CN104928714A - Thermal concentration system for dilute brine based on hydrogen chloride synthesis - Google Patents
Thermal concentration system for dilute brine based on hydrogen chloride synthesis Download PDFInfo
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Abstract
The invention relates to a thermal concentration system for dilute brine based on hydrogen chloride synthesis. The thermal concentration system is characterized by comprising a dilute brine concentrating furnace based on hydrogen chloride synthesis, and a flash tank for concentrating dilute brine, wherein a hydrogen chloride synthesis section of the dilute brine concentrating furnace based on hydrogen chloride synthesis is provided with a cyclic-heating clamping sleeve for dilute brine; a pipeline A and a pipeline B of the cyclic-heating clamping sleeve for dilute brine are communicated with the flash tank, so that a thermal concentration circulating channel for dilute brine is formed. Through the adoption of the thermal concentration system for dilute brine based on hydrogen chloride synthesis, which is disclosed by the invention, condensed acid can be directly prepared through cooling, and saturated by-product steam can be generated through the cooperation of a jacket structure and the flash tank; besides, the dilute brine is concentrated, so that four functions of synthesizing the hydrogen chloride, preparing the acid, generating the by-product steam, and concentrating the dilute brine are integrated in the thermal concentration system; the equipment investment is greatly simplified; the resources are reasonably integrated; the cost is reduced.
Description
Technical field
The present invention relates to the hot concentration systems of a kind of light salt brine, particularly the hot concentration systems of a kind of light salt brine based on hydrogen chloride synthesis.
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 310g/L, needs the saltiness again improving electrolytic solution to initial level to continue electrolysis production product.
Mainly adopt at present and improve electrolytic solution saltiness in two ways, the first dissolves enrichment for adopting pure solid salt, and its shortcoming is: when producing caustic soda, alkali per ton needs the solid salt of consumption 1.5 times, and its cost is higher, does not have the market competitiveness; The second is the mode adopting bittern reinforcing body salt to combine, 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.
Summary of the invention
The technical problem to be solved in the present invention is to provide the hot concentration systems of a kind of light salt brine based on hydrogen chloride synthesis, can either byproduct steam, can realize again light salt brine smoothly concentrated, to drop into and running cost low.
For solving the problems of the technologies described above, technical scheme of the present invention is: the hot concentration systems of a kind of light salt brine based on hydrogen chloride synthesis, its innovative point is: comprise hydrogen chloride synthesis light salt brine and concentrate stove and the concentrated flash evaporation tank of light salt brine, described hydrogen chloride synthesis light salt brine concentrates stove and is divided into hydrogen chloride synthesis section and hydrogenchloride cooling section from bottom to top successively, this hydrogen chloride synthesis section has one for absorbing hydrogen chloride synthesis stage heat and is positioned at the light salt brine circulating-heating chuck layer of hydrogen chloride synthesis section high-temperature part, described light salt brine circulating-heating chuck layer top has a light salt brine wetting vapour outlet, bottom has a light salt brine backflow import and at least one light salt brine supplements import, described light salt brine concentrates has a vapour outlet with the center, tank body top of flash evaporation tank, tank wall has the light salt brine bypass outlet that a light salt brine wetting vapour import and being positioned at side wall upper part is positioned at sidewall bottom, and tank body bottom has a strong brine outlet and first discharging hole exported lower than strong brine, above-mentioned light salt brine wetting vapour outlet is by pipeline A and light salt brine wetting vapour inlet communication, and light salt brine backflow import is communicated with light salt brine bypass outlet by pipeline B, and then forms a hot concentration cycles passage of light salt brine.
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 circulating-heating chuck layer is formed between the steel shell of described second hydrogen chloride synthesis section and graphite cylinder body; This light salt brine circulating-heating 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, the light salt brine circulating-heating chuck layer bottom of described second hydrogen chloride synthesis section is provided with the second discharging hole, and this second discharging hole accesses a light salt brine storage tank by pipeline G.
Preferably, the pipeline H of described second hydrogen chloride synthesis section is also equipped with feed flow pneumavalve.
Preferably, the hydrogenchloride outlet of described hydrogenchloride cooling section accesses hydrogenchloride feed channel by pipeline D upwards, and condensation acid outlet accesses a condensation acid tank by downward pipeline E; And pipeline D is communicated with the pipeline E below it by downtake.
