
を上記蒸発缶の各熱交換部に導入するとともに電
解槽の陰極室側からの苛性ソーダ溶液を最終段の
蒸発缶の熱交換部に供給して上記ベーパーと間接
熱交換させて加熱したのち、その苛性ソーダ溶液
をフラツシユ部でフラツシユさせて蒸気と濃縮さ
れた苛性ソーダ溶液とに分離し、分離した蒸気を
抜き出すと共に濃縮された苛性ソーダ溶液を順次
前段の蒸発缶の熱交換部に移送し、そこで間接熱
交換させると共にフラツシユさせ、以後各段の蒸
発缶で加熱とフラツシユを繰り返して第１段の蒸
発缶のフラツシユ部より苛性ソーダの濃縮液を取
り出すようにしたものである。(Means for Solving the Problems) In order to achieve the above object, the present invention provides a method for concentrating a caustic soda solution obtained by ion-exchange membrane electrolysis, in which a heat exchange part is provided in the upper part and a flash part is provided in the lower part. The concentrating evaporators connected together are connected in series in multiple stages, and the brine from the anode chamber side of the electrolyzer is flashed under reduced pressure, and the generated vapor is introduced into each heat exchange section of the evaporator and electrolyzed. The caustic soda solution from the cathode chamber side of the tank is supplied to the heat exchange section of the final stage evaporator and heated by indirect heat exchange with the vapor, and then the caustic soda solution is flashed in the flash section and concentrated into steam. It is separated into a caustic soda solution, the separated vapor is extracted, and the concentrated caustic soda solution is sequentially transferred to the heat exchange section of the evaporator in the previous stage, where it is subjected to indirect heat exchange and flashed, and then heated and heated in each evaporator. The concentrated solution of caustic soda is taken out from the flash section of the first stage evaporator by repeating flashing.
（作用）
本発明においては、苛性ソーダ溶液より沸点上
昇が極めて低い陽極室側のブラインをフラツシユ
してベーパーとすることでより高い温度のベーパ
ーを取り出すことができ、これを苛性ソーダ溶液
の熱源として用いることで有効な熱回収が行え、
しかも蒸発缶の熱交換部ではベーパーと苛性ソー
ダ溶液とを伝熱管などを介して間接熱交換させ、
そのベーパーの潜熱により苛性ソーダ溶液を加熱
することで熱交換が良好となり装置が小型できる
と共に装置材料は、苛性ソーダ溶液に対して耐蝕
性を有する材質を選べばよいため、そのコストが
安くなる。(Function) In the present invention, by flashing the brine on the anode chamber side, whose boiling point rise is extremely lower than that of the caustic soda solution, and turning it into vapor, the vapor at a higher temperature can be taken out, and this can be used as a heat source for the caustic soda solution. can perform effective heat recovery,
Moreover, in the heat exchange section of the evaporator, vapor and caustic soda solution are indirectly heat exchanged via heat transfer tubes, etc.
By heating the caustic soda solution using the latent heat of the vapor, heat exchange is good, and the device can be made smaller. At the same time, the device material can be selected from materials that are resistant to corrosion against the caustic soda solution, which reduces the cost.
（実施例）
次に本発明の好適実施例を添付図面によつて説
明する。(Embodiments) Next, preferred embodiments of the present invention will be described with reference to the accompanying drawings.
第２図において、１は電解槽で、イオン交換膜
により陽極室側１ｂと陰極室側１ａとに区画さ
れ、各室１ａ，１ｂには図示していないが電極が
設けられており、ブライン中の塩化ナトリウムの
電気分解により陰極室側１ａで苛性ソーダが製造
される。 In Fig. 2, 1 is an electrolytic cell, which is divided into an anode chamber side 1b and a cathode chamber side 1a by an ion exchange membrane.Each chamber 1a, 1b is equipped with an electrode (not shown), and is in brine. Caustic soda is produced in the cathode chamber side 1a by electrolysis of sodium chloride.
この苛性ソーダを濃縮装置は多段な蒸発缶V1，
V2，V3からなつている。各蒸発缶V1，V2，V3
は、上部にシエルアンドキユーブ式の熱交換部
E1，E2，E3と、その下部に一体に設けられたフ
ラツシユ部F1，F2，F3とからなつている。 The device for concentrating this caustic soda is a multi-stage evaporator V 1 ,
It consists of V 2 and V 3 . Each evaporator V 1 , V 2 , V 3
Has a shell-and-cube heat exchanger on the top.
It consists of E 1 , E 2 , E 3 and flash portions F 1 , F 2 , F 3 integrally provided below them.
