CN104928716A - Light salt brine pretreatment device - Google Patents
Light salt brine pretreatment device Download PDFInfo
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- CN104928716A CN104928716A CN201510273198.5A CN201510273198A CN104928716A CN 104928716 A CN104928716 A CN 104928716A CN 201510273198 A CN201510273198 A CN 201510273198A CN 104928716 A CN104928716 A CN 104928716A
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Abstract
The invention relates to a light salt brine pretreatment device. The innovation point is that the light salt brine pretreatment device comprises a salt brine heat exchanger, a circulating pipeline, a sodium sulfite dropwise-adding device and a diluted hydrochloric acid dropwise-adding device, wherein a refrigerant inlet of the salt brine heat exchanger is communicated with light salt brine supply equipment by a pipeline K; a refrigerant outlet of the salt brine heat exchanger is communicated with a light salt brine storage tank by a pipeline L; the two ends of the circulating pipeline are communicated with the bottom of the light salt brine storage tank and the pipeline K respectively; and the sodium sulfite dropwise-adding device and the diluted hydrochloric acid dropwise-adding device are arranged on the pipeline K and the pipeline L. The light salt brine pretreatment device has the advantages that: the initial temperature of the light salt brine entering heat concentration equipment is increased by utilizing the salt brine heat exchanger, and the heat consumption is reduced; the sodium sulfite dropwise-adding device, the diluted hydrochloric acid dropwise-adding device and the salt brine heat exchanger are matched for dissolving chlorate in the light salt brine and regulating the pH value of the light salt brine, so that the light salt brine is controlled to be alkalescent, and the service life of the heat concentration equipment in a next process is prolonged.
Description
Technical field
The present invention relates to a kind of heat-exchanger rig, particularly a kind of light salt brine pretreatment unit.
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 the mode adopting the low electrolytic solution of saltiness to add a large amount of solid salt to combine, namely adopt the electrolytic solution after electrolysis with ion-exchange film or purchase bittern in addition and carry out Substitute For Partial solid salt, solid salt is dropped into again to reach the saliferous standard of electrolytic solution in bittern, because electrolytic solution or bittern price under unit saltiness same case are lower than solid salt, therefore can greatly reduce cost, this kind of mode is generally adopted by producer most of in industry; The third is the mode adopting strong brine to add a small amount of solid salt, heat pump techniques or other hot concentration techniques is utilized to concentrate the low electrolytic solution (light salt brine) of saltiness or bittern, it compares the second way, can reduce the addition of solid salt further, reduce costs.
But general containing free chlorine in electrolytic solution or bittern, it is comparatively large to the corrodibility of thickening equipment, therefore research and develop that a kind of can to reduce the light salt brine pretreatment unit that electrolytic corrosion extends thickening equipment work-ing life imperative.
Summary of the invention
The technical problem to be solved in the present invention is to provide and a kind ofly can reduces electrolytic corrosion and improve the light salt brine pretreatment unit of light salt brine initial temperature.
For solving the problems of the technologies described above, technical scheme of the present invention is: a kind of light salt brine pretreatment unit, its innovative point is: comprise brine heat exchanger, light salt brine supply arrangement, light salt brine storage tank, circulating line, S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder, brine heat exchanger comprises tube side portion and shell side portion, tube side portion has a Heating medium and a heating agent outlet, shell side portion has a refrigerant import and a refrigerant exit, this refrigerant import is communicated with a light salt brine supply arrangement by pipeline K, refrigerant exit is communicated with a light salt brine storage tank by pipeline L, circulating line, the fluid inlet of this circulating line is communicated with light salt brine tank bottom, and liquid outlet is communicated with pipeline K, and is provided with recycle pump on circulating line, 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, configuration liquid service comprises dosing house steward and the S-WAT dosing arm that is communicated with dosing house steward liquid outlet and hydrochloric acid dosing arm, pipeline K on front side of the fluid inlet access circulating line liquid outlet of dosing house steward, the liquid outlet of S-WAT dosing arm and hydrochloric acid dosing arm respectively with S-WAT dosing import, dilute hydrochloric acid dosing inlet communication.
Preferably, described S-WAT dosing arm and hydrochloric acid dosing arm are separately installed with S-WAT dosing stopping valve and hydrochloric acid dosing stopping valve.
Preferably, described pipeline K is provided with sampling line, and on sampling line, being provided with PH detector and redox potential on line analyzer, the output signal access S-WAT of described PH detector and redox potential on line analyzer drips pump and dilute hydrochloric acid drips pump.
The invention has the advantages that:
The Heating medium of brine heat exchanger is connected the hot thickening equipment being used for concentrated light salt brine, strong brine temperature after concentrated generally can reach more than 180 DEG C, imported in brine heat exchanger, in brine heat exchanger, heat exchange is carried out with the 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, to promote light salt brine in the initial temperature entering hot thickening equipment, reduce heat exhaustion, more energy-conservation.
