CN220951197U - System for preparing caustic soda by recycling natural alkali tail liquid - Google Patents
System for preparing caustic soda by recycling natural alkali tail liquid Download PDFInfo
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- CN220951197U CN220951197U CN202322788421.2U CN202322788421U CN220951197U CN 220951197 U CN220951197 U CN 220951197U CN 202322788421 U CN202322788421 U CN 202322788421U CN 220951197 U CN220951197 U CN 220951197U
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 title claims abstract description 138
- 239000007788 liquid Substances 0.000 title claims abstract description 67
- 239000003513 alkali Substances 0.000 title claims abstract description 46
- 235000011121 sodium hydroxide Nutrition 0.000 title claims abstract description 46
- 238000004064 recycling Methods 0.000 title claims abstract description 13
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 78
- 239000012267 brine Substances 0.000 claims abstract description 77
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000000460 chlorine Substances 0.000 claims abstract description 52
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 52
- 229920001429 chelating resin Polymers 0.000 claims abstract description 48
- 238000010521 absorption reaction Methods 0.000 claims abstract description 43
- 150000003839 salts Chemical class 0.000 claims abstract description 41
- 238000004519 manufacturing process Methods 0.000 claims abstract description 32
- 239000001257 hydrogen Substances 0.000 claims abstract description 29
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 29
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 24
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 24
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 22
- 238000000746 purification Methods 0.000 claims abstract description 14
- 241001625808 Trona Species 0.000 claims abstract description 12
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 12
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 29
- 238000001035 drying Methods 0.000 claims description 22
- 238000005406 washing Methods 0.000 claims description 22
- 238000006298 dechlorination reaction Methods 0.000 claims description 21
- 239000012452 mother liquor Substances 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 10
- 239000012528 membrane Substances 0.000 claims description 10
- 229910002651 NO3 Inorganic materials 0.000 claims description 9
- 238000007670 refining Methods 0.000 claims description 9
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 8
- 239000002994 raw material Substances 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000010354 integration Effects 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 12
- 239000000243 solution Substances 0.000 description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 description 6
- 239000011780 sodium chloride Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 4
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000009993 causticizing Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000003843 chloralkali process Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 150000004691 decahydrates Chemical class 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a system for preparing caustic soda by recycling natural alkali tail liquid, which comprises a tail liquid treatment unit, a brine purification unit and a chlor-alkali production unit; the liquid inlet of the absorption reaction device of the tail liquid treatment unit is connected with a trona liquid inlet pipe, the outlet of the salt dissolving barrel of the tail liquid treatment unit is connected with the inlet pipeline of the brine pretreatment device of the brine purification unit, the outlet of the chelating resin tower group of the brine purification unit is connected with the inlet pipeline of the anode chamber of the electrolytic tank of the chlor-alkali production unit, and the outlet of the hydrogen chloride synthesis furnace of the chlor-alkali production unit is connected with the air inlet pipeline of the absorption reaction device of the tail liquid treatment unit. The utility model has the advantages that: the whole system takes chlorine as a balance element, and is recycled in the system to prepare caustic soda, and hydrogen, chlorine and salt generated by the chlor-alkali production unit and the tail liquid treatment unit are mutually used as raw materials, so that the production process of the integration of the production of the trona and the chemical circulation of the chlor-alkali is realized, and the zero emission, the environmental protection and the energy conservation are basically realized.
Description
Technical Field
The utility model relates to the technical field of caustic soda, in particular to a system for preparing caustic soda by recycling a tail liquid of natural caustic soda.
Background
The natural alkali tail liquid is the enriched high-salt brine produced by the natural alkali-to-sodium carbonate process system in a circulating way, the quality of the sodium carbonate product is ensured by quantitative discharge, the foreign traditional natural alkali tail liquid treatment is the piling of a construction mother liquor pond, and the tail liquid is used for producing high salt alkali or used for desulfurization in China. The tail liquid is used as desulfurizing agent, and is limited by the use amount and low in use of higher resources. And the produced high-salt alkali and industrial salt has high impurity content, poor market acceptance and poor economic benefit.