先ず電解槽１の陽極室１ｂからのブライン３が
フラツシユー４に導入され、そこで減圧下でフラ
ツシユされてベーパー５を発生させる。このベー
パー５は、各蒸発缶V1，V2，V3のそれぞれの熱
交換部E1，E2，E3に導入される。またフラツシ
ヤー４でフラツシユ後のブライン３ａは電解槽１
に戻される。 First, brine 3 from the anode chamber 1b of the electrolytic cell 1 is introduced into a flash 4, where it is flashed under reduced pressure to generate vapor 5. This vapor 5 is introduced into the respective heat exchange parts E 1 , E 2 , E 3 of the evaporators V 1 , V 2 , V 3 . Furthermore, the brine 3a after being flashed by the flasher 4 is in the electrolytic tank 1.
will be returned to.
一方、電解槽１の陰極側１ａで製造された苛性
ソーダ溶液２は、最終段、すなわち第３段の蒸発
缶V3の熱交換部E3に供給され、そこでフラツシ
ヤー４より導入されたベーパー５との間接熱交換
により、加熱され、ついでフラツシユ部F3でフ
ラツシユすることで、蒸気と濃縮された苛性ソー
ダ溶液とに気液分離される。蒸気６は蒸発缶V3
から抜きだされ、コンデンサ７で凝縮され凝縮水
となる。一方濃縮された苛性ソーダ溶液は、適宜
その蒸発缶３を循環されると共に第２段の蒸発缶
V2の熱交換部E2にされ、搬送され、そこで同じ
くフラツシヤー４より導入されたベーパー５との
間接熱交換により加熱され、下方のフラツシユ部
F2でフラツシユして気液分離され、蒸気６と濃
縮された苛性ソーダ溶液となり、蒸気６が抜き出
されると共に濃縮された苛性ソーダ溶液が第１段
の蒸発缶V1の熱交換部E1に導入され、上述のよ
うに加熱されると共にフラツシユ部F1でフラツ
シユされて気液分離され、そのフラツシユ部F1
より濃縮苛性ソーダ溶液２ａが取り出される。 On the other hand, the caustic soda solution 2 produced on the cathode side 1a of the electrolytic cell 1 is supplied to the heat exchange section E3 of the final stage, that is, the third stage evaporator V3 , where it is mixed with the vapor 5 introduced from the flasher 4. It is heated by indirect heat exchange, and then flashed in the flashing section F3 to separate gas and liquid into steam and concentrated caustic soda solution. Steam 6 is evaporator V 3
It is extracted from the water and condensed in the condenser 7 to become condensed water. On the other hand, the concentrated caustic soda solution is appropriately circulated through the evaporator 3 and sent to the second stage evaporator.
It is transported to the heat exchange section E 2 of V 2 , where it is heated by indirect heat exchange with the vapor 5 also introduced from the flasher 4, and is transferred to the lower flash section.
It is flashed with F2 and separated into gas and liquid to become steam 6 and a concentrated caustic soda solution.The steam 6 is extracted and the concentrated caustic soda solution is introduced into the heat exchange section E1 of the first stage evaporator V1 . is heated as described above and flashed in the flashing section F1 to separate gas and liquid, and the flashing section F1
A more concentrated caustic soda solution 2a is taken out.
このようにブラインをフラツシヤー４でフラツ
シユさせ、そこで発生したベーパー５を苛性ソー
ダ溶液２の加熱熱源として用いることで有効な熱
回収が行える。特にブラインの沸点上昇は、苛性
ソーダ溶液の沸点上昇より極めて少なく、例えば
大気圧下でのブラインの沸点上昇は＋３℃である
のに対し、苛性ソーダ溶液では＋20℃であり、従
つてフラツシヤー４から発生するベーパー５は、
減圧度が少なく、しかも温度降下の少ない高い熱
量のベーパー５が得られる。またベーパー５は、
上述のようにブラインの沸点上昇が極めて小さい
ため、塩化物を含まない水蒸気となり、蒸発缶
V1，V2，V3の熱交換部E1，E2，E3は、ベーパー
５側の腐食を考慮せずに苛性ソーダ溶液に対する
腐食のみを考慮した材料を選べばよい。従つて、
熱交換部V1，V2，V3をシエルアンドチユーブで
構成する場合、シエル側は鋼材とし苛性ソーダ溶
液の通るチユーブ側はNi材などを用いればよく、
そのコストを低減できる。 Effective heat recovery can be achieved by flashing the brine in the flasher 4 and using the vapor 5 generated there as a heat source for heating the caustic soda solution 2. In particular, the boiling point increase of brine is much smaller than that of caustic soda solution; for example, the boiling point increase of brine under atmospheric pressure is +3°C, whereas that of caustic soda solution is +20°C, so that the boiling point increase generated from flasher 4 Vapor 5 is
Vapor 5 having a high calorific value with a small degree of pressure reduction and a small temperature drop can be obtained. Also, Vapor 5 is
As mentioned above, the increase in the boiling point of brine is extremely small, so it becomes water vapor that does not contain chlorides, and the boiling point rises in the brine.
