CN204714914U - A kind of production of caustic soda electrolytic solution recycling system - Google Patents
A kind of production of caustic soda electrolytic solution recycling system Download PDFInfo
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- CN204714914U CN204714914U CN201520345264.0U CN201520345264U CN204714914U CN 204714914 U CN204714914 U CN 204714914U CN 201520345264 U CN201520345264 U CN 201520345264U CN 204714914 U CN204714914 U CN 204714914U
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- light salt
- salt brine
- brine
- hydrogen chloride
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Abstract
The utility model relates to a kind of production of caustic soda electrolytic solution recycling system, its innovative point is: comprise hydrogen chloride synthesis light salt brine and concentrate stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank, and described hydrogen chloride synthesis light salt brine concentrates stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank and forms one by each pipeline communication.The utility model has the advantage of: utilize hydrogen chloride synthesis light salt brine to concentrate stove and light salt brine and concentrate concentration systems with flash evaporation tank composition, realize the recycling of salt solution, and can saturation steam be produced.Brine temp after concentrated is at about 180 DEG C, imported in brine heat exchanger, in brine heat exchanger, heat exchange is carried out with the electrolytic solution after adopting ion-exchange membrane electrolysis electrolysis, the light salt brine of about 65 DEG C is heated to about 95 DEG C, promote light salt brine and enter the initial temperature that hydrogen chloride synthesis light salt brine concentrates stove, reduce heat exhaustion.
Description
Technical field
The utility model relates to a kind of electrolytic solution recycling system, particularly a kind of production of caustic soda electrolytic solution recycling system.
Background technology
Chlor-alkali industry mainly adopts diaphragm process and ion-exchange membrane electrolysis two kinds of production technique to make related products, in the production process of ion-exchange membrane electrolysis, electrolytic solution is after electrolysis, its saltiness can be down to about 200g/L from 300 ~ 310g/L, needs the saltiness again improving electrolytic solution to initial level to continue electrolysis production product.
Mainly adopt at present and improve saltiness in two ways, the first is for adopting pure solid salt, and its shortcoming is: when producing caustic soda, alkali per ton needs the solid salt of consumption 1.5 tons, and its cost is higher, does not have the market competitiveness, has substantially seldom adopted; The second is adopt bittern to add the mode that a large amount of solid salt combines, namely under procurement unit's saltiness same case, price carrys out Substitute For Partial solid salt lower than the bittern of solid salt, in bittern, drop into solid salt again to reach the saliferous standard of electrolytic solution, this kind of mode is generally adopted by producer most of in industry; The third is the mode adopting concentrated brine to add a small amount of solid salt, utilize heat pump techniques concentrated brine, it compares the second way, the addition of solid salt can be reduced further, reduce costs, but heat pump techniques initial investment is very large, and also has certain cost in use, and the cost of concentrated brine is at about 30 yuan/ton.
Therefore, the electrolytic solution saltiness method for improving that further a kind of cost of research and development is cheaper and relevant device imperative.
Utility model content
The technical problems to be solved in the utility model is to provide the low and energy-conservation production of caustic soda electrolytic solution recycling system of a kind of production cost.
