CN111099639B - Ammonia supply system and method for preparing sodium carbonate - Google Patents
Ammonia supply system and method for preparing sodium carbonate Download PDFInfo
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- CN111099639B CN111099639B CN202010019806.0A CN202010019806A CN111099639B CN 111099639 B CN111099639 B CN 111099639B CN 202010019806 A CN202010019806 A CN 202010019806A CN 111099639 B CN111099639 B CN 111099639B
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- sodium carbonate
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 200
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 147
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 88
- 229910000029 sodium carbonate Inorganic materials 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims description 41
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims abstract description 206
- 238000004821 distillation Methods 0.000 claims abstract description 128
- 235000019270 ammonium chloride Nutrition 0.000 claims abstract description 103
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 238000005406 washing Methods 0.000 claims abstract description 55
- 238000006243 chemical reaction Methods 0.000 claims abstract description 51
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 35
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 34
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 34
- 239000003507 refrigerant Substances 0.000 claims abstract description 32
- 238000002360 preparation method Methods 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims description 76
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 27
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 27
- 239000004571 lime Substances 0.000 claims description 27
- 238000010438 heat treatment Methods 0.000 claims description 22
- 239000012295 chemical reaction liquid Substances 0.000 claims description 17
- 238000001354 calcination Methods 0.000 claims description 15
- 238000002844 melting Methods 0.000 claims description 14
- 230000008018 melting Effects 0.000 claims description 14
- 239000002699 waste material Substances 0.000 claims description 13
- 238000011033 desalting Methods 0.000 claims description 11
- 239000007787 solid Substances 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- 238000001802 infusion Methods 0.000 claims description 4
- 239000000872 buffer Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000003860 storage Methods 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000003513 alkali Substances 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 3
- 238000004090 dissolution Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 51
- 235000017550 sodium carbonate Nutrition 0.000 description 49
- 239000007789 gas Substances 0.000 description 36
- 230000008020 evaporation Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 238000009621 Solvay process Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000007853 buffer solution Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/18—Preparation by the ammonia-soda process
-
- 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
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides an ammonia supply system for preparing sodium carbonate, which comprises a heat exchange unit, a distillation unit, an ammonium chloride preparation unit and a calcium hydroxide preparation unit; the ammonium chloride preparation unit comprises an ammonium chloride dissolving tank, a cyclone separator and a tail gas washing tower; the distillation unit comprises a distillation tower, a reaction barrel and a flash evaporator, the distillation tower is provided with an ammonia gas outlet, and a raw material inlet of the distillation tower is communicated with an ammonium chloride dissolution tank pipeline; the heat exchange unit comprises a heat exchanger, the heat exchanger is provided with a refrigerant inlet, a heat medium inlet, a refrigerant outlet and a heat medium outlet, the heat medium inlet of the heat exchanger is communicated with a flash evaporator pipeline, and the refrigerant outlet of the heat exchanger is communicated with a washing water inlet pipeline of the tail gas washing tower; the calcium hydroxide preparation unit is communicated with a raw material inlet pipeline of a distillation tower of the distillation tower. The ammonia supply system for preparing sodium carbonate can be used for providing ammonia in an ammonia process for preparing alkali, avoids accidents of a liquid ammonia storage tank, and has high heat energy utilization efficiency.
Description
Technical Field
The invention relates to the field of chemical equipment, in particular to an ammonia supply system and method for preparing sodium carbonate.