Light salt brine after ion-exchange membrane electrolysis electrolysis is before brine heat exchanger, first in light salt brine, sodium sulfite solution is dripped by S-WAT Dropping feeder, because light salt brine is alkalescence, simultaneously, after brine heat exchanger, light salt brine temperature increase reaches 90 DEG C, is conducive to the decomposition to oxymuriate in light salt brine under this condition, greatly reduce corrodibility, improve the work-ing life of total system; And after heat exchange, in light salt brine, drip the dilute hydrochloric acid of appropriate amount, and then regulate the pH value of light salt brine, light salt brine is controlled in weakly alkaline, extend the work-ing life of the hot thickening equipment of later process.
Sampling line is arranged PH detector and redox potential on line analyzer, to detect pH value and the redox condition of light salt brine, and then control the dropping of dilute hydrochloric acid and sodium sulfite solution, be conducive to realizing Automated condtrol.
Accompanying drawing explanation
Fig. 1 is light salt brine pretreatment unit structural representation of the present invention.
Embodiment
As shown in Figure 1, brine heat exchanger 3, light salt brine supply arrangement, light salt brine storage tank 4, circulating line N, S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder is comprised.
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, the strong brine that Heating medium 31 concentrates out for connecting light salt brine thickening equipment, shell side portion has a refrigerant import 33 and a refrigerant exit 34, this refrigerant import 33 is communicated with a light salt brine supply arrangement by pipeline K, and refrigerant exit 34 is communicated with a light salt brine storage tank 4 by pipeline L.
Circulating line N, the fluid inlet of this circulating line N is communicated with bottom light salt brine storage tank 4, liquid outlet is communicated with pipeline K, and recycle pump 43 is provided with on circulating line N, by pipeline K, pipeline L, circulating line N, brine heat exchanger 3, light salt brine storage tank 4, recycle pump 43 are formed a light salt brine warm-up cycle pipeline.
S-WAT Dropping feeder comprises S-WAT preparation still 51, S-WAT drips pump 52, the top of S-WAT preparation still 51 has S-WAT dosing import 511 and a solid sodium sulfite opening for feed 512, the fluid inlet that S-WAT drips pump 52 is communicated with the bottom that S-WAT prepares still 51, and S-WAT drips the pipeline K on rear side of the liquid outlet access circulating line N liquid outlet of pump 52.
Dilute hydrochloric acid Dropping feeder comprises dilute hydrochloric acid preparation still 61, dilute hydrochloric acid drips pump 62, the top of dilute hydrochloric acid preparation still 61 has a dilute hydrochloric acid dosing import 611 and a pressure equalizing pipe 612, the fluid inlet of dilute hydrochloric acid dropping pump 62 is prepared bottom still 61 with dilute hydrochloric acid and is communicated with, and the liquid outlet that dilute hydrochloric acid drips pump 62 is communicated with pipeline L.
Configuration liquid service comprises dosing house steward P and the S-WAT dosing arm Q that is communicated with dosing house steward P liquid outlet and hydrochloric acid dosing arm R, pipeline K on front side of the fluid inlet access circulating line N liquid outlet of dosing house steward, S-WAT dosing arm Q is communicated with S-WAT dosing import 511, dilute hydrochloric acid dosing import 611 respectively with the liquid outlet of hydrochloric acid dosing arm R.And S-WAT dosing stopping valve 513 and hydrochloric acid dosing stopping valve 613 is separately installed with on S-WAT dosing arm Q and hydrochloric acid dosing arm R.
As the present invention's embodiment more specifically: be provided with sampling line O on pipeline K, and on sampling line O, be provided with PH detector 71 and redox potential on line analyzer 72, the output signal of this PH detector 71 and redox potential on line analyzer 72 accesses S-WAT by DCS or PLC and drips pump 51 and dilute hydrochloric acid dropping pump 61, to detect pH value and the redox condition of light salt brine, and then control the dropping of dilute hydrochloric acid and sodium sulfite solution, be conducive to realizing Automated condtrol.