The chlor-alkali process for preparing caustic soda is a method for preparing caustic soda by using an electrolysis saturated salt water solution, and has the problems that subsidiary products of hydrogen and chlorine are difficult to treat due to explosion and toxicity, investment, storage and transportation costs are high, the downstream product market is saturated, and the added value is low.
The caustic soda tail liquid can also be prepared by a causticizing method, sodium carbonate and sodium bicarbonate in the tail liquid are utilized to react with lime to produce caustic soda, the caustic soda produced by the process has low concentration, and waste water and waste residue produced by the process are difficult to treat.
Disclosure of utility model
The utility model aims to provide a system for preparing caustic soda by recycling a natural alkali tail liquid.
The utility model is implemented by the following technical scheme: the system for preparing caustic soda by recycling the tail liquid of the trona comprises a tail liquid treatment unit, a brine purification unit and a chlor-alkali production unit;
The liquid inlet of the absorption reaction device of the tail liquid treatment unit is connected with a trona liquid inlet pipe, the outlet of the salt dissolving barrel of the tail liquid treatment unit is connected with the inlet pipeline of the brine pretreatment device of the brine purification unit, the outlet of the chelating resin tower group of the brine purification unit is connected with the inlet pipeline of the anode chamber of the electrolytic tank of the chlor-alkali production unit, and the outlet of the chlor-alkali production unit is connected with the inlet pipeline of the absorption reaction device of the tail liquid treatment unit.
Further, the tail liquid treatment unit comprises an absorption reaction device, a decahydrobase crystallizer, a decahydrobase filter, a denitration salt-making mother liquor barrel, a salt-making crystallizer, a salt filter and a salt-dissolving barrel;
The liquid outlet of the absorption reaction device is connected with an inlet pipeline of the decahydroalkali crystallizer, an outlet of the decahydroalkali crystallizer is connected with an inlet pipeline of a decahydroalkali filter, an outlet of the decahydroalkali filter is connected with an inlet pipeline of a denitration salt-making mother liquor barrel, an outlet of the denitration salt-making mother liquor barrel is connected with an inlet pipeline of the salt-making crystallizer, an outlet of the salt-making crystallizer is connected with an inlet pipeline of a salt filter, and an outlet of the salt filter is connected with an inlet pipeline of the salt-making barrel.
Further, the absorption reaction device of the tail liquid treatment unit comprises a first absorption reactor, a first mother liquid barrel, a second absorption reactor and a second mother liquid barrel which are sequentially connected in series, wherein the air inlets of the first absorption reactor and the second absorption reactor are respectively connected with an outlet pipeline of a hydrogen chloride synthesis furnace of the chlor-alkali production unit, and the air outlets of the first absorption reactor and the second absorption reactor are connected with a tail gas treatment pipeline.
Further, the brine purifying unit comprises a brine preprocessor, a brine refining filter, a refined brine bucket and a chelating resin tower group;
The outlet of the brine pretreatment device is connected with the inlet pipeline of the brine refined filter, the outlet of the brine refined filter is connected with the inlet pipeline of the refined brine barrel, and the outlet of the refined brine barrel is connected with the inlet pipeline of the chelating resin tower group.
Further, the chelating resin tower group comprises a first chelating resin tower, a second chelating resin tower and a third chelating resin tower, wherein the first chelating resin tower, the second chelating resin tower and the third chelating resin tower are connected in parallel, and a switching pipeline is respectively connected between an outlet of the first chelating resin tower and an inlet of the second chelating resin tower, an outlet of the second chelating resin tower and an inlet of the third chelating resin tower.
