CN105951119A - Method for preparing sodium hydroxide - Google Patents
Method for preparing sodium hydroxide Download PDFInfo
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- CN105951119A CN105951119A CN201610515916.XA CN201610515916A CN105951119A CN 105951119 A CN105951119 A CN 105951119A CN 201610515916 A CN201610515916 A CN 201610515916A CN 105951119 A CN105951119 A CN 105951119A
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/02—Process control or regulation
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a method for preparing sodium hydroxide. The method comprises the steps that S1, a refined saturated sodium chloride solution is added into a preheater to be preheated, wherein the preheating temperature is 47 to 63 DEG C; S2, the preheated saturated sodium chloride solution is transferred into an anode chamber of an electrolytic bath, the power is turned on for energization, when the current of a circuit reaches 5.3 KA, acid is added into the anode chamber, and the pH value of a cathode chamber is maintained at 2 to 3; S3, the temperature of the electrolytic bath is increased to 62 to 73 DEG C, and heat preservation energization reaction is carried out; S4, air exhaust treatment is carried out on the anode chamber and the cathode chamber, and pressure of the anode chamber and the cathode chamber is maintained at 47.35*10<3> Pa to 53.41*10<3> Pa; and S5, a part of a sodium hydroxide solution obtained from the side surface of the cathode chamber flows back to the cathode chamber, hydrogen is generated above an electrode of the cathode chamber, and chlorine is generated above an electrode of the anode chamber. According to the saturated sodium chlorate electrolysis manner, gases adhering to the surfaces of the electrodes are reduced, the conductive ability of an entire electrolytic system is improved, and the yield of sodium hydroxide is greatly improved.
Description
Technical field
The present invention relates to the preparation of industrial chemicals, particularly to a kind of method preparing sodium hydroxide.
Background technology
Sodium hydroxide, chemical formula is NaOH, it is commonly called as Caustic soda, Caustic soda, caustic soda, for a kind of highly basic with severe corrosive, generally lamellar or particle shape, (heat release when being dissolved in water) soluble in water also forms alkaline solution, separately has hygroscopy, easily draw the steam (deliquescence) in air and carbon dioxide (going bad), hydrochloric acid can be added and check whether to go bad.
In prior art, the mode of production of industrial sodium hydroxide is mainly to be electrolysed saturated aqueous common salt, and it mainly uses in formerly modern chlorine industry.
But meanwhile, due to being electrolysed saturated table salt water when, the hydroxide ion that cathode chamber produces can little by little gather on the cation exchange membrane of cathode chamber side, along with hydroxyl concentration in this place constantly increases, thus be possible to cross cation exchange membrane, thus will result in the problems such as anode chamber's chlorine yield falls sharply.
Summary of the invention
It is an object of the invention to provide a kind of method preparing sodium hydroxide being favorably improved naoh concentration.
The above-mentioned purpose of the present invention has the technical scheme that a kind of method preparing sodium hydroxide, comprises the following steps,
S1, being joined in preheater by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；
S2, transferring in electrolyzer anode chamber by the saturated nacl aqueous solution after preheating, cathode chamber is then passed through distilled water, and turns on the power energising, when the electric current of circuit reaches 5.3KA, adds acid in anode chamber, and to keep the pH value of cathode chamber be 2～3；
S3, the temperature of electrolysis bath is increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction；
S4, process that cathode chamber and anode chamber are bled, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；
S5, cathode chamber side is produced the sodium hydroxide solution that obtains it is partly refluxed in cathode chamber, output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber.
By said method, first it is that refined saturated sodium-chloride is preheated, so so that saturated sodium-chloride can be quickly carried out electrolysis after entering into electrolysis bath, improves the efficiency of electrolysis.
Secondly, by the way of acid adding in the anode compartment, improve the pH value of solution, the hydroxyl low amounts that so can be effectively prevented cathode chamber generation passes through cation exchange membrane, and causes the absorption of chlorine in anode chamber, thus not only reduces the productivity of chlorine, meanwhile, it is also introduced into new material.
