CN217398466U - Soda production system - Google Patents
Soda production system Download PDFInfo
- Publication number
- CN217398466U CN217398466U CN202220910753.6U CN202220910753U CN217398466U CN 217398466 U CN217398466 U CN 217398466U CN 202220910753 U CN202220910753 U CN 202220910753U CN 217398466 U CN217398466 U CN 217398466U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- soda
- neutralization tower
- inlet
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 84
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 64
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 35
- 238000001704 evaporation Methods 0.000 claims abstract description 31
- 230000008020 evaporation Effects 0.000 claims abstract description 29
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 28
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 21
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 21
- 235000017550 sodium carbonate Nutrition 0.000 claims abstract description 20
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 20
- 239000000463 material Substances 0.000 claims abstract description 19
- 239000012452 mother liquor Substances 0.000 claims abstract description 16
- 238000001035 drying Methods 0.000 claims abstract description 15
- 239000000872 buffer Substances 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 9
- 238000005119 centrifugation Methods 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 42
- 229910021529 ammonia Inorganic materials 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 12
- 239000002699 waste material Substances 0.000 abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 239000003513 alkali Substances 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 230000009897 systematic effect Effects 0.000 abstract description 2
- 230000009466 transformation Effects 0.000 abstract description 2
- 238000010276 construction Methods 0.000 abstract 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 14
- 239000007789 gas Substances 0.000 description 14
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 235000019270 ammonium chloride Nutrition 0.000 description 7
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 6
- 239000001110 calcium chloride Substances 0.000 description 6
- 229910001628 calcium chloride Inorganic materials 0.000 description 6
- 238000004821 distillation Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 235000017557 sodium bicarbonate Nutrition 0.000 description 6
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical class O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 5
- 238000009621 Solvay process Methods 0.000 description 4
- 239000012295 chemical reaction liquid Substances 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241000208125 Nicotiana Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005008 domestic process Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 229940074869 marquis Drugs 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- VBUNOIXRZNJNAD-UHFFFAOYSA-N ponazuril Chemical compound CC1=CC(N2C(N(C)C(=O)NC2=O)=O)=CC=C1OC1=CC=C(S(=O)(=O)C(F)(F)F)C=C1 VBUNOIXRZNJNAD-UHFFFAOYSA-N 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- -1 soda ash Chemical compound 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
Classifications
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The utility model discloses a soda production system belongs to soda production technical field. The technical scheme is as follows: comprises a neutralization tower, wherein a caustic soda inlet of the neutralization tower is connected with a caustic soda pipeline, and a carbon dioxide gas inlet of the neutralization tower is connected with a carbon dioxide gas pipeline; the discharge hole of the neutralization tower is respectively connected with the feed inlets of a plurality of evaporators through pipelines, and the evaporation completion liquid outlet of each evaporator is connected with an evaporation completion liquid tank through a pipeline; the evaporation completion liquid tank is connected with the centrifuge; the centrifugal mother liquor outlet of the centrifugal machine is connected with a centrifugal mother liquor backflow inlet of the evaporator through a pipeline, the soda ash outlet of the centrifugal machine is connected with an inlet of the soda ash material conveying device through a pipeline, and an outlet of the soda ash material conveying device is connected with the drying device through a pipeline. The utility model discloses do not have ammonia still process's ammonia still waste liquid problem, also need not to construct one set of synthetic ammonia device like alliing oneself with the supporting construction of alkali process, still reduced carbon volume of subtracting simultaneously, can effectively promote the green transformation of economic society and systematic deep-turning.
Description
Technical Field
The utility model relates to a soda production technical field, concretely relates to soda production system.
Background
At present, the domestic soda production processes mainly comprise the following two processes:
1. ammonia-soda process (also known as Sorviei process)
The process takes raw salt and limestone as main raw materials. The refined saturated brine is made into ammonia brine after absorbing ammonia, and reacts with carbon dioxide generated after limestone decomposition to generate sodium bicarbonate. Sodium bicarbonate is calcined in the calcining process to generate sodium carbonate, namely light alkali and carbon dioxide, the light alkali is hydrated and then calcined again to obtain heavy soda ash, and the carbon dioxide is compressed to be used as high-concentration carbon dioxide gas to react with ammonia brine to generate the sodium bicarbonate. The mother liquor after the carbonization reaction contains a large amount of ammonia, which is mainly present in the form of ammonium chloride. The mother liquor is mixed with calcium hydroxide prepared from calcium oxide generated after limestone calcination to generate ammonia hydroxide and calcium chloride. After the ammonia hydroxide is distilled, the ammonia is recycled, and the calcium chloride is discharged along with the ammonia distillation waste liquid.