Further, the brine purifying unit also comprises a dechlorination tower, a dechlorination fresh-salt water barrel and a membrane type denitration device;
The export of the fresh salt cask of chlor-alkali production unit with the entry pipeline connection of dechlorination tower, the export of dechlorination tower with the entry pipeline connection of dechlorination fresh salt cask, the export of dechlorination fresh salt cask with the entry pipeline connection of diaphragm type denitrification facility, the lean nitrate water export of diaphragm type denitrification facility with salt dissolving bucket pipeline connection, the rich nitrate water export of diaphragm type denitrification facility is connected with the entry pipeline of second mother liquor bucket.
Further, the chlor-alkali production unit comprises an electrolytic tank, a dilute salt water barrel, a caustic soda barrel, a hydrogen washing tower, a hydrogen compressor, a chlorine washing tower, a first chlorine drying tower, a second chlorine drying tower, a chlorine compressor and a hydrogen chloride synthetic furnace;
The anode chamber liquid outlet of the electrolytic tank is connected with the inlet pipeline of the dilute brine bucket, the cathode chamber liquid outlet of the electrolytic tank is connected with the inlet pipeline of the caustic soda bucket, the outlet of the caustic soda bucket is respectively connected with the cathode chamber inlet of the electrolytic tank and the sodium hydroxide delivery pipeline through pipelines, the chlorine outlet of the electrolytic tank is connected with the inlet pipeline of the chlorine washing tower, the outlet of the chlorine washing tower is connected with the inlet pipeline of the first chlorine drying tower, the outlet of the first chlorine drying tower is connected with the inlet pipeline of the second chlorine drying tower, the outlet of the second chlorine drying tower is connected with the inlet pipeline of the chlorine compressor, and the outlet of the chlorine compressor is connected with the inlet pipeline of the hydrogen chloride synthesis furnace;
The hydrogen outlet of the electrolytic tank is connected with the inlet pipeline of the hydrogen washing tower, the outlet of the hydrogen washing tower is connected with the inlet pipeline of the hydrogen compressor, and the outlet of the hydrogen compressor is connected with the inlet pipeline of the hydrogen chloride synthetic furnace.
The utility model has the advantages that: the salt produced by evaporating the natural alkali tail liquid through the tail liquid treatment unit can be used as the raw material of the chlor-alkali production unit to produce caustic soda, and the caustic soda is sent to a soda device for production; after the hydrogen and the chlorine which are generated by the chlor-alkali production unit are respectively treated, hydrogen chloride is produced in the synthesis furnace and is sent to the absorption reaction device, the tail solution of the trona is used as an absorbent, sodium carbonate in the alkali liquor is converted into sodium chloride along with the conversion reaction when the hydrogen chloride is absorbed, and the sodium chloride can be recycled as a main raw material of chlor-alkali;
The whole system takes chlorine as a balance element, and is recycled in the system to prepare caustic soda, and hydrogen, chlorine and salt generated by a chlor-alkali production unit and a tail liquid treatment unit are mutually used as raw materials, so that resources are fully and reasonably utilized, the production process of the integration of the production of natural alkali and the chemical circulation of chlor-alkali is realized, zero emission is basically realized, and the system is environment-friendly and energy-saving;
Chlorine in the natural alkali tail liquid is separated out in the form of sodium chloride, and sodium chloride is produced after salt is dissolved again after filtering treatment.