Owing to the water saturation vapour pressure in the case of 70 DEG C is 31.18 × 103Pa, is adjusted to 47.35 × 10 by the pressure of electrolysis bath3Pa～53.41 × 103Pa, so can be effectively improved hydrogen and efficiency that chlorine spins off from solution, thus be conducive to improving hydrogen and the normal output of chlorine, and chlorine back dissolving can also be reduced to the amount in saturated nacl aqueous solution, and it is also beneficial to improve the amount of sodium hydroxide output.
By by the sodium hydroxide partial reflux of output to cathode chamber, so can be effectively improved the concentration of sodium hydroxide, the size of concentration can be controlled by capacity of returns, and when increasing the naoh concentration of cathode chamber, also improve the conductive capability of whole electrolysis bath, thus be conducive to improving the generation amount of sodium hydroxide.
As preferably, the hydrogen portion of S5 output is passed in cathode chamber along the surface of cation exchange membrane.
As preferably, it is produce hydrogen total amount 30%～40% by the amount of the hydrogen in cathode chamber.
So it is passed in cathode chamber by the surface along cation exchange membrane of hydrogen, effectively the solution of other parts in the solution on cation exchange membrane surface and cathode chamber can be caused turbulent flow, thus advantageously reduce the hydroxyl surface aggregation at cation exchange membrane, and then the most just can further reduce the hydroxyl probability through cation exchange membrane.
As preferably, opening stirring paddle in the cathodic compartment and be stirred in S3, the rotating speed of stirring paddle is 60～70 turns/min.
Owing to can be attached on negative electrode with the form of bubble after hydrionic generation, thus one layer of air film will be produced on the surface of negative electrode, thus can reduce the area that negative electrode contacts with the aqueous slkali of solution, thus result in the decline of aqueous slkali electric conduction quantity, and then be unfavorable for the generation of sodium hydroxide.By the way of stirring, can effectively improve the amount of flow of sodium hydroxide in cathode chamber, be attached on negative electrode such that it is able to eliminate hydrogen, improve the efficiency that hydrogen produces.
And the rotating speed of 60～70 turns/min can ensure that the flow velocity of the sodium hydroxide solution in cathode chamber is unlikely to excessive, thus cation exchange membrane is impacted.
As preferably, the capacity of returns of sodium hydroxide solution is the 1/5～3/5 of its Gross Output amount.
As preferably, opening stirring paddle in the anode compartment and be stirred in S3, the rotating speed of stirring paddle is 40～45 turns/min.
Saturated nacl aqueous solution in anode chamber is stirred, mainly it is attached on anode also for minimizing chlorine, and while 40～45 turns/min rotating speed ensure that chlorine bubbles normally departs from anode, it is also possible to avoid chlorine bubbles self to rupture and be again dissolved in saturated nacl aqueous solution.
As preferably, the acid added in S2 is hydrochloric acid.
Hydrochloric acid is possible not only to be effectively improved the hydrionic concentration of anode chamber, and meanwhile, new ion concentration also will not be introduced by it, and other impurity so can be avoided the purity of chlorine and the impact of the conductive capability of saturated nacl aqueous solution.
In sum, the method have the advantages that
1., by reducing the pressure in electrolysis bath, the concentration of superjacent hydrogen and chlorine can be efficiently reduced, thus beneficially hydrogen and the output of chlorine, and then also it is advantageous for improving the yield of sodium hydroxide；
2. by the way of stirring, eliminate the attachment on electrode of hydrogen and chlorine, thus substantially increase the electric conductivity of whole electrolysis bath, and then be conducive to improving the yield of sodium hydroxide.
3. can not only control the pH value of solution in anode chamber by addition hydrochloric acid, also will not introduce new impurity element simultaneously.
Detailed description of the invention
Embodiment 1,
By refined saturated nacl aqueous solution with flow as 200m3/ h joins in preheater and preheats, and preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 1/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 30% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/h, mass concentration is 34%, and the productivity of sodium hydroxide is 97.5%.
Embodiment 2,
Being joined in preheater with flow for 200m3/h by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 3/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 40% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/h, mass concentration is 41%, and the productivity of sodium hydroxide is 98.6%.
Embodiment 3,
Being joined in preheater with flow for 200m3/h by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 2/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 35% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/h, mass concentration is 36%, and the productivity of sodium hydroxide is 97.9%.