For the heat exchange parts E 1 , E 2 , and E 3 of V 1 , V 2 , and V 3 , materials may be selected taking into consideration only corrosion against the caustic soda solution without considering corrosion on the vapor 5 side. Therefore,
When the heat exchange parts V 1 , V 2 , and V 3 are configured with shell and tubes, the shell side may be made of steel, and the tube side through which the caustic soda solution passes may be made of Ni material, etc.
The cost can be reduced.
さらにベーパー５と苛性ソーダ溶液とが間接熱
交換するにおいてベーパー５はチユーブ外面で凝
縮し、水膜をつくつて流下するが、この水膜は充
分薄いため全体が液の場合の伝熱係数より充分高
い伝熱係数となるため、その熱交換率もきわめて
高く装置を小形化できる。 Furthermore, when the vapor 5 and the caustic soda solution exchange indirect heat, the vapor 5 condenses on the outer surface of the tube and flows down forming a water film, but this water film is sufficiently thin that the heat transfer coefficient is sufficiently higher than that of the case where the entire liquid is a liquid. Since it has a heat transfer coefficient, its heat exchange rate is also extremely high and the device can be made smaller.
尚上述の実施例においては蒸発缶３段の例で説
明したが段数はこれに限定されるものではない。 In the above-mentioned embodiment, an example of three stages of evaporators has been described, but the number of stages is not limited to this.
［発明の効果］
以上説明したきたことから明らかなように本発
明によれば次のごとき優れた効果を発揮する。[Effects of the Invention] As is clear from the above explanation, the present invention exhibits the following excellent effects.
(1) 省エネルギーに寄与する。(1) Contributes to energy conservation.
(2) 装置が小型化され、コストダウンを可能とす
る。(2) The device becomes smaller and costs can be reduced.
(3) 蒸発缶の熱交換部における苛性ソーダ溶液濃
縮のための熱交換はブラインのフラツシユベー
パーを加熱源とする気―液熱交換であるので、
ベーパー側の材料は高級材料を使う必要はな
く、カーボンスチールで充分耐蝕性があり、か
つ熱交換の効果はきわめて大である。(3) The heat exchange for concentrating the caustic soda solution in the heat exchange section of the evaporator is a gas-liquid heat exchange using brine flash vapor as the heating source.
The material on the vapor side does not need to be a high-grade material; carbon steel is sufficiently resistant to corrosion, and the heat exchange effect is extremely large.
本発明は以上のごとく、イオン交換膜法電解に
より得られる苛性ソーダ溶液を効率よくかつ低コ
ストにて濃縮することを可能ならしめる苛性ソー
ダ溶液の濃縮法を提供するもので、その工業的価
値はきわめて大きい。 As described above, the present invention provides a method for concentrating a caustic soda solution that makes it possible to efficiently and at low cost concentrate a caustic soda solution obtained by ion-exchange membrane electrolysis, and its industrial value is extremely large. .
第１図は従来のイオン交換膜法電解で得られる
苛性ソーダ溶液の加熱源としてブラインを使用す
る液―液熱交換による濃縮方法の一例のフローシ
ート、第２図は本発明のブラインのフラツシユベ
ーパーを加熱源として使用する気―液熱交換によ
る苛性ソーダ溶液の濃縮方法を実施する装置の一
実施例のフローシートである。
図中、１は電解槽、１ａは陰極室側、１ｂは陽
極室側、２は苛性ソーダ溶液（未濃縮）、２は濃
縮苛性ソーダ溶液、３はブライン、３ａはブライ
ン（フラツシユ後）、４はフラツシヤー、５はブ
ラインのフラツシユーベーパー、６は蒸気、７は
コンデンサー、V1，V2，V3は濃縮用蒸発缶、
E1，E2，E3は熱交換部、F1，F2，F3はフラツシ
ユ部である。
Figure 1 is a flow sheet of an example of a concentration method by liquid-liquid heat exchange using brine as a heating source for a caustic soda solution obtained by conventional ion-exchange membrane electrolysis, and Figure 2 is a flow sheet of a brine flash vapor of the present invention. 1 is a flow sheet of an example of an apparatus for carrying out a method for concentrating a caustic soda solution by gas-liquid heat exchange using a gas-liquid heat exchanger as a heating source. In the figure, 1 is the electrolytic cell, 1a is the cathode chamber side, 1b is the anode chamber side, 2 is the caustic soda solution (unconcentrated), 2 is the concentrated caustic soda solution, 3 is the brine, 3a is the brine (after flashing), 4 is the flasher , 5 is a brine flash vapor, 6 is steam, 7 is a condenser, V 1 , V 2 , V 3 are evaporators for concentration,
E 1 , E 2 , and E 3 are heat exchange parts, and F 1 , F 2 , and F 3 are flash parts.