Preferably, described light salt brine concentrates and accesses a light salt brine storage tank with the first discharging hole of flash evaporation tank by pipeline F, and is provided with thief hole on pipeline F.
Preferably, described light salt brine concentrates the light salt brine wetting vapour outlet 1 ~ 2m exceeding the second hydrogen chloride synthesis section with the first discharging hole of flash evaporation tank.
The invention has the advantages that:
[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 generate saturation steam, cooling circulating water need not be adopted to carry out most of heat of absorption reaction generation, greatly reduce the consumption of cooling circulating water, reduce the consumption of water resources, reduce costs.
[2] hydrogen chloride synthesis light salt brine concentrates stove and adopts the first hydrogen chloride synthesis section, the second hydrogen chloride synthesis section, tri-chlorination hydrogen synthesis stage and hydrogenchloride cooling section four parts, in the heat absorption cooling that first and third hydrogen chloride synthesis section adopts cooling circulating water to carry out reacting, light salt brine is then adopted to cool at the second section that heat is maximum, meanwhile, this heat is utilized to carry out light salt brine concentrated concentrated; And topmost is hydrogenchloride cooling section, while to hydrogen chloride gas cooling, and be mixed with concentrated hydrochloric acid by the hydrogen chloride gas after dilute hydrochloric acid and cooling.
[3] the hot concentration systems of the light salt brine based on hydrogen chloride synthesis of the present invention directly can either obtain finished product hydrochloric acid, by-product saturation steam can be coordinated with flash evaporation tank again by jacket structured, simultaneously, light salt brine is concentrated, realize the function of hydrogen chloride synthesis, relieving haperacidity, byproduct steam and concentrated light salt brine four-in-one, simplified apparatus drops into greatly, and reasonable integration resource, reduces costs.
[4] access downtake between the pipeline D of hydrogenchloride cooling section hydrogenchloride outlet and the pipeline E that export of condensation acid, the wet hydrogen chloride gas of part is being separated condensation acid by during pipeline D, and this condensation is sour flows directly into condensation acid tank by downtake and pipeline E.
[5] light salt brine concentrates and is provided with thief hole with on the pipeline F of flash evaporation tank first discharging hole, to carry out accurately sampling in concentration process, and then is convenient to Controlling System and controls concentration process and result accurately, guarantee concentrated quality.
Accompanying drawing explanation
Fig. 1 is based on the hot concentration systems structural representation of the light salt brine of hydrogen chloride synthesis in the present invention.
Fig. 2 is that in the present invention, hydrogen chloride synthesis light salt brine concentrates furnace structure schematic diagram.
To be that in the present invention, light salt brine is concentrated use flash evaporation tank structural representation to Fig. 3.
Embodiment
as shown in Figure 1comprise hydrogen chloride synthesis light salt brine and concentrate stove 1 and the concentrated flash evaporation tank 2 of light salt brine, hydrogen chloride synthesis light salt brine concentrates stove 1 and is divided into hydrogen chloride synthesis section and hydrogenchloride cooling section from bottom to top successively, this hydrogen chloride synthesis section has one for absorbing hydrogen chloride synthesis stage heat and is positioned at the light salt brine circulating-heating chuck layer of hydrogen chloride synthesis section high-temperature part, light salt brine circulating-heating 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 has a vapour outlet 22a with the center, tank body top of flash evaporation tank 2, tank wall has the light salt brine bypass outlet 21b that a light salt brine wetting vapour import 21a and being positioned at side wall upper part is positioned at sidewall bottom, and tank body bottom has the first discharging hole 23b that a strong brine outlet 23a and exports lower than strong brine;
Above-mentioned light salt brine wetting vapour outlet j is communicated with light salt brine wetting vapour import 21a by pipeline A, and light salt brine backflow import y is communicated with light salt brine bypass outlet 21b by pipeline B, and then forms a hot concentration cycles passage of light salt brine.