Background
In the process of producing sodium carbonate by an ammonia-soda process, ammonia does not participate in the product, but only participates in chemical reaction as an intermediate medium, and finally is recovered through a distillation process. However, ammonia loss is often associated with the actual production system process, such as waste liquid discharge, filtration system aeration, pipeline equipment leakage, tail gas evacuation, equipment switching and the like. Therefore, soda plants for the ammonia-soda process are equipped with an ammonia storage step, and the distillation step is supplemented with liquid ammonia at random. The gaseous ammonia is pressurized to obtain liquid ammonia, the liquid ammonia is corrosive and easy to volatilize, and the ammonia is inflammable and explosive, poisonous, harmful and pungent gas with pungent smell, so that the accident rate of the liquid ammonia is quite high; in the process of storing and conveying liquid ammonia, serious potential risks such as fire explosion, personnel poisoning choking, burning and the like can occur due to leakage of the liquid ammonia due to various reasons or accidents.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide an ammonia supply system and method for preparing sodium carbonate.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows: an ammonia supply system for preparing sodium carbonate, which comprises a heat exchange unit, a distillation unit, an ammonium chloride preparation unit and a calcium hydroxide preparation unit;
The ammonium chloride preparation unit comprises an ammonium chloride dissolving tank, a cyclone separator and a tail gas washing tower, wherein the ammonium chloride dissolving tank is provided with a liquid inlet, a liquid outlet and a solid feed inlet, the upper part of the tail gas washing tower is provided with a washing water inlet, the lower part of the tail gas washing tower is provided with a washing liquid outlet and an ash-removing tail gas inlet, the washing liquid outlet of the tail gas washing tower is communicated with the cyclone separator pipeline, and the liquid outlet of the cyclone separator is communicated with the liquid inlet pipeline of the ammonium chloride dissolving tank;
The distillation unit comprises a distillation tower, a flash evaporator and a reaction barrel, wherein the distillation tower is provided with an air cap layer, the air cap layer divides the distillation tower into a heating layer positioned above the air cap layer and a distillation layer positioned below the air cap layer, the lower part of the distillation layer is provided with a waste liquid outlet of the distillation tower, a steam inlet of the distillation tower and a flash steam inlet of the distillation tower, the upper part of the distillation layer is provided with a reaction liquid inlet of the distillation tower, the waste liquid outlet of the distillation tower is communicated with a liquid inlet pipeline of the flash evaporator, the steam inlet of the distillation tower is used for inputting distillation steam, the flash steam inlet of the distillation tower is communicated with a steam outlet pipeline of the flash evaporator, the heating layer is provided with an ammonium chloride solution inlet of the distillation tower, an ammonia gas output pipeline and an ammonium chloride solution outlet of the distillation tower, the ammonium chloride solution inlet of the distillation tower is communicated with a liquid outlet pipeline of the ammonium chloride solution tank, the top of the reaction barrel is provided with an ammonia gas outlet of the distillation tower, the ammonia gas outlet of the reaction barrel is communicated with a liquid inlet of the reaction barrel, the reaction liquid outlet of the reaction barrel is communicated with the reaction liquid inlet of the reaction barrel, and the reaction liquid inlet of the reaction barrel is communicated with the ammonium chloride solution inlet of the reaction barrel;
The heat exchange unit comprises a heat exchanger, the heat exchanger is provided with a refrigerant inlet, a heat medium inlet, a refrigerant outlet and a heat medium outlet, the refrigerant outlet of the heat exchanger is communicated with a washing water inlet pipeline of the tail gas washing tower, the ammonia supply system for preparing sodium carbonate is matched with the sodium carbonate preparation unit for use, the sodium carbonate preparation unit is provided with a calcination process, and the heat medium inlet of the heat exchanger is communicated with a steam condensate drain pipeline of the calcination process of the sodium carbonate preparation unit;
The lime hydrate preparation unit includes the lime slaker, the lime slaker is provided with the inlet, the inlet of lime slaker with cyclone's liquid outlet pipeline intercommunication, the lime slaker is provided with the calcium hydroxide export, the calcium hydroxide export of lime slaker with the calcium hydroxide entry pipeline intercommunication of reaction bucket, the lime slaker is provided with the lime slaker tail gas export, the lime slaker the tail gas export with the ash slaker tail gas entry pipeline intercommunication of scrubbing tower.
The ammonia supply system for preparing the sodium carbonate can be used for providing ammonia in an ammonia process, so that the ammonia is prevented from being provided by a liquid ammonia storage tank in the ammonia process, the accident occurrence of the liquid ammonia storage tank is avoided, the serious danger source in the ammonia process is eliminated, and the labor consumption cost is reduced; the water of the refrigerant medium is used for washing ash-removing tail gas and then is alkalescent, so that reaction heat can be generated when the water is used for dissolving and preparing the ammonium chloride solution, the temperature of the ammonium chloride solution is increased, and the steam consumption can be reduced after the ammonium chloride solution is sent to a distillation tower; the ammonia supply system for preparing the sodium carbonate is used for preparing the ammonium chloride solution and the calcium hydroxide respectively after the ash-converted tail gas is washed by water as a refrigerant medium, so that the temperature of the ammonium chloride solution is close to that of the calcium hydroxide, the ammonium chloride solution and the calcium hydroxide are mixed and then enter the distillation tower through the raw material inlet of the distillation tower, and because the temperature of the ammonium chloride solution is close to that of the calcium hydroxide, the steam consumption in the distillation process is reduced, and the energy is saved; according to the ammonia supply system for preparing the sodium carbonate, the washing liquid obtained by washing the ash-converted tail gas with water serving as a refrigerant medium after heat exchange is used for preparing the calcium hydroxide, and additional steam supplementing and water heating are not needed for preparing the calcium hydroxide, so that the heat energy is fully and effectively utilized; the top of reaction bucket is provided with the ammonia export, the ammonia export of reaction bucket with the zone of heating pipeline intercommunication for the ammonia that overflows from the reaction liquid in the reaction process directly gets into the zone of heating and exports from the ammonia output pipeline of distillation column, has reduced the energy that the distillation consumed.