Claims (1)
ーダ溶液の濃縮法において、上部に熱交換部、下
部にフラツシユ部を一体に連結した濃縮用蒸発缶
を多段に直列に接続し、他方電解槽の陽極室側か
らのブラインを減圧下でフラツシユさせ、その発
生ベーパーを上記蒸発缶の各熱交換部に導入する
とともに電解槽の陰極室側からの苛性ソーダ溶液
を最終段の蒸発缶の熱交換部に供給して上記ベー
パーと間接熱交換させて加熱したのち、その苛性
ソーダ溶液をフラツシユ部でフラツシユさせて蒸
気と濃縮された苛性ソーダ溶液とに分離し、分離
した蒸気を抜き出すと共に濃縮された苛性ソーダ
溶液を順次前段の蒸発缶の熱交換部に移送し、そ
こで間接熱交換させると共にフラツシユさせ、以
後各段の蒸発缶で加熱とフラツシユを繰り返して
第１段の蒸発缶のフラツシユ部より苛性ソーダの
濃縮液を取り出すことを特徴とする苛性ソーダ溶
液の濃縮法。1. In a method for concentrating a caustic soda solution obtained by ion-exchange membrane electrolysis, concentrating evaporators each having a heat exchange section in the upper part and a flash section in the lower part integrally connected are connected in series in multiple stages, and the anode of the electrolytic cell is connected in series in multiple stages. The brine from the chamber side is flashed under reduced pressure, and the generated vapor is introduced into each heat exchange section of the evaporator, and the caustic soda solution from the cathode chamber side of the electrolyzer is supplied to the heat exchange section of the final stage evaporator. After heating by indirect heat exchange with the vapor, the caustic soda solution is flashed in a flashing section and separated into vapor and concentrated caustic soda solution.The separated vapor is extracted and the concentrated caustic soda solution is sequentially transferred to the previous stage. The concentrated solution of caustic soda is transferred to the heat exchange section of the first evaporator, where it is subjected to indirect heat exchange and flashed, and then heating and flashing are repeated in each stage of the evaporator to take out the concentrated solution of caustic soda from the flash section of the first stage evaporator. A method for concentrating caustic soda solution characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP971480A JPS56109817A (en) | 1980-01-30 | 1980-01-30 | Concentrating method for caustic soda solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP971480A JPS56109817A (en) | 1980-01-30 | 1980-01-30 | Concentrating method for caustic soda solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56109817A JPS56109817A (en) | 1981-08-31 |
| JPS6332726B2 true JPS6332726B2 (en) | 1988-07-01 |
Family
ID=11727924
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP971480A Granted JPS56109817A (en) | 1980-01-30 | 1980-01-30 | Concentrating method for caustic soda solution |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56109817A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103628085A (en) * | 2013-11-22 | 2014-03-12 | 新汶矿业集团有限责任公司泰山盐化工分公司 | Method for cyclic utilization of water resources in chlor-alkali production |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8317994B2 (en) | 2008-08-07 | 2012-11-27 | Westlake Vinyl Corporation | Method of concentrating an aqueous caustic alkali using a catholyte heat recovery evaporator |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53113299A (en) * | 1977-03-15 | 1978-10-03 | Asahi Glass Co Ltd | Method of concentrating caustic alkaline sulution for ion exchange membrane electrolysis |
| JPS5428297A (en) * | 1977-08-04 | 1979-03-02 | Ebara Corp | Effective heat utilization method in caustic soda producing plant by ion exchange or electrolytic method |
-
1980
- 1980-01-30 JP JP971480A patent/JPS56109817A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53113299A (en) * | 1977-03-15 | 1978-10-03 | Asahi Glass Co Ltd | Method of concentrating caustic alkaline sulution for ion exchange membrane electrolysis |
| JPS5428297A (en) * | 1977-08-04 | 1979-03-02 | Ebara Corp | Effective heat utilization method in caustic soda producing plant by ion exchange or electrolytic method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103628085A (en) * | 2013-11-22 | 2014-03-12 | 新汶矿业集团有限责任公司泰山盐化工分公司 | Method for cyclic utilization of water resources in chlor-alkali production |
| CN103628085B (en) * | 2013-11-22 | 2016-10-05 | 新汶矿业集团有限责任公司泰山盐化工分公司 | Water resource circulation utilization method in chlor-alkali production |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56109817A (en) | 1981-08-31 |
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