For solving the problems of the technologies described above, the technical solution of the utility model is: a kind of production of caustic soda electrolytic solution recycling system, its innovative point is: comprise hydrogen chloride synthesis light salt brine and concentrate stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank, and described hydrogen chloride synthesis light salt brine concentrates stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank and forms one by each pipeline communication; Hydrogen chloride synthesis light salt brine concentrates stove and accessory has one for absorbing hydrogen chloride synthesis stage heat and the light salt brine circulation chuck layer being positioned at hydrogen chloride synthesis section high-temperature part, this light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet, and bottom has a light salt brine backflow import and at least one light salt brine supplements import; Light salt brine concentrates to be had one with the tank wall of flash evaporation tank and is positioned at side wall upper part and by the light salt brine wetting vapour import of pipeline A and light salt brine wetting vapour outlet, and one is positioned at sidewall bottom and the light salt brine bypass outlet of the inlet communication that refluxed by pipeline B and light salt brine, tank body bottom has a strong brine outlet; Brine heat exchanger comprises tube side portion and shell side portion, tube side portion has a Heating medium and a heating agent outlet, this Heating medium concentrates the strong brine outlet with flash evaporation tank by pipeline I and light salt brine, and heating agent outlet accesses one for storing the brine tank of strong brine by pipeline J; Shell side portion has a refrigerant import and a refrigerant exit, and this refrigerant import is communicated with light salt brine supply arrangement by pipeline K, and refrigerant exit is communicated with light salt brine storage tank by pipeline L; And refrigerant import or export side is provided with S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder; Light salt brine tank bottom has a light salt brine and supplements outlet, and this light salt brine supplements outlet and supplements inlet communication by pipeline M and light salt brine and then supplement light salt brine for hydrogen chloride synthesis light salt brine concentrates stove, and is provided with light salt brine high-pressure pump on pipeline M.
Preferably, described hydrogen chloride synthesis light salt brine concentrates stove and is mainly divided into the first hydrogen chloride synthesis section, the second hydrogen chloride synthesis section, tri-chlorination hydrogen synthesis stage and hydrogenchloride cooling section four parts from bottom to top, and it is formed by graphite cylinder body and the steel shell be enclosed within outside cylindrical shell; Each steel shell of four parts all forms a unsplit casing by Flange joint, and each graphite cylinder body connects conducting and forms a graphite inner container; A cooling water circulation chuck layer of the first hydrogen chloride synthesis section is formed between the steel shell of described first hydrogen chloride synthesis section and graphite cylinder body; Bottom first hydrogen chloride synthesis section cooling water circulation chuck layer, there is a cooling water circulation import of lower floor; A light salt brine circulation chuck layer is formed between the steel shell of described second hydrogen chloride synthesis section and graphite cylinder body; This light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet, and bottom has a light salt brine backflow import and at least one light salt brine supplements import; This light salt brine supplements import and carries out feed flow by light salt brine high-pressure pump by pipeline H; Form a cooling water circulation chuck layer of tri-chlorination hydrogen synthesis stage between the steel shell of described tri-chlorination hydrogen synthesis stage and graphite cylinder body, tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer top has a cooling water circulation outlet of lower floor; This tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer is communicated with the cooling water circulation chuck layer of formation lower floor with the first hydrogen chloride synthesis section cooling water circulation chuck layer by pipeline C; Form a cooling water circulation chuck layer of hydrogenchloride cooling section between the steel shell of described hydrogenchloride cooling section and graphite cylinder body, the bottom of hydrogenchloride cooling section cooling water circulation chuck layer and top are respectively equipped with the cooling water circulation outlet of the cooling water circulation import in upper strata and upper strata; The steel shell bottom of hydrogenchloride cooling section is provided with the hydrogenchloride that graphite cylinder body inner with it be communicated with to export, is provided with the condensation acid that graphite cylinder body inner with it be communicated with on bottom the steel shell of hydrogenchloride cooling section and exports.
Preferably, described light salt brine high-pressure pump has two, is arranged in parallel on pipeline M.
Preferably, be also provided with a circulating line between described brine heat exchanger and light salt brine storage tank, the fluid inlet of this circulating line is communicated with light salt brine tank bottom, and liquid outlet is communicated with the pipeline K on front side of brine heat exchanger, and is provided with recycle pump on circulating line.
Preferably, described pipeline K is provided with sampling line O.
The utility model has the advantage of:
(1) utilize hydrogen chloride synthesis light salt brine to concentrate stove and light salt brine and concentrate concentration systems with flash evaporation tank composition, it is in the process preparing hydrogen chloride gas, the heat of reaction is utilized to carry out concentrated light salt brine, and then improve the concentration of light salt brine, realize the recycling of salt solution, and can saturation steam be produced; Meanwhile, hydrogen chloride synthesis light salt brine concentrates stove and need not all adopt cooling circulating water to carry out most of heat of absorption reaction generation, can reduce the consumption of cooling circulating water, reduce costs.