Drawings
In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the structure of the utility model;
FIG. 2 is a schematic diagram of a tail fluid treatment unit according to the present utility model;
FIG. 3 is a schematic diagram of a brine purification unit according to the present utility model;
FIG. 4 is a schematic diagram of a chlor-alkali production unit in the utility model;
In the figure: the device comprises a tail liquid treatment unit 1, an absorption reaction device 1.1, a first absorption reactor 1.1.1, a first mother liquor barrel 1.1.2, a second absorption reactor 1.1.3, a second mother liquor barrel 1.1.4, a tail gas treatment pipeline 1.1.5, a decahydrobase crystallizer 1.2, a decahydrobase filter 1.3, a denitration salt-making mother liquor barrel 1.4, a salt-making crystallizer 1.5, a salt filter 1.6, a salt-making barrel 1.7 and a trona feed liquor pipe 1.8;
A brine purifying unit 2, a brine preprocessor 2.1, a brine refining filter 2.2, a refined brine barrel 2.3, a chelating resin tower group 2.4, a first chelating resin tower 2.4.1, a second chelating resin tower 2.4.2, a third chelating resin tower 2.4.3, a switching pipeline 2.4.5, a dechlorination tower 2.5, a dechlorination light brine barrel 2.6 and a membrane type denitration device 2.7;
The device comprises a chlor-alkali production unit 3, an electrolytic tank 3.1, a dilute brine barrel 3.2, a caustic soda barrel 3.3, a hydrogen washing tower 3.4, a hydrogen compressor 3.5, a chlorine washing tower 3.6, a first chlorine drying tower 3.7, a second chlorine drying tower 3.8, a chlorine compressor 3.9, a hydrogen chloride synthesis furnace 3.10 and a sodium hydroxide delivery pipeline 3.11.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
As shown in fig. 1-3, the system for preparing caustic soda by recycling the tail liquid of natural alkali comprises a tail liquid treatment unit 1, a brine purification unit 2 and a chlor-alkali production unit 3;
The liquid inlet of the absorption reaction device 1.1 of the tail liquid treatment unit 1 is connected with a trona liquid inlet pipe 1.8, the outlet of a salt dissolving barrel 1.7 of the tail liquid treatment unit 1 is connected with an inlet pipeline of a brine pretreatment device 2.1 of a brine purification unit 2, the outlet of a chelating resin tower group 2.4 of the brine purification unit 2 is connected with an anode chamber inlet pipeline of an electrolytic tank 3.1 of a chlor-alkali production unit 3, and the outlet of a hydrogen chloride synthetic furnace 3.10 of the chlor-alkali production unit 3 is connected with an air inlet pipeline of the absorption reaction device 1.1 of the tail liquid treatment unit 1.
The tail liquid treatment unit 1 comprises an absorption reaction device 1.1, a decahydroalkali crystallizer 1.2, a decahydroalkali filter 1.3, a denitration salt-making mother liquor barrel 1.4, a salt-making crystallizer 1.5, a salt filter 1.6 and a salt-dissolving barrel 1.7;
The liquid outlet of the absorption reaction device 1.1 is connected with an inlet pipeline of a decahydroalkali crystallizer 1.2, the outlet of the decahydroalkali crystallizer 1.2 is connected with an inlet pipeline of a decahydroalkali filter 1.3, the outlet of the decahydroalkali filter 1.3 is connected with an inlet pipeline of a denitration salt-making mother liquor barrel 1.4, the outlet of the denitration salt-making mother liquor barrel 1.4 is connected with an inlet pipeline of a salt-making crystallizer 1.5, the outlet of the salt-making crystallizer 1.5 is connected with an inlet pipeline of a salt filter 1.6, and the outlet of the salt filter 1.6 is connected with an inlet pipeline of a salt-making barrel 1.7.
The absorption reaction device 1.1 of the tail liquid treatment unit 1 comprises a first absorption reactor 1.1.1, a first mother liquor barrel 1.1.2, a second absorption reactor 1.1.3 and a second mother liquor barrel 1.1.4 which are sequentially connected in series, wherein air inlets of the first absorption reactor 1.1.1 and the second absorption reactor 1.1.3 are respectively connected with an outlet pipeline of a hydrogen chloride synthesis furnace 3.10 of the chlor-alkali production unit 3, and air outlets of the first absorption reactor 1.1.1 and the second absorption reactor 1.1.3 are connected with the tail gas treatment pipeline 1.1.5.
The brine purifying unit 2 comprises a brine preprocessor 2.1, a brine refining filter 2.2, a refined brine barrel 2.3 and a chelating resin tower group 2.4;
The outlet of the brine preprocessor 2.1 is connected with the inlet pipeline of the brine refining filter 2.2, the outlet of the brine refining filter 2.2 is connected with the inlet pipeline of the refined brine barrel 2.3, and the outlet of the refined brine barrel 2.3 is connected with the inlet pipeline of the chelating resin tower group 2.4.
