CN107304057B - Ammonia method alkali preparation system utilizing ammonia distillation waste liquid flash evaporation circulating water - Google Patents
Ammonia method alkali preparation system utilizing ammonia distillation waste liquid flash evaporation circulating water Download PDFInfo
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- CN107304057B CN107304057B CN201610261455.8A CN201610261455A CN107304057B CN 107304057 B CN107304057 B CN 107304057B CN 201610261455 A CN201610261455 A CN 201610261455A CN 107304057 B CN107304057 B CN 107304057B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 213
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 105
- 238000001704 evaporation Methods 0.000 title claims abstract description 78
- 230000008020 evaporation Effects 0.000 title claims abstract description 74
- 239000007788 liquid Substances 0.000 title claims abstract description 66
- 239000002699 waste material Substances 0.000 title claims abstract description 54
- 238000004821 distillation Methods 0.000 title claims abstract description 53
- 239000003513 alkali Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000002360 preparation method Methods 0.000 title claims abstract description 28
- 239000012267 brine Substances 0.000 claims abstract description 136
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 60
- 238000010438 heat treatment Methods 0.000 claims abstract description 12
- 239000013505 freshwater Substances 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 239000002918 waste heat Substances 0.000 abstract description 7
- 239000012141 concentrate Substances 0.000 abstract description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 235000017550 sodium carbonate Nutrition 0.000 description 5
- 229910000029 sodium carbonate Inorganic materials 0.000 description 5
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000009621 Solvay process Methods 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 235000019270 ammonium chloride Nutrition 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- 235000012255 calcium oxide Nutrition 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000008233 hard water Substances 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000123 paper Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 150000003388 sodium compounds Chemical class 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the field of alkali production industry, in particular to an ammonia process alkali production system utilizing ammonia distillation waste liquid flash evaporation circulating water, which comprises an ammonia process alkali production unit, an evaporation concentration unit arranged at the front end of a brine inlet of the ammonia process alkali production unit, an ammonia distillation waste liquid heat exchanger arranged at an ammonia distillation waste liquid outlet of the ammonia process alkali production unit, and a flash evaporator arranged at the front end of a steam inlet of the evaporation concentration unit. The circulating water is heated by the ammonia distillation waste liquid from the ammonia process alkali preparation unit in the ammonia distillation waste liquid heat exchanger, then enters a flash evaporator to generate flash evaporation steam, the flash evaporation steam enters an evaporation concentration unit to evaporate and concentrate brine, and the concentrated brine enters the ammonia process alkali preparation unit to be used for alkali preparation. Compared with the existing ammonia process alkali preparing system, the waste heat of the ammonia distillation waste liquid is recycled while the consumption of a brine heating source is reduced, and the production cost of the ammonia process alkali preparing system is reduced.
Description
Technical Field
The invention relates to the field of alkali production industry, in particular to an ammonia process alkali production system utilizing ammonia distillation waste liquid flash evaporation circulating water.
Background
Sodium carbonate, commonly known as soda ash, soda, is an important raw material for glass, paper, soap, detergents, textile, leather and other industries, and is also commonly used as a softener for hard water and also used for manufacturing sodium compounds. Its industrial preparation method mainly includes two kinds of ammonia-alkali method and combined alkali-making method.
The ammonia-soda process (also called solvay process) is a soda ash process invented by belgium engineers Su Erwei (1838-1922) in 1892. The sodium carbonate is prepared from salt (sodium chloride), limestone (calcined to generate quicklime and carbon dioxide) and ammonia gas. Firstly, introducing ammonia gas into saturated saline water to form ammonia saline water, and then introducing carbon dioxide to generate sodium bicarbonate sediment and ammonium chloride solution with smaller solubility. The chemical reaction principle is as follows:
NaCl+NH 3 +H 2 O+CO 2 ＝NaHCO 3 +NH 4 Cl
and (3) calcining the NaHCO3 tiny crystals obtained by filtering and washing by heating to obtain the sodium carbonate product.
2NaHCO 3 ＝Na 2 CO 3 +H 2 O+CO 2
The discharged carbon dioxide gas can be recycled. Filtrate containing ammonium chloride and lime milk [ Ca (OH) 2 ]The ammonia gas discharged by mixing and heating can be recycled.
CaO+H 2 O＝Ca(OH) 2 ，
2NH 4 Cl+Ca(OH) 2 ＝CaCl 2 +2NH 3 +2H 2 O
The simple flow of its industrial production is shown in figure 3.
The temperature of the ammonia distillation waste liquid generated in the production process of preparing alkali by an ammonia-alkali method is about 90-98 degrees, more waste heat exists, and in the existing production process, on one hand, the ammonia distillation waste liquid is directly discharged and cannot be effectively recycled, on the other hand, in order to improve the alkali preparation efficiency, the brine is required to be heated by a heat source so as to improve the concentration of the brine, and the two factors cause energy waste.
Disclosure of Invention
The invention aims to solve the technical problem of overcoming the defects existing in the prior art and providing an ammonia process alkali preparation system which effectively recovers waste heat and utilizes ammonia distillation waste liquid flash evaporation circulating water.