Preferably, the ammonia gas output pipeline of the distillation tower is arranged at the top of the heating layer, the ammonium chloride solution outlet of the distillation tower is arranged at the bottom of the heating layer, the ammonia supply system for preparing sodium carbonate is matched with the sodium carbonate preparing unit for use, the sodium carbonate preparing unit is provided with a calcining procedure, and the heat medium inlet of the heat exchanger is communicated with the steam condensate water drain pipeline of the calcining procedure of the sodium carbonate preparing unit.
According to the ammonia supply system for preparing the sodium carbonate, the waste heat utilization is carried out after the heat exchange of the steam condensate water in the calcining process of the sodium carbonate preparation unit, so that the problems of high quality and low use of the condensate water or direct emptying of the condensate water are avoided, part of heat in the condensate water is transferred to the coolant medium water through the heat exchanger, and the condensate water is used for preparing the ammonium chloride solution after being used as the coolant medium water to wash the ash-converted tail gas, so that the energy consumption in the distillation process is reduced.
Preferably, the flash evaporator comprises a first flash evaporator and a second flash evaporator, wherein the first flash evaporator is provided with a steam outlet, a condensed water inlet and a condensed water outlet, the second flash evaporator is provided with a steam outlet, a condensed water outlet and a condensed water inlet, a waste liquid outlet of the distillation tower is communicated with a condensed water inlet pipeline of the first flash evaporator, a flash steam inlet of the distillation tower is communicated with a steam outlet pipeline of the first flash evaporator, a steam outlet of the second flash evaporator is communicated with a flash steam inlet pipeline of the distillation tower, a condensed water outlet of the second flash evaporator is communicated with a heat medium inlet pipeline of the heat exchanger, and a condensed water inlet of the second flash evaporator is communicated with a steam condensed water drain pipeline of a calcining procedure of preparing the soda unit.
Preferably, a flash pump is communicated with a pipeline between the condensed water outlet of the second flash evaporator and the heat medium inlet of the heat exchanger.
Preferably, the sodium carbonate preparation unit is provided with an ammonium chloride drain pipe, and an ammonium chloride solution inlet of the distillation tower is communicated with an ammonium chloride drain pipe pipeline of the sodium carbonate preparation unit.
The ammonia supply system for preparing the sodium carbonate can recycle ammonium chloride generated in the process of preparing the sodium carbonate by the sodium carbonate preparing unit, and reduces the production cost.
Preferably, the heat exchange unit further comprises a desalting water bucket, wherein the desalting water bucket is provided with a liquid inlet, and a heating medium outlet of the heat exchanger is communicated with a liquid inlet pipeline of the desalting water bucket.
According to the ammonia supply system for preparing the sodium carbonate, after the steam condensate water is collected, the heat energy of the steam condensate water is replaced through the flash evaporator and the heat exchanger, and the obtained high-quality condensate water is supplemented into the desalting water bucket, so that the effective utilization of the high-quality heat energy is realized.
Preferably, a buffer solution tank and an ammonium chloride infusion pump which are connected in series are communicated on a pipeline between the ammonium chloride solution inlet of the distillation tower and the liquid outlet of the ammonium chloride dissolving tank.
Preferably, the ammonia supply system for preparing sodium carbonate further comprises a purification unit, the solid outlet of the cyclone separator is communicated with the purification unit through a pipeline, and the heat exchanger is a liquid-liquid plate heat exchanger.