(2) brine temp after concentrating is at about 180 DEG C, imported in brine heat exchanger, in brine heat exchanger, heat exchange is carried out with the electrolytic solution (light salt brine) after adopting ion-exchange membrane electrolysis electrolysis, the light salt brine of about 65 DEG C is heated to about 95 DEG C, promote light salt brine and enter the initial temperature that hydrogen chloride synthesis light salt brine concentrates stove, reduce heat exhaustion.
(3) S-WAT Dropping feeder is utilized to drip S-WAT in light salt brine, because light salt brine is alkalescence, simultaneously, after brine heat exchanger, light salt brine temperature reaches 90 DEG C, and it is conducive to the decomposition of oxymuriate in light salt brine, greatly reduce corrodibility, improve the work-ing life of total system; Dilute hydrochloric acid Dropping feeder, for regulating the pH value of light salt brine in pipeline, avoids pH value excessive.
Accompanying drawing explanation
Fig. 1 is the utility model production of caustic soda electrolytic solution recycling system architecture schematic diagram.
Fig. 2 is that the utility model hydrogen chloride synthesis light salt brine concentrates furnace structure schematic diagram.
Embodiment
As shown in Figure 1, the utility model production of caustic soda electrolytic solution recycling system mainly comprises hydrogen chloride synthesis light salt brine and concentrates stove 1, light salt brine concentrated flash evaporation tank 2, brine heat exchanger 3 and light salt brine storage tank 4, and hydrogen chloride synthesis light salt brine concentrates stove 1, light salt brine is concentrated forms one with flash evaporation tank 2, brine heat exchanger 3 and light salt brine storage tank 4 by each pipeline communication.
Hydrogen chloride synthesis light salt brine concentrates stove 1 to be had one for absorbing hydrogen chloride synthesis stage heat and is positioned at the light salt brine circulation chuck layer of hydrogen chloride synthesis section high-temperature part, this light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet j, and bottom has a light salt brine backflow import y and at least one light salt brine supplements import i;
Light salt brine concentrates to be had one with the tank wall of flash evaporation tank 2 and is positioned at side wall upper part and exports by pipeline A and light salt brine wetting vapour the light salt brine wetting vapour import 21a that j is communicated with, and one is positioned at sidewall bottom and is refluxed the light salt brine bypass outlet 21b that import y is communicated with by pipeline B and light salt brine, tank body bottom has a strong brine outlet 23a;
Brine heat exchanger 3 comprises tube side portion and shell side portion, tube side portion has a Heating medium 31 and a heating agent outlet 32, this Heating medium 31 is concentrated by pipeline I and light salt brine and exports 23a with the strong brine of flash evaporation tank 2 and be communicated with, and heating agent outlet 32 accesses one for storing the brine tank of strong brine by pipeline J; Shell side portion has a refrigerant import 33 and a refrigerant exit 34, and this refrigerant import 33 is communicated with light salt brine supply arrangement by pipeline K, and refrigerant exit 34 is communicated with light salt brine storage tank 4 by pipeline L; And refrigerant import 33 or outlet 34 sides are provided with S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder.
There is bottom light salt brine storage tank 4 light salt brine and supplement outlet 41, this light salt brine supplements outlet 41 and supplements import i by pipeline M with light salt brine and be communicated with and then supplement light salt brine for hydrogen chloride synthesis light salt brine concentrates stove 1, and is provided with light salt brine high-pressure pump 42 on pipeline M.In the present embodiment, light salt brine high-pressure pump 42 has two, is arranged in parallel on pipeline M.