The chelating resin tower set 2.4 comprises a first chelating resin tower 2.4.1, a second chelating resin tower 2.4.2 and a third chelating resin tower 2.4.3, wherein the first chelating resin tower 2.4.1, the second chelating resin tower 2.4.2 and the third chelating resin tower 2.4.3 are connected in parallel, and a switching pipeline 2.4.5 is respectively connected between an outlet of the first chelating resin tower 2.4.1 and an inlet of the second chelating resin tower 2.4.2, and between an outlet of the second chelating resin tower 2.4.2 and an inlet of the third chelating resin tower 2.4.3.
The brine purifying unit 2 also comprises a dechlorination tower 2.5, a dechlorination light brine barrel 2.6 and a membrane type denitration device 2.7;
The outlet of the dilute brine barrel 3.2 of the chlor-alkali production unit 3 is connected with the inlet pipeline of the dechlorination tower 2.5, the outlet of the dechlorination tower 2.5 is connected with the inlet pipeline of the dechlorination dilute brine barrel 2.6, the outlet of the dechlorination dilute brine barrel 2.6 is connected with the inlet pipeline of the membrane type denitrification device 2.7, the lean nitrate brine outlet of the membrane type denitrification device 2.7 is connected with the pipeline of the salt dissolving barrel 1.7, and the rich nitrate brine outlet of the membrane type denitrification device 2.7 is connected with the inlet pipeline of the second mother liquor barrel 1.1.4.
The chlor-alkali production unit 3 comprises an electrolytic tank 3.1, a dilute brine barrel 3.2, a caustic soda barrel 3.3, a hydrogen gas washing tower 3.4, a hydrogen gas compressor 3.5, a chlorine gas washing tower 3.6, a first chlorine gas drying tower 3.7, a second chlorine gas drying tower 3.8, a chlorine gas compressor 3.9 and a hydrogen chloride synthesis furnace 3.10;
The outlet of the anode chamber of the electrolytic tank 3.1 is connected with the inlet pipeline of the dilute brine barrel 3.2, the outlet of the cathode chamber of the electrolytic tank 3.1 is connected with the inlet pipeline of the caustic soda barrel 3.3, the outlet of the caustic soda barrel 3.3 is respectively connected with the inlet of the cathode chamber of the electrolytic tank 3.1 and the sodium hydroxide delivery pipeline 3.11 through pipelines, the chlorine outlet of the electrolytic tank 3.1 is connected with the inlet pipeline of the chlorine washing tower 3.6, the outlet of the chlorine washing tower 3.6 is connected with the inlet pipeline of the first chlorine drying tower 3.7, the outlet of the first chlorine drying tower 3.7 is connected with the inlet pipeline of the second chlorine drying tower 3.8, the outlet of the second chlorine drying tower 3.8 is connected with the inlet pipeline of the chlorine compressor 3.9, and the outlet of the chlorine compressor 3.9 is connected with the inlet pipeline of the hydrogen chloride synthesis furnace 3.10;
The hydrogen outlet of the electrolytic tank 3.1 is connected with the inlet pipeline of the hydrogen washing tower 3.4, the outlet of the hydrogen washing tower 3.4 is connected with the inlet pipeline of the hydrogen compressor 3.5, and the outlet of the hydrogen compressor 3.5 is connected with the inlet pipeline of the hydrogen chloride synthetic furnace 3.10.