The invention provides an ammonia supply method for preparing sodium carbonate, which is applied to any ammonia supply system for preparing sodium carbonate;
the ammonia supply method for preparing sodium carbonate comprises the following steps:
(1) Preparing an ammonium chloride solution in an ammonium chloride dissolving tank, preparing calcium hydroxide by a calcium hydroxide preparation unit, conveying the ammonium chloride solution to a distillation tower pair, evaporating free ammonia in the ammonium chloride solution, enabling the ammonium chloride solution to enter a reaction barrel, enabling the calcium hydroxide to enter a reaction tube for mixing reaction with the ammonium chloride solution, enabling reaction solution to enter a distillation tower for distillation, and outputting ammonia generated by the distillation tower from an ammonia outlet of the distillation tower for preparing ammonia for sodium carbonate;
(2) Steam condensate water in the calcining process of the sodium carbonate unit enters a heat medium inlet of the heat exchanger and simultaneously enters a refrigerant inlet of the heat exchanger as water of a refrigerant to exchange heat;
(3) In the heat exchange process of the heat exchanger, water flowing out from the refrigerant outlet is input into the tail gas washing tower and then flows out from a washing liquid outlet of the tail gas washing tower to enter the cyclone separator;
(4) The washing liquid is separated by the cyclone separator and then enters the ammonium chloride dissolving tank from the liquid outlet of the cyclone separator.
Preferably, in the step (2), the temperature of the condensed water generated by the flash evaporator is 90-96 ℃, the temperature of the water used as the refrigerant is 25-30 ℃, the temperature of the condensed water at the heat medium outlet is 35-40 ℃, and the temperature of the water at the refrigerant outlet is 48-52 ℃.
The invention has the beneficial effects that: the invention provides an ammonia supply system for preparing sodium carbonate, which can be used for providing ammonia in an ammonia process for preparing sodium carbonate, so that the ammonia is prevented from being provided by a liquid ammonia storage tank in the ammonia process, the accident occurrence of the liquid ammonia storage tank is avoided, the serious dangerous source in the ammonia process for preparing sodium carbonate is eliminated, and the labor consumption cost is reduced; the ammonia supply system for preparing the sodium carbonate disclosed by the invention has the advantages that the condensed water generated after the flash evaporation of the distillation tower is subjected to heat exchange and then is subjected to waste heat utilization, so that the problems of high quality and low use or direct emptying of the condensed water are avoided; the water of the refrigerant medium is used for washing ash-removing tail gas to be alkalescent, so that reaction heat can be generated when the water is used for dissolving and preparing the ammonium chloride solution, the temperature of the ammonium chloride solution is increased, and the steam consumption can be reduced after the ammonium chloride solution is sent to a distillation tower.
Drawings
FIG. 1 is a schematic diagram of an ammonia supply system for preparing soda ash according to an embodiment of the invention;
Wherein, 1, a heat exchanger, 101, a heat medium inlet, 102, a refrigerant inlet, 103, a refrigerant outlet, 104, a heat medium outlet, 2, a distillation tower, 201, a distillation layer, 202, a heating layer, 203, a gas cap layer, 204, an ammonia gas output pipeline of the distillation tower, 205, an ammonium chloride solution inlet of the distillation tower, 206, a flash steam inlet of the distillation tower, 207, a waste liquid outlet of the distillation tower, 208, a steam inlet of the distillation tower, 209, an ammonium chloride solution outlet of the distillation tower, 2010, a reaction liquid inlet of the distillation tower, 3, a tail gas washing tower, 301, a washing water inlet of the tail gas washing tower, 302, a washing liquid outlet of the tail gas washing tower, 4, an ammonium chloride dissolving tank, 401, a solid feed inlet of the ammonium chloride dissolving tank, 402, a liquid inlet of the ammonium chloride dissolving tank, 403, a liquid outlet of the ammonium chloride dissolving tank, 404, a buffer liquid tank, 405, an ammonium chloride infusion pump, 5, an ash machine, 501, a liquid inlet of a ash melting machine, 502, a calcium hydroxide outlet of the ash melting machine, 503, an ash melting tail gas outlet of the ash melting machine, 6, a cyclone separator, 601, a feed inlet of the cyclone separator, 602, a liquid outlet of the cyclone separator, 603, a solid outlet of the cyclone separator, 7, a first flash evaporator, 701, a condensed water inlet of the first flash evaporator, 702, a vapor outlet of the first flash evaporator, 703, a condensed water outlet of the first flash evaporator, 704, a waste liquid barrel, 8, a second flash evaporator, 801, a flash pump, 802, a condensed water outlet of the second flash evaporator, 803, a condensed water inlet of the second flash evaporator, 804, a vapor outlet of the second flash evaporator, 805, a vapor condensed water drain pipe for a calcination process of a soda preparation unit, 9, a purification unit, 10, a reaction barrel, 1001, an ammonia outlet of the reaction barrel, 1002, a reaction liquid outlet of the reaction barrel, 1003, a calcium hydroxide inlet of the reaction barrel, 1004. an ammonium chloride solution inlet of the reaction barrel, 11, and a desalting water barrel.