Also be provided with a circulating line N between brine heat exchanger 3 and light salt brine storage tank 4, the fluid inlet of this circulating line N is communicated with bottom light salt brine storage tank 4, and liquid outlet is communicated with the pipeline K on front side of brine heat exchanger 3, and is provided with recycle pump 43 on circulating line N.In addition, in order to accurately regulate the pH value of light salt brine, and measure the content of its free chloro ion, pipeline K is provided with sampling line O.
As the utility model embodiment more specifically, hydrogen chloride synthesis light salt brine concentrates the concrete structure of stove 1
as shown in Figure 2: be mainly divided into the first hydrogen chloride synthesis section 11, second hydrogen chloride synthesis section 12, tri-chlorination hydrogen synthesis stage 13 and hydrogenchloride cooling section 14 4 parts from bottom to top, it is formed by graphite cylinder body and the steel shell be enclosed within outside cylindrical shell; Each steel shell of four parts all forms a unsplit casing by Flange joint, and each graphite cylinder body connects conducting and forms a graphite inner container.
A cooling water circulation chuck layer of the first hydrogen chloride synthesis section is formed between the steel shell 111 of the first hydrogen chloride synthesis section 11 and graphite cylinder body 112; And bottom the first hydrogen chloride synthesis section cooling water circulation chuck layer, there is a cooling water circulation import e of lower floor;
A light salt brine circulation chuck layer is formed between the steel shell 121 of the second hydrogen chloride synthesis section 12 and graphite cylinder body 122; This light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet j, and bottom has a light salt brine backflow import y and at least one light salt brine supplements import i; This light salt brine supplements import i and carries out feed flow by light salt brine high-pressure pump by pipeline H, and is also equipped with feed flow pneumavalve 121 on pipeline H, and this feed flow pneumavalve 121 concentrates according to light salt brine and undertaken opening and closing supplementary light salt brine by the liquid level of flash evaporation tank 2.In addition, the light salt brine circulation chuck layer bottom of the second hydrogen chloride synthesis section 12 is provided with the second discharging hole h and accesses a light salt brine groove by pipeline G.
Form a cooling water circulation chuck layer of tri-chlorination hydrogen synthesis stage between the steel shell 131 of tri-chlorination hydrogen synthesis stage 13 and graphite cylinder body 132, tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer top has a lower floor cooling water circulation outlet l; This tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer is communicated with the cooling water circulation chuck layer of formation lower floor with the first hydrogen chloride synthesis section cooling water circulation chuck layer by pipeline C;
Form a cooling water circulation chuck layer of hydrogenchloride cooling section between the steel shell 141 of above-mentioned hydrogenchloride cooling section 14 and graphite cylinder body 142, the bottom of hydrogenchloride cooling section cooling water circulation chuck layer and top are respectively equipped with upper strata cooling water circulation import n and upper strata cooling water circulation outlet q; The steel shell bottom of hydrogenchloride cooling section 14 is provided with the hydrogenchloride that graphite cylinder body inner with it be communicated with and exports p, be provided with the condensation acid that graphite cylinder body inner with it be communicated with on bottom the steel shell of hydrogenchloride cooling section 14 and export o.、
As the utility model embodiment more specifically: S-WAT Dropping feeder comprises S-WAT preparation still, S-WAT drips pump, the top of described S-WAT preparation still has a S-WAT dosing import and a solid sodium sulfite opening for feed, the fluid inlet that S-WAT drips pump is communicated with the bottom that S-WAT prepares still, and S-WAT drips the pipeline K on rear side of the liquid outlet access circulating line liquid outlet of pump;
Dilute hydrochloric acid Dropping feeder comprises dilute hydrochloric acid preparation still, dilute hydrochloric acid drips pump, the top of described dilute hydrochloric acid preparation still has a dilute hydrochloric acid dosing import and a pressure equalizing pipe, the fluid inlet of dilute hydrochloric acid dropping pump is prepared bottom still with dilute hydrochloric acid and is communicated with, and the liquid outlet that dilute hydrochloric acid drips pump is communicated with pipeline L.