The discharge amount of the ammonia distillation waste liquid is about 10t/t of soda ash, and the main component of the ammonia distillation waste liquid is calcium chloride. At present, the main domestic method for treating the waste liquid is accumulation storage, and a small amount of waste liquid is also used for preparing calcium chloride, but because the amount of the waste liquid is too large, the calcium chloride prepared for treating ammonia distillation waste liquid can be called as the water car salary, and because the market is too small, the generation of the calcium chloride is not good for experts in the industry.
It is expected that the process for producing soda by the ammonia-soda process is eliminated in short time along with the increasingly strict environmental protection policy in China.
2. Combined alkali method (also known as marquis alkali manufacturing method)
The process is provided for solving the problem of ammonia distillation waste liquid generated by an ammonia-soda process. The process needs a set of soda ash generating device and a matched ammonia synthesis device.
The refined saturated brine is made into ammonia brine after absorbing ammonia, and reacts with carbon dioxide from an ammonia synthesis device to generate sodium bicarbonate. Sodium bicarbonate is calcined to generate sodium carbonate, namely soda ash, and ammonium chloride in the carbonized mother liquor is crystallized and separated out from the mother liquor after evaporation and filtration and is sold as a product.
The ammonium chloride is a chemical fertilizer, but because of the existence of chlorine, the ammonium chloride can be used as a fertilizer, soil can be hardened, the quality of most crops such as fruits, tobaccos and the like can be reduced, the ammonium chloride can be only used in paddy fields in south China, and the market of the ammonium chloride is limited because the ammonium chloride is inferior to that of most other fertilizers at present.
Although the united alkali method successfully solves the problem of ammonia distillation waste liquid of the ammonia-alkali method, a set of matched ammonia synthesis device needs to be built at the same time, so that the investment, the occupied area and the like of the soda ash device with the same scale are greatly increased.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: overcomes the defects of the prior art, and provides a soda production system and a production process thereof to solve the problems.
In one aspect, the utility model provides a soda production system, which comprises a neutralization tower, wherein a caustic soda inlet of the neutralization tower is connected with a caustic soda pipeline, and a carbon dioxide gas inlet of the neutralization tower is connected with a carbon dioxide gas pipeline; the discharge hole of the neutralization tower is respectively connected with the feed inlets of a plurality of evaporators through pipelines, and the evaporation completion liquid outlet of each evaporator is connected with an evaporation completion liquid tank through a pipeline; the evaporation completion liquid tank is connected with the centrifuge; the centrifugal mother liquor outlet of the centrifugal machine is connected with a centrifugal mother liquor backflow inlet of the evaporator through a pipeline, the soda ash outlet of the centrifugal machine is connected with an inlet of the soda ash material conveying device through a pipeline, and an outlet of the soda ash material conveying device is connected with the drying device through a pipeline.
Preferably, a neutralization tower buffer tank is connected between the neutralization tower and the evaporator, and a material reflux outlet of the neutralization tower buffer tank is respectively connected with a caustic soda inlet of the neutralization tower and an inlet of the flash tank through pipelines; and a condensate outlet of the flash tank is connected with a material reflux inlet of the neutralization tower through a pipeline.
Preferably, a pipeline mixer is arranged on the caustic soda pipeline, and a material reflux outlet of the neutralizing tower buffer tank is connected with an inlet of the pipeline mixer through a pipeline.
Preferably, the steam outlet of the flash tank is connected with the steam inlet of the condenser through a pipeline; the soda material conveying device adopts a spiral feeder; the drying device adopts a drying bed.
Preferably, the caustic soda inlet of the neutralization tower is positioned at the upper part of the neutralization tower, and the carbon dioxide gas inlet is positioned at the top of the neutralization tower.
Preferably, a centrifugal mother liquor tank is connected between the centrifugal machine and the evaporator.
Preferably, the evaporator is a forced circulation evaporator.
On the other hand, the utility model also provides a process for producing soda by utilizing the production system, the caustic soda and carbon dioxide gas react in the neutralization tower, and the product generated by the reaction is pumped to a plurality of evaporators for evaporation; the evaporated evaporation completion liquid is pumped into an evaporation completion liquid tank and enters a centrifuge for centrifugation; the centrifuged mother liquor is pumped back to the evaporator, and the centrifuged soda ash is conveyed to a drying device for drying.
Preferably, part of the product generated in the neutralization tower is pumped into a pipeline mixer and enters the neutralization tower together with the caustic soda, part of the product enters a flash tank for flash evaporation, and the condensate after flash evaporation flows back to the neutralization tower.
Preferably, the caustic soda concentration is 10 to 50%.