Detailed Description
For a better description of the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to the following specific examples.
Example 1
As an ammonia supply system for preparing sodium carbonate, as shown in figure 1, the ammonia supply system comprises a heat exchange unit, a distillation unit, an ammonium chloride preparation unit and a calcium hydroxide preparation unit;
The ammonium chloride preparation unit comprises an ammonium chloride dissolving tank 4, a cyclone separator 6 and a tail gas washing tower 3, wherein the ammonium chloride dissolving tank 4 is provided with a liquid inlet 402, a liquid outlet 403 and a solid feed inlet 401, the upper part of the tail gas washing tower 3 is provided with a washing water inlet 301, the lower part of the tail gas washing tower 3 is provided with a washing liquid outlet 302 and an ash-converted tail gas inlet, the cyclone separator 6 is provided with a feed inlet 601 of the cyclone separator and a liquid outlet 602 of the cyclone separator, the washing liquid outlet 302 of the tail gas washing tower is communicated with the feed inlet 601 of the cyclone separator through a pipeline, and the liquid outlet 602 of the cyclone separator is communicated with the liquid inlet 402 of the ammonium chloride dissolving tank through a pipeline;
The distillation unit comprises a distillation tower 2, a flash evaporator and a reaction barrel 10, wherein the distillation tower is provided with an air cap layer 203, the air cap layer 203 divides the distillation tower into a heating layer 202 positioned above the air cap layer and a distillation layer 201 positioned below the air cap layer, a waste liquid outlet 207 of the distillation tower, a steam inlet 208 of the distillation tower and a flash steam inlet 206 of the distillation tower are arranged at the lower part of the distillation layer 201, a reaction liquid inlet 2010 of the distillation tower is arranged at the upper part of the distillation layer 201, the waste liquid outlet 207 of the distillation tower is communicated with a liquid inlet pipeline of the flash evaporator, the steam inlet 208 of the distillation tower is used for inputting distillation steam, the flash steam inlet 206 of the distillation tower is communicated with a steam outlet 702 pipeline of the flash evaporator, the heating layer 202 is provided with an ammonium chloride solution inlet 205 of the distillation tower, an ammonia gas outlet pipeline 204 and an ammonium chloride solution outlet 209, the ammonium chloride solution inlet 205 of the distillation tower is communicated with a liquid outlet 403 pipeline of the ammonium chloride dissolving tank, an ammonia outlet 1001 is arranged at the top of the reaction barrel 10, the ammonia outlet of the reaction barrel is communicated with the heating layer 202 pipeline, a reaction liquid outlet 1002 is arranged at the bottom of the reaction barrel 10, the reaction liquid outlet of the reaction barrel is communicated with the reaction liquid inlet 1002 of the reaction liquid inlet of the reaction barrel 10 and the reaction liquid inlet of the reaction barrel is communicated with an ammonium chloride solution inlet 1004;
The heat exchange unit comprises a heat exchanger 1, wherein the heat exchanger 1 is provided with a refrigerant inlet 102, a heat medium inlet 101, a refrigerant outlet 103 and a heat medium outlet 104, an ammonia supply system for preparing sodium carbonate is matched with the sodium carbonate preparing unit for use, the sodium carbonate preparing unit is provided with a calcining procedure, the heat medium inlet 101 of the heat exchanger is communicated with a steam condensate drain pipe 805 in the calcining procedure of the sodium carbonate preparing unit through a pipeline, and the refrigerant outlet 103 of the heat exchanger is communicated with a washing water inlet 301 of the tail gas washing tower through a pipeline;
The calcium hydroxide preparation unit comprises a lime slaker 5, wherein the lime slaker is provided with a liquid inlet 501, the liquid inlet 501 of the lime slaker is communicated with a liquid outlet 602 pipeline of the cyclone separator, the lime slaker is provided with a calcium hydroxide outlet 502, the calcium hydroxide outlet 502 of the lime slaker is communicated with a calcium hydroxide inlet 1003 pipeline of the reaction barrel, the top of the lime slaker 5 is provided with a lime slaker tail gas outlet 503, and the lime slaker tail gas outlet 503 is communicated with a lime slaker tail gas inlet pipeline of the washing tower 3.