In the present invention, 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 circulating-heating 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 circulating-heating 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 circulating-heating 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 storage tank 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 present invention's embodiment more specifically, access hydrogenchloride feed channel at the hydrogenchloride outlet p of hydrogenchloride cooling section 14 by pipeline D upwards, condensation acid outlet o accesses a condensation acid tank by downward pipeline E; In order to avoid the wet hydrogen chloride gas of part is by the acid blocking that is condensed during pipeline D, pipeline D is communicated with the pipeline E below it by downtake 141, makes condensation acid flow into condensation acid tank smoothly by downtake and pipeline E.
In the present invention, light salt brine is concentrated with flash evaporation tank 2 concrete structure is: it comprises cylindrical shell 21, upper cover 22, lower cover 23, and the upper and lower end of cylindrical shell 21 welds upper cover 22 respectively, lower cover 23 forms an airtight container.
The center, top of upper cover 2 is provided with vapour outlet 22a, and relief valve port 22b and site pressure meter mouth 22c.
Light salt brine wetting vapour import 21a is provided with in the middle part of the sidewall of cylindrical shell 21, the sidewall bottom of cylindrical shell 21 is provided with light salt brine bypass outlet 21b, and this light salt brine bypass outlet 21b is positioned at light salt brine wetting vapour import 21a opposite, the top of cylindrical shell 21 sidewall is also provided with operating pressure meter mouth 21c.
The top of cylindrical shell 21 is built-in with a foam removal net 24, and cylindrical shell 21 top is built-in with the cool water shower head be positioned at above foam removal net 24, this cool water shower head and a cooling water circulation pipeline communication.
In addition, in order to control the liquid inlet volume of light salt brine wetting vapour accurately, the sidewall of cylindrical shell 21 is respectively arranged with the first running liquidometer interface group and the second running liquidometer interface group, and the angle that the first running liquidometer interface group 21d, the second running liquidometer interface group 21e and cylindrical shell 21 axis are formed is 90 °.
The bottom of lower cover 23 is provided with strong brine outlet 23a, and is positioned at the first discharging hole 23b of bottom center.
As the present invention's embodiment more specifically, light salt brine concentrates and accesses a light salt brine storage tank with the first discharging hole 23b of flash evaporation tank 2 by pipeline F, the light salt brine storage tank that this light salt brine storage tank and the second discharging hole access is same, and is provided with thief hole on pipeline F; This first discharging hole 23b exceeds the light salt brine wetting vapour outlet j1 ~ 2m of the second hydrogen chloride synthesis section 12 in addition.
Principle of work:
Light salt brine enters by light salt brine high-pressure pump and pipeline H the light salt brine circulating-heating 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 circulating-heating 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 circulating-heating 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.
Table one: under indicate the every contrast adopting light salt brine of the present invention hot concentration systems to prepare strong brine and other usual manners to prepare strong brine:
conclusion:the hot concentration systems of light salt brine of the present invention and heat pump concentration technique all adopt bittern to concentrate, and add a small amount of solid salt, raw materials cost is low; In addition, comparatively heat pump concentration technique is lower for the concentrated cost of the hot concentration systems of light salt brine, and input cost is little.
The present invention is based on the additional economic benefit of the hot concentration systems of light salt brine of hydrogen chloride synthesis, for hydrogenchloride output 150t/d:
(1) byproduct steam: hydrogenchloride per ton can by-product 0.65 ton of pressure at the saturation steam of 0.6 ~ 0.9MPaGd, the average byproduct steam 4.1t/h of single hot concentration systems, produces moon 32800t/a per year, by 150 yuan/ton of vaporimeters, can improve effects 4,920,000 yuan; Meanwhile, the heat of hydrogen chloride synthetic reaction is absorbed by light salt brine, and decrease recirculating cooling water system investment, run and recirculated water consumption costs, byproduct steam pure water expense etc., can accumulate added benefit about 5,970,000 yuan the whole year.
(2) concentrated light salt brine: for the light salt brine of 200g/l, it is through the heat of absorbing hydrogen chloride synthesis, the moisture of 4.1t/h can be evaporated, namely the light salt brine of 13.9t/h (i.e. concentration 200g/l) can be condensed into the strong brine (concentration 300g/l) of 9.7t/h.The thermo-compression evaporation technique that current employing is more advanced, it often evaporates 1 ton of water, and normal production cost is 30 yuan, and adopts the hot concentration systems of light salt brine of the present invention can workout cost about 1,000,000 yuan, and without the need to extra heat pump evaporation equipment investment.