Preferably, the pH value of the discharge of the neutralization tower is controlled to be 11-14 through the feeding amount of caustic soda, so that the byproduct NaHCO can be reduced 3 And (4) generating.
Preferably, the flash tank flashes water out of the product of the neutralization tower, reaction heat is taken away by vaporization of the water, and the reaction temperature in the neutralization tower is controlled to be 40-70 ℃ by the circulation amount of the product of the neutralization tower into the flash tank, and the reaction pressure is controlled to be normal pressure to 50 kPaG.
Preferably, the caustic soda and the carbon dioxide gas flow into the neutralization tower in a concurrent flow mode, flooding cannot occur due to the adoption of the concurrent flow operation, the gas-liquid flux can be greatly improved, and the pH value is easier to control.
The production principle of the utility model is that caustic soda reacts with carbon dioxide gas:
2NaOH+CO 2 ＝Na 2 CO 3 +H 2 O
Na 2 CO 3 +CO 2 +H 2 O＝2NaHCO 3
NaOH+NaHCO 3 ＝Na 2 CO 3 +H 2 O
2NaOH+SO 2 ＝Na 2 SO 3 +H 2 O
excess carbon dioxide is generated to sodium bicarbonate; sodium hydroxide is in excess to produce sodium carbonate.
Compared with the prior art, the utility model, following beneficial effect has:
the utility model provides a brand-new soda production system, which does not have the problem of ammonia evaporation waste liquid of an ammonia-soda process, and also does not need to construct a set of synthetic ammonia device in a matching way of a combined soda process, thereby greatly reducing the investment, the occupied area and the like. Simultaneously the utility model discloses a technology has still reduced carbon and has subtracted discharge capacity, can effectively promote the environmental protection of economic society and change and systematic deep and profound transformation.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure, 1-neutralization tower, 2-evaporator, 201-evaporation chamber, 202-heating chamber, 3-evaporation completion liquid tank, 4-centrifuge, 5-spiral feeder, 6-drying bed, 7-neutralization tower buffer tank, 8-flash tank, 9-pipeline mixer, 10-condenser, 11-centrifugal mother liquid tank, 12-vacuum pump, 13-blower, 14-air filter, 15-drying blower, 16-air heater and 17-water seal tank.
Detailed Description
As shown in fig. 1, the soda production system of the utility model comprises a neutralization tower 1, a caustic soda inlet at the upper part of the neutralization tower 1 is connected with a caustic soda pipeline, and a pipeline mixer 9 is arranged on the caustic soda pipeline; the carbon dioxide gas inlet at the top of the neutralization tower 1 is connected with a carbon dioxide gas line. A discharge port of the neutralization tower 1 is respectively connected with feed ports of a plurality of (four shown in figure 1) evaporators 2 through pipelines, a neutralization tower buffer tank 7 is also connected between the neutralization tower 1 and the evaporators 2, and a material reflux outlet of the neutralization tower buffer tank 7 is respectively connected with an inlet of a pipeline mixer 9 and an inlet of a flash tank 8 through pipelines; a condensate outlet of the flash tank 8 is connected with a material reflux inlet of the neutralization tower 1 through a pipeline; the material reflux outlet of the neutralization tower buffer tank 7 is connected with the inlet of the pipeline mixer 9 through a pipeline. An evaporation completion liquid outlet of the evaporator 2 is connected with an evaporation completion liquid tank 3 through a pipeline; the evaporation completion liquid tank 3 is connected with a centrifuge 4; the centrifugal mother liquor outlet of the centrifuge 4 is connected with the centrifugal mother liquor reflux inlet of the evaporator 2 through a pipeline. A centrifugal mother liquor tank 11 is connected between the centrifugal machine 4 and the evaporator 2; the outlet of the centrifuge 4 is connected with the inlet of the soda material conveying device through a pipeline, and the outlet of the soda material conveying device is connected with the drying device through a pipeline. Wherein the conveying device of the calcined soda materials can adopt a screw feeder 5. The drying device can adopt a drying bed 6, and high-temperature air is conveyed into the drying bed 6 through an air filter 14, a drying blower 15 and an air heater 16 to dry the soda. The steam outlet of the flash tank 8 is connected with the steam inlet of a condenser 10 through a pipeline, the condenser 10 can adopt various forms, and fig. 1 shows a vacuum condensation mode by using a vacuum pump 12. The condensate of the condenser 10 is discharged through the water seal tank 17.
The carbon dioxide gas in the present invention may be exhaust gas or gas from a boiler, a coal chemical industry, a petrochemical industry, etc. containing carbon dioxide gas, but is not limited thereto.