Further, an ammonia gas output pipeline of the distillation tower is arranged at the top of the heating layer, and an ammonium chloride solution outlet of the distillation tower is arranged at the bottom of the heating layer.
In order to further improve the evaporation efficiency, the flash evaporator comprises a first flash evaporator 7 and a second flash evaporator 8, wherein the first flash evaporator is provided with a steam outlet 702, a condensed water inlet 701 and a condensed water outlet 703, a waste liquid outlet 207 of the distillation tower is communicated with a condensed water inlet 701 pipeline of the first flash evaporator, the condensed water outlet 703 of the first flash evaporator is communicated with a waste liquid barrel 704, the second flash evaporator is provided with a steam outlet 804, a condensed water outlet 802 and a condensed water inlet 803, a flash steam inlet 206 of the distillation tower is communicated with a steam outlet 702 pipeline of the first flash evaporator, a steam outlet 804 of the second flash evaporator 8 is communicated with a flash steam inlet 206 pipeline of the distillation tower, and a condensed water outlet 802 of the second flash evaporator is communicated with a heat medium inlet 101 pipeline of the heat exchanger.
Further, a flash pump 801 is connected to a pipeline between the condensed water outlet 802 of the second flash evaporator and the heat medium inlet 101 of the heat exchanger.
In order to realize the recycling of ammonium chloride generated in the process of preparing sodium carbonate, an ammonium chloride solution inlet 205 of the distillation tower is communicated with an ammonium chloride liquid discharge pipe of the sodium carbonate preparing unit.
In order to fully utilize the high-quality heat energy of the distilled condensate water, the heat exchange unit further comprises a desalting water bucket 11, wherein the desalting water bucket is provided with a liquid inlet, and a heat medium outlet 104 of the heat exchanger is communicated with a liquid inlet pipeline of the desalting water bucket.
In order to control the flow of the ammonium chloride solution entering the distillation tower to be stable, a buffer tank 404 and an ammonium chloride infusion pump 405 which are connected in series are communicated on a pipeline between an ammonium chloride solution inlet 205 of the distillation tower and a liquid outlet 403 of the ammonium chloride dissolving tank.
Further, the ammonia supply system for preparing sodium carbonate also comprises a purifying unit 9, a solid outlet 603 of the cyclone separator is communicated with the purifying unit 9 through a pipeline, an ammonia outlet 204 of the distillation tower is used for conveying ammonia to the sodium carbonate preparing unit, and the heat exchanger is a liquid-liquid plate heat exchanger. The tail gas washing tower 3 can purify dust generated in the process of preparing calcium hydroxide, and the dust is prevented from being discharged into the atmosphere.
The ammonia supply system for preparing sodium carbonate can be used for providing ammonia in an ammonia process alkali preparation process, so that ammonia is prevented from being provided by a liquid ammonia storage tank in the ammonia process alkali preparation process, accidents of the liquid ammonia storage tank are avoided, important dangerous sources in the ammonia process alkali preparation process are eliminated, and labor consumption cost is reduced; according to the ammonia supply system for preparing sodium carbonate, the condensed water generated after flash evaporation of the distillation tower is subjected to heat exchange and then is subjected to waste heat utilization, so that the problems of high quality and low use of the condensed water or direct emptying of the condensed water are avoided; the water of the refrigerant medium is used for washing ash-removing tail gas to be alkalescent, so that reaction heat can be generated when the water is used for dissolving and preparing the ammonium chloride solution, the temperature of the ammonium chloride solution is increased, and the steam consumption can be reduced after the ammonium chloride solution is sent to a distillation tower.