The specific operation of this example;
The discharged tail liquid (mainly sodium carbonate, sodium chloride and sodium sulfate) of the trona device is firstly sent to a first absorption reactor 1.1.1 and a second absorption reactor 1.1.3 to react with hydrogen chloride gas sent by a hydrogen chloride synthesis furnace 3.10, the hydrogen chloride gas is firstly dissolved in water to generate hydrochloric acid and then reacts with sodium carbonate in the solution to generate sodium chloride solution and carbon dioxide gas, the discharged carbon dioxide gas is sent to a carbonization tower of the trona device to produce baking soda through a tail gas treatment pipeline 1.1.5, the salt-nitrate solution at the bottom of the tower is sent to a decahydrate crystallizer 1.2, the high-salt mother liquid after the denitration is circularly frozen and denitrated, and then sent to a salt-making crystallizer 1.5 through pumping, salt is circularly evaporated and crystallized at high temperature, salt separated out from salt legs of the crystallizer is sent to a salt filter 1.6 for dehydration after being washed by brine, and wet salt is sent to a salt dissolving bucket 1.7;
The salt dissolving barrel 1.7 is pumped to a brine pretreatment device and a brine refining filter 2.2 for primary brine refining to remove impurities such as calcium, magnesium, free chlorine, organic matters and the like in crude brine, and then the crude brine is pumped to a chelating resin tower group for secondary brine refining to further remove trace cations in the brine so as to reduce the influence of ions on the membrane of the electrolytic tank 3.1;
The refined brine is pumped into a brine overhead tank of an electrolytic tank 3.1 and then flows into an anode chamber of the electrolytic tank 3.1 to carry out electrolytic reaction, 32% caustic soda (NaOH) solution generated by electrolysis is sent into a caustic soda bucket 3.3, one part of the caustic soda solution is sent into a natural caustic soda device for self-use through a sodium hydroxide external delivery pipeline 3.11, and the other part of the caustic soda solution is returned into a cathode chamber of the electrolytic tank 3.1 after being mixed with a small amount of pure water and circulated in the system;
The hydrogen generated in the cathode chamber of the electrolytic tank 3.1 is treated by a hydrogen washing tower 3.4 and then is sent to a hydrogen compressor, the chlorine generated in the anode chamber is treated by a chlorine washing tower 3.6, a first drying tower and a second drying tower and then is sent to a chlorine compressor 3.9, the compressed hydrogen and chlorine enter a hydrogen chloride synthesizing furnace 3.10 to synthesize hydrogen chloride gas at high temperature, and then are sent to a first absorption reactor 1.1.1 and a second absorption reactor 1.1.3;
The dilute brine produced by the electrolytic tank 3.1 enters a dechlorination tower 2.5, free chlorine is removed in vacuum, the lean nitrate brine treated by the membrane type denitration device is sent into a salt dissolving bucket 1.7 to produce saturated brine, and the rich nitrate brine treated by the membrane type denitration device is sent into a second mother liquor bucket 1.1.4.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (7)
1. The system for preparing caustic soda by recycling the tail liquid of the trona is characterized by comprising a tail liquid treatment unit, a brine purification unit and a chlor-alkali production unit;
The liquid inlet of the absorption reaction device of the tail liquid treatment unit is connected with a trona liquid inlet pipe, the outlet of the salt dissolving barrel of the tail liquid treatment unit is connected with the inlet pipeline of the brine pretreatment device of the brine purification unit, the outlet of the chelating resin tower group of the brine purification unit is connected with the inlet pipeline of the anode chamber of the electrolytic tank of the chlor-alkali production unit, and the outlet of the chlor-alkali production unit is connected with the inlet pipeline of the absorption reaction device of the tail liquid treatment unit.
2. The system for preparing caustic soda by recycling the tail liquid of the trona according to claim 1, wherein the tail liquid treatment unit comprises an absorption reaction device, a decahydrobase crystallizer, a decahydrobase filter, a denitration salt-making mother liquor barrel, a salt-making crystallizer, a salt filter and a salt-dissolving barrel;
The liquid outlet of the absorption reaction device is connected with an inlet pipeline of the decahydroalkali crystallizer, an outlet of the decahydroalkali crystallizer is connected with an inlet pipeline of a decahydroalkali filter, an outlet of the decahydroalkali filter is connected with an inlet pipeline of a denitration salt-making mother liquor barrel, an outlet of the denitration salt-making mother liquor barrel is connected with an inlet pipeline of the salt-making crystallizer, an outlet of the salt-making crystallizer is connected with an inlet pipeline of a salt filter, and an outlet of the salt filter is connected with an inlet pipeline of the salt-making barrel.