The working principle is as follows:
flue gas after desulfurization and denitrification treatment of boiler tail gas enters the top of the neutralization tower 1 through a blower 13, caustic soda with the concentration of 10-50% from a caustic soda device is pumped to the upper part of the neutralization tower 1 and is mixed through a pipeline mixer 9, and the flue gas and the caustic soda are reacted in parallel flow in the neutralization tower 1.
The carbon neutralization reaction liquid generated by the reaction of the neutralization tower 1 is buffered by a neutralization tower buffer tank 7, part of the carbon neutralization reaction liquid is pumped to the evaporator 2, part of the carbon neutralization reaction liquid is pumped to a pipeline mixer 9 and enters the neutralization tower 1 together with the caustic soda raw material to participate in the carbon neutralization reaction, the other part of the carbon neutralization reaction liquid enters a flash evaporation tank 8 to be flashed, the liquid material returns to the neutralization tower 1, and the steam is vaporized by the flash evaporation tankThe condenser 10 is discharged after condensation treatment. The evaporation process can adopt single-effect or multi-effect evaporation, and the multi-effect evaporation can adopt two to six effects; the multi-effect evaporation mode can adopt a plurality of modes such as parallel connection or series connection. The utility model discloses the preferred parallelly connected evaporimeter of four effects that adopts, four effect evaporimeters adopt the reinforced evaporation flow of advection, and the heating steam flow direction flows to last effect evaporimeter by first effect evaporimeter, and the feed liquid then is every to imitate business turn over alone. The steam discharged by the fourth effect evaporator is condensed by a condenser 10 and then discharged, the condensing mode can adopt various modes, and fig. 1 shows a vacuum condensing mode by a vacuum pump 12; the condensate of the condenser 10 is discharged through the water-sealed tank 17. Wherein the temperature of a heating chamber of the first-effect evaporator is 110-150 ℃, and the steam pressure is 0.1-0.6 MpaG; the temperature of an evaporation chamber of the fourth-effect evaporator is 50-90 ℃, and the steam pressure is-0.05-0.09 MpaG. Absorbing CO by caustic soda 2 In order to perform exothermic reaction, the problems of easy blockage and easy scaling of the sodium carbonate are considered, and the problems of easy blockage and easy scaling are solved by adopting the external flash tank 8 instead of a heat exchanger for heat transfer. The evaporator 2 can adopt forced circulation or non-forced circulation, and the forced circulation evaporator is preferred in the utility model.
Buffering the evaporation completion liquid with the solid content of 20-60% by an evaporation completion liquid tank 3, then centrifuging by a centrifuge 4, buffering the centrifugal mother liquid by a centrifugal mother liquid tank 11, pumping one part of the centrifugal mother liquid to an evaporator 2, and returning the other part of the centrifugal mother liquid to the neutralization tower 1; and (4) drying and packaging the sodium carbonate with the water content less than or equal to 4% after centrifugation to obtain a qualified product.
The pH value of the discharge of the neutralization tower 1 is 11 to 14 in the feeding amount control of caustic soda to reduce the byproduct NaHCO 3 And (4) generating. The reaction temperature in the neutralization column 1 is controlled to 40-70 ℃ by the amount of product circulated into the flash tank 8.
Although the present invention has been described in detail by referring to the drawings in conjunction with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and substance of the present invention, and these modifications or substitutions are intended to be within the scope of the present invention/any person skilled in the art can easily conceive of changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (6)
1. A soda production system is characterized by comprising a neutralization tower (1), wherein a caustic soda inlet of the neutralization tower (1) is connected with a caustic soda pipeline, and a carbon dioxide gas inlet of the neutralization tower (1) is connected with a carbon dioxide gas pipeline; a discharge port of the neutralization tower (1) is respectively connected with feed ports of a plurality of evaporators (2) through pipelines, and evaporation completion liquid outlets of the evaporators (2) are connected with evaporation completion liquid tanks (3) through pipelines; the evaporation completion liquid tank (3) is connected with a centrifugal machine (4); a centrifugal mother liquor outlet of the centrifugal machine (4) is connected with a centrifugal mother liquor backflow inlet of the evaporator (2) through a pipeline, a soda ash outlet of the centrifugal machine (4) is connected with an inlet of a soda ash material conveying device through a pipeline, and an outlet of the soda ash material conveying device is connected with a drying device through a pipeline.
2. The soda production system according to claim 1, wherein a neutralization tower buffer tank (7) is connected between the neutralization tower (1) and the evaporator (2), and a material reflux outlet of the neutralization tower buffer tank (7) is respectively connected with a caustic soda inlet of the neutralization tower (1) and an inlet of the flash tank (8) through pipelines; a condensate outlet of the flash tank (8) is connected with a material reflux inlet of the neutralization tower (1) through a pipeline.