An ammonia supply method for preparing sodium carbonate, which uses the ammonia supply system for preparing sodium carbonate as described in example 1;
the ammonia supply method for preparing sodium carbonate comprises the following steps:
(1) Preparing an ammonium chloride solution in an ammonium chloride dissolving tank, preparing calcium hydroxide by a calcium hydroxide preparation unit, conveying the ammonium chloride solution to a distillation tower heating layer pair, evaporating free ammonia in the ammonium chloride solution, enabling the ammonium chloride solution to enter a reaction barrel, enabling the calcium hydroxide to enter the reaction barrel to be mixed with the ammonium chloride solution for reaction, enabling reaction solution to enter a distillation layer of the distillation tower for distillation, and outputting ammonia generated by the distillation tower from an ammonia outlet of the distillation tower for preparing ammonia for sodium carbonate;
(2) Steam condensate water in the calcining process of the sodium carbonate unit enters a heat medium inlet of the heat exchanger and simultaneously enters a refrigerant inlet of the heat exchanger as water of a refrigerant to exchange heat;
(3) In the heat exchange process of the heat exchanger, water flowing out from the refrigerant outlet is input into the tail gas washing tower and then flows out from a washing liquid outlet of the tail gas washing tower to enter the cyclone separator;
(4) The washing liquid is separated by the cyclone separator and then enters the ammonium chloride dissolving tank from the liquid outlet of the cyclone separator.
Further, in the step (1), when the mass fraction of the ammonium chloride solution in the ammonium chloride dissolving tank reaches 25%, free ammonia in the ammonium chloride solution fed to the distillation column pair is evaporated.
Further, in the step (2), the temperature of the condensed water generated by the flash evaporator is 90-96 ℃, the temperature of the water used as the refrigerant is 25-30 ℃, the temperature of the condensed water at the outlet of the heating medium is 35-40 ℃, and the temperature of the water at the outlet of the refrigerant is 48-52 ℃.
Finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted equally without departing from the spirit and scope of the technical solution of the present invention.
Claims (7)
1. An ammonia supply system for preparing sodium carbonate is characterized by comprising a heat exchange unit, a distillation unit, an ammonium chloride preparation unit and a calcium hydroxide preparation unit;
The ammonium chloride preparation unit comprises an ammonium chloride dissolving tank, a cyclone separator and a tail gas washing tower, wherein the ammonium chloride dissolving tank is provided with a liquid inlet, a liquid outlet and a solid feed inlet, the upper part of the tail gas washing tower is provided with a washing water inlet, the lower part of the tail gas washing tower is provided with a washing liquid outlet and an ash-removing tail gas inlet, the washing liquid outlet of the tail gas washing tower is communicated with the cyclone separator pipeline, and the liquid outlet of the cyclone separator is communicated with the liquid inlet pipeline of the ammonium chloride dissolving tank;
The distillation unit comprises a distillation tower, a flash evaporator and a reaction barrel, wherein the distillation tower is provided with an air cap layer, the air cap layer divides the distillation tower into a heating layer positioned above the air cap layer and a distillation layer positioned below the air cap layer, the lower part of the distillation layer is provided with a waste liquid outlet of the distillation tower, a steam inlet of the distillation tower and a flash steam inlet of the distillation tower, the upper part of the distillation layer is provided with a reaction liquid inlet of the distillation tower, the waste liquid outlet of the distillation tower is communicated with a liquid inlet pipeline of the flash evaporator, the steam inlet of the distillation tower is used for inputting distillation steam, the flash steam inlet of the distillation tower is communicated with a steam outlet pipeline of the flash evaporator, the heating layer is provided with an ammonium chloride solution inlet of the distillation tower, an ammonia gas output pipeline and an ammonium chloride solution outlet of the distillation tower, the ammonium chloride solution inlet of the distillation tower is communicated with a liquid outlet pipeline of the ammonium chloride solution tank, the top of the reaction barrel is provided with an ammonia gas outlet of the distillation tower, the ammonia gas outlet of the reaction barrel is communicated with a liquid inlet of the reaction barrel, the reaction liquid outlet of the reaction barrel is communicated with the reaction liquid inlet of the reaction barrel, and the reaction liquid inlet of the reaction barrel is communicated with the ammonium chloride solution inlet of the reaction barrel;
The heat exchange unit comprises a heat exchanger, the heat exchanger is provided with a refrigerant inlet, a heat medium inlet, a refrigerant outlet and a heat medium outlet, and the refrigerant outlet of the heat exchanger is communicated with a washing water inlet pipeline of the tail gas washing tower;
The calcium hydroxide preparation unit comprises a lime melting machine, wherein the lime melting machine is provided with a liquid inlet, the liquid inlet of the lime melting machine is communicated with a liquid outlet pipeline of the cyclone separator, the lime melting machine is provided with a calcium hydroxide outlet, the calcium hydroxide outlet of the lime melting machine is communicated with a calcium hydroxide inlet pipeline of the reaction barrel, the lime melting machine is provided with a lime melting tail gas outlet, and the lime melting tail gas outlet of the lime melting machine is communicated with a lime melting tail gas inlet pipeline of the washing tower;
a buffer tank and an ammonium chloride infusion pump which are connected in series are communicated on a pipeline between an ammonium chloride solution inlet of the distillation tower and a liquid outlet of the ammonium chloride dissolving tank;
The ammonia supply system for preparing sodium carbonate further comprises a purification unit, a solid outlet of the cyclone separator is communicated with the purification unit through a pipeline, and the heat exchanger is a liquid-liquid plate heat exchanger.