Principle of work of the present utility model:
Light salt brine enters by light salt brine high-pressure pump and pipeline H the light salt brine circulation chuck layer that hydrogen chloride synthesis light salt brine concentrates stove, hydrogen chloride synthesis light salt brine concentrate stove burn with hydrogen and chlorine prepare hydrogen chloride gas process in release a large amount of heat, this heat major part is absorbed by the light salt brine in light salt brine circulation chuck layer, forms High Temperature High Pressure light salt brine wetting vapour;
Light salt brine wetting vapour enters the concentrated flash evaporation tank of light salt brine by pipeline A, due to pressure drop, make light salt brine generation Evaporation Phenomenon, moisture in light salt brine is formed by evaporation to steam and discharges with flash evaporation tank top from light salt brine is concentrated, and the light salt brine that saltiness increases continue through light salt brine bypass outlet be back to hydrogen chloride synthesis light salt brine concentrate stove light salt brine circulation chuck layer continue heating and pressurizing, evaporate again to enter in the concentrated flash evaporation tank of light salt brine.
In continuous evaporation, concentration process, liquid level reduces gradually, utilizes light salt brine to concentrate and monitors its inside liquid level with the liquidometer of flash evaporation tank tank wall, when liquid level is lower than set(ting)value, then control pipeline H conducting, for the hot concentration cycles passage of light salt brine supplements light salt brine by feed flow pneumavalve;
Timing gathers light salt brine from the thief hole of pipeline F and concentrates with the salt solution flash evaporation tank, when light salt brine saltiness is progressively increased to the strong brine requiring concentration, it can be discharged from the strong brine outlet bottom lower cover.
More than show and describe ultimate principle of the present utility model and principal character and advantage of the present utility model.The technician of the industry should understand; the utility model is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present utility model; under the prerequisite not departing from the utility model spirit and scope; the utility model also has various changes and modifications, and these changes and improvements all fall within the scope of claimed the utility model.The claimed scope of the utility model is defined by appending claims and equivalent thereof.
Claims (5)
1. a production of caustic soda electrolytic solution recycling system, it is characterized in that: comprise hydrogen chloride synthesis light salt brine and concentrate stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank, described hydrogen chloride synthesis light salt brine concentrates stove, the concentrated flash evaporation tank of light salt brine, brine heat exchanger and light salt brine storage tank and forms one by each pipeline communication;
Hydrogen chloride synthesis light salt brine concentrates stove and accessory has one for absorbing hydrogen chloride synthesis stage heat and the light salt brine circulation chuck layer being positioned at hydrogen chloride synthesis section high-temperature part, this light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet, and bottom has a light salt brine backflow import and at least one light salt brine supplements import;
Light salt brine concentrates to be had one with the tank wall of flash evaporation tank and is positioned at side wall upper part and by the light salt brine wetting vapour import of pipeline A and light salt brine wetting vapour outlet, and one is positioned at sidewall bottom and the light salt brine bypass outlet of the inlet communication that refluxed by pipeline B and light salt brine, tank body bottom has a strong brine outlet;
Brine heat exchanger comprises tube side portion and shell side portion, tube side portion has a Heating medium and a heating agent outlet, this Heating medium concentrates the strong brine outlet with flash evaporation tank by pipeline I and light salt brine, and heating agent outlet accesses one for storing the brine tank of strong brine by pipeline J; Shell side portion has a refrigerant import and a refrigerant exit, and this refrigerant import is communicated with light salt brine supply arrangement by pipeline K, and refrigerant exit is communicated with light salt brine storage tank by pipeline L; And refrigerant import or export side is provided with S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder;
Light salt brine tank bottom has a light salt brine and supplements outlet, and this light salt brine supplements outlet and supplements inlet communication by pipeline M and light salt brine and then supplement light salt brine for hydrogen chloride synthesis light salt brine concentrates stove, and is provided with light salt brine high-pressure pump on pipeline M.