3. Soda production system according to claim 2, characterised in that a pipeline mixer (9) is arranged on the soda line, and the material return outlet of the neutralisation column buffer tank (7) is connected to the inlet of the pipeline mixer (9) by a pipeline.
4. Soda production system according to claim 1, characterized in that the caustic soda inlet of the neutralization tower (1) is located in the upper part of the neutralization tower (1) and the carbon dioxide gas inlet is located at the top of the neutralization tower (1).
5. Soda production system according to claim 1, characterised in that a mother liquor tank (11) for centrifugation is also connected between the centrifuge (4) and the evaporator (2).
6. Soda production system according to claim 1, characterised in that the evaporator (2) is a forced circulation evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220910753.6U CN217398466U (en) | 2022-04-19 | 2022-04-19 | Soda production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220910753.6U CN217398466U (en) | 2022-04-19 | 2022-04-19 | Soda production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217398466U true CN217398466U (en) | 2022-09-09 |
Family
ID=83142555
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220910753.6U Active CN217398466U (en) | 2022-04-19 | 2022-04-19 | Soda production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217398466U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114560479A (en) * | 2022-04-19 | 2022-05-31 | 山东凯泰科技股份有限公司 | Sodium carbonate production system and production process thereof |
-
2022
- 2022-04-19 CN CN202220910753.6U patent/CN217398466U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114560479A (en) * | 2022-04-19 | 2022-05-31 | 山东凯泰科技股份有限公司 | Sodium carbonate production system and production process thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111701419B (en) | Sodium-alkali dry-method desulfurized fly ash recycling method | |
| CN102145912B (en) | Process for preparing calcium chloride solution by utilizing ammonia soda filtration mother liquor | |
| CN108046295A (en) | The method that sodium acid carbonate and ammonium sulfate are produced with metabisulfite solution | |
| CN217398466U (en) | Soda production system | |
| CN108726542A (en) | The production method and production equipment of sodium bicarbonate | |
| CN102515112B (en) | Method for preparing sodium sulfide from hydrogen sulfide waste gas produced in production of viscose fibre | |
| CN109809437A (en) | Novel energy-saving environment-friendly heavy soda ash production technology and system | |
| CN100556811C (en) | A kind of production method of low-salt dense soda ash and the system that produces low-salt dense soda ash thereof | |
| CN107162034B (en) | A kind of system and technique preparing nano-calcium carbonate and amino compound fertilizer using the coal chemical industry three wastes | |
| CN114560479A (en) | Sodium carbonate production system and production process thereof | |
| CN207498073U (en) | Novel energy-saving environment-friendly heavy soda ash production system | |
| CN109928408A (en) | The method and system of ammonia is recycled from potassium nitrate process by-product ammonium chloride | |
| CN102515210B (en) | Method for producing potassium bicarbonate through self-carbonization multiple-effect cross flow continues evaporation crystallization | |
| CN108217690A (en) | A kind of technique that secondary salt is extracted from desulfurization waste liquor | |
| CN101780961B (en) | Energy saving, consumption reduction and high efficiency process for manufacturing borax with carbon alkaline method | |
| CN214456896U (en) | Waste water treatment and recovery device in PTA (pure terephthalic acid) production industry | |
| CN102079550B (en) | Waste saline purification technique | |
| CN102295376A (en) | Recycling treatment method for lignin production wastewater | |
| CN110980765A (en) | Process for preparing ammonium chloride | |
| CN214528165U (en) | Novel three-section ammonia distillation system for ammonia distillation by using light calcined powder | |
| CN215876285U (en) | Negative pressure distillation system | |
| CN100436322C (en) | Sodium carbonate preparing process | |
| CN103935971A (en) | Green cycle production novel method of hydrazine hydrate, hydrazonium salts, and ADC foaming agent | |
| CN110697814A (en) | Ammonia-containing sulfate wastewater treatment system and process | |
| CN220034104U (en) | Continuous cooling crystallization ammonium chloride separation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: Room 1701, No. 28 Longcheng Road, Shibei District, Qingdao City, Shandong Province, 266000 Patentee after: Shandong Jierui Kaitai Technology Co.,Ltd. Country or region after: China Address before: 266034 room 701, floor 7, building 3, Yangui hall, No. 17, Kunshan Road, Shibei District, Qingdao, Shandong Patentee before: SHANDONG KAITAI TECHNOLOGY Co.,Ltd. Country or region before: China |
|
| CP03 | Change of name, title or address |