2. The ammonia supply system for preparing sodium carbonate according to claim 1, wherein an ammonia output pipeline of the distillation tower is arranged at the top of the heating layer, an ammonium chloride solution outlet of the distillation tower is arranged at the bottom of the heating layer, the ammonia supply system for preparing sodium carbonate is matched with a sodium carbonate preparing unit for use, the sodium carbonate preparing unit is provided with a calcining procedure, and a heating medium inlet of the heat exchanger is communicated with a steam condensate drain pipeline of the calcining procedure of the sodium carbonate preparing unit.
3. The ammonia supply system for producing sodium carbonate according to claim 2, wherein the flash evaporator comprises a first flash evaporator and a second flash evaporator, the first flash evaporator is provided with a steam outlet, a condensed water inlet and a condensed water outlet, the second flash evaporator is provided with a steam outlet, a condensed water outlet and a condensed water inlet, the waste liquid outlet of the distillation column is communicated with the condensed water inlet pipeline of the first flash evaporator, the flash steam inlet of the distillation column is communicated with the steam outlet pipeline of the first flash evaporator, the steam outlet of the second flash evaporator is communicated with the flash steam inlet pipeline of the distillation column, the condensed water outlet of the second flash evaporator is communicated with the heat medium inlet pipeline of the heat exchanger, and the condensed water inlet of the second flash evaporator is communicated with the steam condensed water drain pipeline of the calcination process for producing sodium carbonate unit.
4. The ammonia supply system for preparing sodium carbonate according to claim 3, wherein a flash pump is connected to a pipeline between the condensed water outlet of the second flash evaporator and the heat medium inlet of the heat exchanger.
5. The ammonia supply system for preparing sodium carbonate according to claim 3, wherein the sodium carbonate preparing unit is provided with an ammonium chloride drain pipe, and an ammonium chloride solution inlet of the distillation tower is communicated with the ammonium chloride drain pipe pipeline of the sodium carbonate preparing unit.
6. The ammonia supply system for preparing sodium carbonate according to claim 1, wherein the heat exchange unit further comprises a desalting water barrel, the desalting water barrel is provided with a liquid inlet, and the heat medium outlet of the heat exchanger is communicated with the liquid inlet pipeline of the desalting water barrel.
7. An ammonia supply method for preparing sodium carbonate, which is characterized in that the ammonia supply method for preparing sodium carbonate uses the ammonia supply system for preparing sodium carbonate according to any one of claims 1-6;
the ammonia supply method for preparing sodium carbonate comprises the following steps:
(1) Preparing an ammonium chloride solution in an ammonium chloride dissolving tank, preparing calcium hydroxide by a calcium hydroxide preparation unit, conveying the ammonium chloride solution to a distillation tower heating layer pair, evaporating free ammonia in the ammonium chloride solution, enabling the ammonium chloride solution to enter a reaction barrel, enabling the calcium hydroxide to enter a reaction tube for mixing reaction with the ammonium chloride solution, enabling reaction solution to enter a distillation layer of the distillation tower for distillation, and outputting ammonia generated by the distillation tower from an ammonia outlet of the distillation tower for preparing ammonia for sodium carbonate;
(2) Steam condensate water in the calcining process of the sodium carbonate unit enters a heat medium inlet of the heat exchanger and simultaneously enters a refrigerant inlet of the heat exchanger as water of a refrigerant to exchange heat;
(3) In the heat exchange process of the heat exchanger, water flowing out from the refrigerant outlet is input into the tail gas washing tower and then flows out from a washing liquid outlet of the tail gas washing tower to enter the cyclone separator;
(4) The washing liquid is separated by the cyclone separator and then enters the ammonium chloride dissolving tank from the liquid outlet of the cyclone separator.
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