Embodiment 4,
Being joined in preheater with flow for 200m3/h by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, with 300 m3The flow of/h joins in electric tank cathode room, and turns on the power energising, when the electric current of circuit reaches 5.3KA, adds hydrochloric acid in anode chamber, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 1/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 35% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/ h, mass concentration is 35%, and the productivity of sodium hydroxide is 97.8%.
Embodiment 5,
By refined saturated nacl aqueous solution with flow as 200m3/ h joins in preheater and preheats, and preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 1/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 40% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/ h, mass concentration is 35.5%, and the productivity of sodium hydroxide is 98.1%.
Embodiment 6,
By refined saturated nacl aqueous solution with flow as 200m3/ h joins in preheater and preheats, and preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 2/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 40% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/h, mass concentration is 37%, and the productivity of sodium hydroxide is 98.0%.
Embodiment 7,
Being joined in preheater with flow for 200m3/h by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；Saturated nacl aqueous solution after preheating is transferred in electrolyzer anode chamber, join in electric tank cathode room with the flow of 300 m3/h, and turn on the power energising, when the electric current of circuit reaches 5.3KA, in anode chamber, add hydrochloric acid, and to keep the pH value of cathode chamber be 2～3；The temperature of electrolysis bath being increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction, meanwhile, the speed of agitator of cathode chamber is 60～70 turns/min, and the speed of agitator of anode chamber is 40～45 turns/min；Cathode chamber and anode chamber are bled process, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；Output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber, collect in hydrogen gas tank and chlorine pot respectively, cathode chamber side is produced the 3/5 of the sodium hydroxide solution obtained and is back in cathode chamber, be back to the 30% of the hydrogen total amount produced above cathode chamber in cathode chamber.Finally produce the amount of sodium hydroxide is 100m3/ h, mass concentration is 40%, and the productivity of sodium hydroxide is 98.4.
This specific embodiment is only explanation of the invention; it is not limitation of the present invention; the present embodiment can be made after reading this specification by those skilled in the art as required does not has the amendment of creative contribution, but as long as all being protected by Patent Law in scope of the presently claimed invention.
Claims (7)
1. the method preparing sodium hydroxide, comprises the following steps,
S1, being joined in preheater by refined saturated nacl aqueous solution and preheat, preheating temperature is 47 DEG C～63 DEG C；
S2, transferring in electrolyzer anode chamber by the saturated nacl aqueous solution after preheating, cathode chamber is then passed through distilled water, and turns on the power energising, when the electric current of circuit reaches 5.3KA, adds acid in anode chamber, and to keep the pH value of cathode chamber be 2～3；
S3, the temperature of electrolysis bath is increased to 62 DEG C～73 DEG C, and carries out insulation energising reaction；
S4, process that cathode chamber and anode chamber are bled, and to keep the pressure of cathode chamber and anode chamber be 47.35 × 103Pa～53.41 × 103Pa；
S5, cathode chamber side is produced the sodium hydroxide solution that obtains it is partly refluxed in cathode chamber, output hydrogen above the electrode of cathode chamber, output chlorine above the electrode of anode chamber.
A kind of method preparing sodium hydroxide the most according to claim 1, it is characterised in that: the hydrogen portion of S5 output is passed in cathode chamber along the surface of cation exchange membrane.
A kind of method preparing sodium hydroxide the most according to claim 2, it is characterised in that: by the amount of the hydrogen in cathode chamber be produce hydrogen total amount 30%～40%.
A kind of method preparing sodium hydroxide the most according to claim 3, it is characterised in that: opening stirring paddle in S3 in the cathodic compartment and be stirred, the rotating speed of stirring paddle is 60～70 turns/min.
A kind of method preparing sodium hydroxide the most according to claim 1, it is characterised in that: the capacity of returns of sodium hydroxide solution is the 1/5～3/5 of its Gross Output amount.
A kind of method preparing sodium hydroxide the most according to claim 1, it is characterised in that: opening stirring paddle in S3 in the anode compartment and be stirred, the rotating speed of stirring paddle is 40～45 turns/min.