Principle of work:
Light salt brine after ion-exchange membrane electrolysis electrolysis is entering in pipeline K, by preparation pipeline P, preparation pipeline Q, preparation pipeline R and it on S-WAT dosing stopping valve and hydrochloric acid dosing stopping valve enter S-WAT preparation still, dilute hydrochloric acid preparation still, for preparation sodium sulfite solution and dilute hydrochloric acid provide the light salt brine solvent not containing tramp material;
Light salt brine after ion-exchange membrane electrolysis electrolysis is generally at about 65 DEG C, it enters the shell side part of brine heat exchanger by pipeline K, and reach 180 DEG C by the strong brine temperature after hot thickening equipment concentrates, strong brine enters the tube side part of brine heat exchanger by Heating medium, carry out heat exchange with light salt brine, and then light salt brine is heated to 90-95 DEG C;
Light salt brine after ion-exchange membrane electrolysis electrolysis before the shell side part being entered brine heat exchanger by pipeline K, utilize S-WAT drip pump drip in pipeline K concentration about 4% sodium sulfite solution; Because light salt brine is alkalescence, meanwhile, after brine heat exchanger, light salt brine temperature increase reaches more than 90 DEG C, is beneficial to the decomposition to oxymuriate in light salt brine under this condition, reduces light salt brine to the corrosion of equipment, pipeline;
Light salt brine through heating is entering light salt brine storage tank by pipeline L, utilize dilute hydrochloric acid to drip pump and drip dilute hydrochloric acid in pipeline L, the pH value of dilute hydrochloric acid to light salt brine is utilized to regulate, light salt brine potential of hydrogen is controlled in weak base state, extend the work-ing life of the hot thickening equipment of later process, also be conducive to promoting hot thickening equipment byproduct quality, such as, utilize hydrogen chloride synthesis light salt brine to concentrate the steam quality produced when stove concentrates light salt brine.
More than show and describe ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.Application claims protection domain is defined by appending claims and equivalent thereof.
Claims (3)
1. a light salt brine pretreatment unit, is characterized in that: comprise brine heat exchanger, light salt brine supply arrangement, light salt brine storage tank, circulating line, S-WAT Dropping feeder and dilute hydrochloric acid Dropping feeder,
Brine heat exchanger comprises tube side portion and shell side portion, tube side portion has a Heating medium and a heating agent outlet, shell side portion has a refrigerant import and a refrigerant exit, this refrigerant import is communicated with a light salt brine supply arrangement by pipeline K, and refrigerant exit is communicated with a light salt brine storage tank by pipeline L;
Circulating line, the fluid inlet of this circulating line is communicated with light salt brine tank bottom, and liquid outlet is communicated with pipeline K, and is provided with recycle pump on circulating line;
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;
Configuration liquid service comprises dosing house steward and the S-WAT dosing arm that is communicated with dosing house steward liquid outlet and hydrochloric acid dosing arm, pipeline K on front side of the fluid inlet access circulating line liquid outlet of dosing house steward, the liquid outlet of S-WAT dosing arm and hydrochloric acid dosing arm respectively with S-WAT dosing import, dilute hydrochloric acid dosing inlet communication.
2. light salt brine pretreatment unit according to claim 1, is characterized in that: described S-WAT dosing arm and hydrochloric acid dosing arm are separately installed with S-WAT dosing stopping valve and hydrochloric acid dosing stopping valve.
3. light salt brine pretreatment unit according to claim 1, it is characterized in that: described pipeline K is provided with sampling line, and on sampling line, being provided with PH detector and redox potential on line analyzer, the output signal access S-WAT of described PH detector and redox potential on line analyzer drips pump and dilute hydrochloric acid drips pump.
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| CN201510273198.5A CN104928716B (en) | 2015-05-26 | 2015-05-26 | Light salt brine pretreatment device |
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| CN201510273198.5A CN104928716B (en) | 2015-05-26 | 2015-05-26 | Light salt brine pretreatment device |
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Cited By (2)
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| CN106065484A (en) * | 2016-08-03 | 2016-11-02 | 金川集团股份有限公司 | A kind of ion-exchange membrane electrolyzer anode means for feeding acid and method |
| CN112210788A (en) * | 2020-10-15 | 2021-01-12 | 吕子红 | Method and equipment for decomposing chlorate in light salt water for producing chlor-alkali |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106065484A (en) * | 2016-08-03 | 2016-11-02 | 金川集团股份有限公司 | A kind of ion-exchange membrane electrolyzer anode means for feeding acid and method |
| CN106065484B (en) * | 2016-08-03 | 2018-02-02 | 金川集团股份有限公司 | A kind of ion-exchange membrane electrolyzer anode means for feeding acid and method |
| CN112210788A (en) * | 2020-10-15 | 2021-01-12 | 吕子红 | Method and equipment for decomposing chlorate in light salt water for producing chlor-alkali |
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| Publication number | Publication date |
|---|---|
| CN104928716B (en) | 2017-05-10 |
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Address after: 226500 Jiangsu province Nantong City Jiuhua town Rugao City Huaxing Road No. 8 Patentee after: Nantong star graphite Co., Ltd Address before: 226500 Jiangsu province Nantong City Jiuhua Jiuhua town of Rugao City neighborhood Patentee before: Nantong Xingqiu Graphite Facilities Company |