(3) light salt brine or bittern consumption during lifting electrolysis with ion-exchange film liquid saltiness: because 100% caustic soda salt consumption per ton is at 1500kg; Solid sodium chloride cost per ton is 250-280 unit, and be often 150-180 unit containing the light salt brine of one ton of salt or bittern cost, and light salt brine directly can be concentrated into the strong brine of concentration 300g/l by the hot concentration systems of light salt brine of the present invention, add and a small amount of solid salt, namely whole the or overwhelming majority adopts light salt brine preparation; Can supporting 100% caustic soda 1.69t/h, annual supporting 1.35 ten thousand ton of 100% caustic soda ability, adopts whole or most light salt brine or bittern to produce, and annually reduces production cost about 2,000,000 yuan.
Claims (7)
1. based on the hot concentration systems of light salt brine of hydrogen chloride synthesis, it is characterized in that: comprise hydrogen chloride synthesis light salt brine and concentrate stove and the concentrated flash evaporation tank of light salt brine,
Described hydrogen chloride synthesis light salt brine concentrates stove and is divided into hydrogen chloride synthesis section and hydrogenchloride cooling section from bottom to top successively, this hydrogen chloride synthesis section has one for absorbing hydrogen chloride synthesis stage heat and is positioned at the light salt brine circulating-heating chuck layer of hydrogen chloride synthesis section high-temperature part, described light salt brine circulating-heating 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;
Described light salt brine concentrates has a vapour outlet with the center, tank body top of flash evaporation tank, tank wall has the light salt brine bypass outlet that a light salt brine wetting vapour import and being positioned at side wall upper part is positioned at sidewall bottom, and tank body bottom has a strong brine outlet and first discharging hole exported lower than strong brine;
Above-mentioned light salt brine wetting vapour outlet is by pipeline A and light salt brine wetting vapour inlet communication, and light salt brine backflow import is communicated with light salt brine bypass outlet by pipeline B, and then forms a hot concentration cycles passage of light salt brine.
2. the hydrogen chloride synthesis heat that utilizes according to claim 1 concentrates light salt brine system, 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 circulating-heating chuck layer is formed between the steel shell of described second hydrogen chloride synthesis section and graphite cylinder body; This light salt brine circulating-heating 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. the hydrogen chloride synthesis heat that utilizes according to claim 2 concentrates light salt brine system, it is characterized in that: the light salt brine circulating-heating chuck layer bottom of described second hydrogen chloride synthesis section is provided with the second discharging hole, and this second discharging hole accesses a light salt brine storage tank by pipeline G.
4. the hydrogen chloride synthesis heat that utilizes according to claim 2 concentrates light salt brine system, it is characterized in that: the pipeline H of described second hydrogen chloride synthesis section is also equipped with feed flow pneumavalve.
5. the hydrogen chloride synthesis heat that utilizes according to claim 2 concentrates light salt brine system, it is characterized in that: the hydrogenchloride outlet of described hydrogenchloride cooling section accesses hydrogenchloride feed channel by pipeline D upwards, condensation acid outlet accesses a condensation acid tank by downward pipeline E; And pipeline D is communicated with the pipeline E below it by downtake.
6. the hydrogen chloride synthesis heat that utilizes according to claim 1 concentrates light salt brine system, it is characterized in that: described light salt brine concentrates and accesses a light salt brine storage tank with the first discharging hole of flash evaporation tank by pipeline F, and is provided with thief hole on pipeline F.
7. the hydrogen chloride synthesis heat that utilizes according to claim 5 concentrates light salt brine system, it is characterized in that: described light salt brine concentrates the light salt brine wetting vapour outlet 1 ~ 2m exceeding the second hydrogen chloride synthesis section with the first discharging hole of flash evaporation tank.
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| CN107999459A (en) * | 2017-12-12 | 2018-05-08 | 南通星球石墨设备有限公司 | A kind of pickling stone device and method |
| CN107999459B (en) * | 2017-12-12 | 2023-08-15 | 南通星球石墨股份有限公司 | Stone pickling equipment and method |
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