A kind of method preparing sodium hydroxide the most according to claim 1, it is characterised in that: the acid added in S2 is hydrochloric acid.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109208024A (en) * | 2018-09-21 | 2019-01-15 | 宁波镇洋化工发展有限公司 | A kind of chlor-alkali production technique |
| CN110923077A (en) * | 2019-11-21 | 2020-03-27 | 甘肃农业职业技术学院 | Preparation method of pine phytoncide process soap |
| CN112125978A (en) * | 2020-09-16 | 2020-12-25 | 陕西国防工业职业技术学院 | Preparation method of high-viscosity water-soluble cellulose ether |
| CN115198108A (en) * | 2021-04-13 | 2022-10-18 | 浙江新化化工股份有限公司 | Method for extracting lithium |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0445295A (en) * | 1990-06-12 | 1992-02-14 | Toagosei Chem Ind Co Ltd | Method for removing chlorate in brine |
| JPH1161476A (en) * | 1997-08-22 | 1999-03-05 | Chlorine Eng Corp Ltd | Starting operation of electrolytic bath in ion-exchange membrane electrolytic process |
| CN103305864A (en) * | 2012-03-15 | 2013-09-18 | 拜耳知识产权有限责任公司 | Method for the electrolysis of alkali chlorides with oxygen consumption electrodes in a micro-gap arrangement |
| CN204097575U (en) * | 2013-11-20 | 2015-01-14 | 新疆宜化化工有限公司 | Electrolysis cells in ionic exchange membrane caustic |
| CN104532283A (en) * | 2014-12-17 | 2015-04-22 | 济宁金威煤电有限公司 | Method and device for producing caustic soda through electrolysis by replacing part of fine brine with light salt brine |
| CN105154910A (en) * | 2015-09-21 | 2015-12-16 | 宁波镇洋化工发展有限公司 | Process for producing alkali |
-
2016
- 2016-07-04 CN CN201610515916.XA patent/CN105951119B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0445295A (en) * | 1990-06-12 | 1992-02-14 | Toagosei Chem Ind Co Ltd | Method for removing chlorate in brine |
| JPH1161476A (en) * | 1997-08-22 | 1999-03-05 | Chlorine Eng Corp Ltd | Starting operation of electrolytic bath in ion-exchange membrane electrolytic process |
| CN103305864A (en) * | 2012-03-15 | 2013-09-18 | 拜耳知识产权有限责任公司 | Method for the electrolysis of alkali chlorides with oxygen consumption electrodes in a micro-gap arrangement |
| CN204097575U (en) * | 2013-11-20 | 2015-01-14 | 新疆宜化化工有限公司 | Electrolysis cells in ionic exchange membrane caustic |
| CN104532283A (en) * | 2014-12-17 | 2015-04-22 | 济宁金威煤电有限公司 | Method and device for producing caustic soda through electrolysis by replacing part of fine brine with light salt brine |
| CN105154910A (en) * | 2015-09-21 | 2015-12-16 | 宁波镇洋化工发展有限公司 | Process for producing alkali |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109208024A (en) * | 2018-09-21 | 2019-01-15 | 宁波镇洋化工发展有限公司 | A kind of chlor-alkali production technique |
| CN109208024B (en) * | 2018-09-21 | 2020-02-28 | 宁波镇洋化工发展有限公司 | Chlor-alkali production process |
| CN110923077A (en) * | 2019-11-21 | 2020-03-27 | 甘肃农业职业技术学院 | Preparation method of pine phytoncide process soap |
| CN112125978A (en) * | 2020-09-16 | 2020-12-25 | 陕西国防工业职业技术学院 | Preparation method of high-viscosity water-soluble cellulose ether |
| CN115198108A (en) * | 2021-04-13 | 2022-10-18 | 浙江新化化工股份有限公司 | Method for extracting lithium |
| CN115198108B (en) * | 2021-04-13 | 2024-03-29 | 浙江新化化工股份有限公司 | Method for extracting lithium |
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Address after: 315204 No. 655 Haitian Road, Ningbo Petrochemical Economic Development Zone, Zhenhai District, Zhejiang, Ningbo, China Patentee after: Zhejiang Zhenyang Development Co., Ltd Address before: 315204 Chemical Industrial Zone, Zhejiang, Ningbo, China Patentee before: NINGBO OCEANKING CHEMICAL DEVELOPMENT Co.,Ltd. |