2. production of caustic soda electrolytic solution recycling system according to claim 1, it is characterized in that: described hydrogen chloride synthesis light salt brine concentrates stove and is mainly divided into the first hydrogen chloride synthesis section, the second hydrogen chloride synthesis section, tri-chlorination hydrogen synthesis stage and hydrogenchloride cooling section four parts from bottom to top, it is formed by graphite cylinder body and the steel shell be enclosed within outside cylindrical shell; Each steel shell of four parts all forms a unsplit casing by Flange joint, and each graphite cylinder body connects conducting and forms a graphite inner container;
A cooling water circulation chuck layer of the first hydrogen chloride synthesis section is formed between the steel shell of described first hydrogen chloride synthesis section and graphite cylinder body; Bottom first hydrogen chloride synthesis section cooling water circulation chuck layer, there is a cooling water circulation import of lower floor;
A light salt brine circulation chuck layer is formed between the steel shell of described second hydrogen chloride synthesis section and graphite cylinder body; This light salt brine circulation chuck layer top has a light salt brine wetting vapour outlet, and bottom has a light salt brine backflow import and at least one light salt brine supplements import; This light salt brine supplements import and carries out feed flow by light salt brine high-pressure pump by pipeline H;
Form a cooling water circulation chuck layer of tri-chlorination hydrogen synthesis stage between the steel shell of described tri-chlorination hydrogen synthesis stage and graphite cylinder body, tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer top has a cooling water circulation outlet of lower floor; This tri-chlorination hydrogen synthesis stage cooling water circulation chuck layer is communicated with the cooling water circulation chuck layer of formation lower floor with the first hydrogen chloride synthesis section cooling water circulation chuck layer by pipeline C;
Form a cooling water circulation chuck layer of hydrogenchloride cooling section between the steel shell of described hydrogenchloride cooling section and graphite cylinder body, the bottom of hydrogenchloride cooling section cooling water circulation chuck layer and top are respectively equipped with the cooling water circulation outlet of the cooling water circulation import in upper strata and upper strata; The steel shell bottom of hydrogenchloride cooling section is provided with the hydrogenchloride that graphite cylinder body inner with it be communicated with to export, is provided with the condensation acid that graphite cylinder body inner with it be communicated with on bottom the steel shell of hydrogenchloride cooling section and exports.
3. production of caustic soda electrolytic solution recycling system according to claim 1, is characterized in that: described light salt brine high-pressure pump has two, is arranged in parallel on pipeline M.
4. production of caustic soda electrolytic solution recycling system according to claim 1, it is characterized in that: between described brine heat exchanger and light salt brine storage tank, be also provided with a circulating line, the fluid inlet of this circulating line is communicated with light salt brine tank bottom, liquid outlet is communicated with the pipeline K on front side of brine heat exchanger, and is provided with recycle pump on circulating line.
5. production of caustic soda electrolytic solution recycling system according to claim 4, is characterized in that: described pipeline K is provided with sampling line O.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520345264.0U CN204714914U (en) | 2015-05-26 | 2015-05-26 | A kind of production of caustic soda electrolytic solution recycling system |
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| CN201520345264.0U CN204714914U (en) | 2015-05-26 | 2015-05-26 | A kind of production of caustic soda electrolytic solution recycling system |
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| CN204714914U true CN204714914U (en) | 2015-10-21 |
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| CN201520345264.0U Withdrawn - After Issue CN204714914U (en) | 2015-05-26 | 2015-05-26 | A kind of production of caustic soda electrolytic solution recycling system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104928715A (en) * | 2015-05-26 | 2015-09-23 | 南通星球石墨设备有限公司 | Electrolyte recycling system for caustic soda production |
-
2015
- 2015-05-26 CN CN201520345264.0U patent/CN204714914U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104928715A (en) * | 2015-05-26 | 2015-09-23 | 南通星球石墨设备有限公司 | Electrolyte recycling system for caustic soda production |
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| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20151021 Effective date of abandoning: 20170510 |
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| AV01 | Patent right actively abandoned |