3. The system for preparing caustic soda by recycling natural alkali tail liquid according to claim 2, wherein the absorption reaction device of the tail liquid treatment unit comprises a first absorption reactor, a first mother liquid barrel, a second absorption reactor and a second mother liquid barrel which are sequentially connected in series, air inlets of the first absorption reactor and the second absorption reactor are respectively connected with an outlet pipeline of a hydrogen chloride synthesis furnace of the chlor-alkali production unit, and air outlets of the first absorption reactor and the second absorption reactor are connected with a tail gas treatment pipeline.
4. The system for preparing caustic soda according to claim 1, wherein the brine purification unit comprises a brine pretreatment device, a brine refining filter, a refined brine barrel and a chelating resin tower group;
The outlet of the brine pretreatment device is connected with the inlet pipeline of the brine refined filter, the outlet of the brine refined filter is connected with the inlet pipeline of the refined brine barrel, and the outlet of the refined brine barrel is connected with the inlet pipeline of the chelating resin tower group.
5. The system for recycling and preparing caustic soda according to claim 4, wherein the chelating resin tower group comprises a first chelating resin tower, a second chelating resin tower and a third chelating resin tower, the first chelating resin tower, the second chelating resin tower and the third chelating resin tower are connected in parallel, and a switching pipeline is respectively connected between an outlet of the first chelating resin tower and an inlet of the second chelating resin tower, and between an outlet of the second chelating resin tower and an inlet of the third chelating resin tower.
6. The system for preparing caustic soda by recycling the tail liquid of natural alkali according to claim 4, wherein the brine purifying unit further comprises a dechlorination tower, a dechlorination light salt water barrel and a membrane type denitration device;
The export of the fresh salt cask of chlor-alkali production unit with the entry pipeline connection of dechlorination tower, the export of dechlorination tower with the entry pipeline connection of dechlorination fresh salt cask, the export of dechlorination fresh salt cask with the entry pipeline connection of diaphragm type denitrification facility, the lean nitrate water export of diaphragm type denitrification facility with salt dissolving bucket pipeline connection, the rich nitrate water export of diaphragm type denitrification facility is connected with the entry pipeline of second mother liquor bucket.
7. The system for preparing caustic soda by recycling the tail liquid of natural alkali according to claim 1, wherein the chlor-alkali production unit comprises an electrolytic tank, a fresh salt water barrel, a caustic soda barrel, a hydrogen washing tower, a hydrogen compressor, a chlorine washing tower, a first chlorine drying tower, a second chlorine drying tower, a chlorine compressor and a hydrogen chloride synthesis furnace;
The anode chamber liquid outlet of the electrolytic tank is connected with the inlet pipeline of the dilute brine bucket, the cathode chamber liquid outlet of the electrolytic tank is connected with the inlet pipeline of the caustic soda bucket, the outlet of the caustic soda bucket is respectively connected with the cathode chamber inlet of the electrolytic tank and the sodium hydroxide delivery pipeline through pipelines, the chlorine outlet of the electrolytic tank is connected with the inlet pipeline of the chlorine washing tower, the outlet of the chlorine washing tower is connected with the inlet pipeline of the first chlorine drying tower, the outlet of the first chlorine drying tower is connected with the inlet pipeline of the second chlorine drying tower, the outlet of the second chlorine drying tower is connected with the inlet pipeline of the chlorine compressor, and the outlet of the chlorine compressor is connected with the inlet pipeline of the hydrogen chloride synthesis furnace;
The hydrogen outlet of the electrolytic tank is connected with the inlet pipeline of the hydrogen washing tower, the outlet of the hydrogen washing tower is connected with the inlet pipeline of the hydrogen compressor, and the outlet of the hydrogen compressor is connected with the inlet pipeline of the hydrogen chloride synthetic furnace.
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