The invention is realized by the following technical scheme:
an ammonia process alkali preparation system utilizing ammonia distillation waste liquid flash evaporation circulating water comprises an ammonia process alkali preparation unit, an evaporation concentration unit arranged at the front end of a brine inlet of the ammonia process alkali preparation unit, an ammonia distillation waste liquid heat exchange arranged at the rear end of an ammonia distillation waste liquid outlet of the ammonia process alkali preparation unit, a flash evaporator arranged at the front end of a steam inlet of the evaporation concentration unit and an ammonia distillation waste liquid heat exchanger; wherein,,
ammonia distillation waste liquid heat exchanger: the ammonia distillation device is provided with a cold source medium channel for circulating water and a heat source medium channel for ammonia distillation waste liquid output by an ammonia process alkali preparation unit, and is used for heating the introduced circulating water by taking the ammonia distillation waste liquid output by the ammonia process alkali preparation unit as a heat source;
flash evaporator: introducing circulating water output by an ammonia distillation waste liquid heat exchanger, flashing the circulating water serving as a flash evaporation raw liquid, and inputting flash evaporation steam generated by flashing into an evaporation concentration unit;
the evaporation concentration unit comprises a brine multi-stage concentration pipeline and a steam multi-stage condensation pipeline which is arranged in a staggered flow with the brine multi-stage concentration pipeline, wherein a steam-brine heat exchanger, a steam-brine evaporator and a flash steam-brine evaporator are sequentially arranged along the fluid trend of the brine multi-stage concentration pipeline,
the steam-brine heat exchanger is provided with a cold source medium channel for passing through brine and a heat source medium channel for outputting steam through the steam-brine evaporator, and is used for introducing the steam output by the steam-brine evaporator and heating the introduced brine by taking the steam-brine evaporator as a heat source;
the steam-brine evaporator is introduced into the ammonia distillation waste liquid-brine evaporator to output steam, the steam is used as a heat source, the brine output by the introduced steam-brine heat exchanger is evaporated and concentrated, and the steam generated by evaporation is output;
the method comprises the steps of (1) a flash evaporation steam-brine evaporator, introducing flash evaporation steam output by the flash evaporator, taking the flash evaporation steam as a heat source, evaporating and concentrating brine output by the introduced steam-brine evaporator, outputting steam generated by evaporation, and introducing the evaporated and concentrated brine into an ammonia process alkali preparation unit;
condensed water output by the steam-brine evaporator and the steam-brine heat exchanger is discharged through a fresh water pipe;
brine multistage concentration pipeline: the brine firstly passes through a cold source medium channel of a steam-brine heat exchanger, then is evaporated by a steam-brine evaporator, then is evaporated by a flash evaporation steam-brine evaporator, and finally, the evaporated concentrated brine is input into an ammonia process alkaline equipment unit;
steam multistage condensation pipeline: the flash steam generated by the flash steam-brine evaporator is used as a heat source to pass through the steam-brine evaporator, and the steam generated by the steam-brine evaporator passes through a heat source medium channel of the steam-brine heat exchanger and is finally discharged through a fresh water pipe.
The steam-brine evaporator is multistage.
The flash evaporator is multistage.
And an ejector pump for introducing the flash steam into the evaporation concentration unit is arranged at the flash steam outlet of the flash evaporator.
And the two ends of the heat source medium channel of the steam-brine heat exchanger are connected with condensers in parallel, steam output by the steam-brine evaporator passes through the heat source medium channel of the condensers, and condensed water generated by the condensers is discharged through the fresh water pipe.
The beneficial effects of the invention are as follows:
due to the arrangement of the evaporation concentration unit, circulating water is heated by waste heat of the ammonia distillation waste liquid, the heated circulating water is subjected to flash evaporation, flash evaporation steam is output and is input into the evaporation concentration unit, brine is evaporated and concentrated, the consumption of a brine heating heat source is reduced, the multi-effect recycling of the waste heat of the ammonia distillation waste liquid is realized, and the production cost of an ammonia process alkali preparation system is reduced while energy is saved.
Drawings
Fig. 1 is a schematic view of the connection structure of the present invention.
Fig. 2 is a schematic diagram of the connection structure of the evaporation concentration unit of the present invention.
FIG. 3 is a simple flow chart of an industrial production of alkali by an ammonia-soda process.
Fig. 4 is a schematic view of the connection structure with the ejector pump of the present invention.
FIG. 5 is a schematic view of the connection structure with a multi-stage flash vessel of the present invention.
Detailed Description
The present invention will be described in further detail below with reference to the drawings and preferred embodiments, so that those skilled in the art can better understand the technical solutions of the present invention.
As shown in FIG. 1, the invention comprises an ammonia process alkali preparing unit, an evaporation concentration unit, an ammonia distillation waste liquid heat exchanger and a flash evaporator; wherein,,
ammonia distillation waste liquid heat exchanger: the ammonia distillation system comprises an ammonia distillation system, an ammonia process alkali production unit, an ammonia process alkali production system and a circulating water treatment unit, wherein the ammonia distillation system is provided with a cold source medium channel through circulating water and a heat source medium channel through the ammonia distillation waste liquid output by the ammonia process alkali production unit;
the full front end of the ammonia distillation waste liquid heat exchanger can be provided with a water supplementing pipe for supplementing water to the system;
flash evaporator: introducing circulating water output by an ammonia distillation waste liquid heat exchanger, flashing the circulating water serving as a flash evaporation raw liquid, and inputting flash evaporation steam generated by flashing into an evaporation concentration unit;
introducing ammonia distillation waste liquid from an ammonia process alkali preparation unit into an ammonia distillation waste liquid heat exchanger, heating the introduced circulating water as a heat source, discharging the circulating water out of the system, and introducing the heated circulating water into a flash evaporator; the circulating water generates flash evaporation steam and condensation water in the flash evaporator, the flash evaporation steam enters the evaporation concentration unit, and the condensation water returns to the circulating water inlet of the ammonia evaporation waste liquid heat exchanger; and in the evaporation concentration unit, flash steam from a flash evaporator is introduced, the flash steam is used as a heat source to evaporate and concentrate the introduced cold source medium brine, fresh water and concentrated brine are generated, the fresh water is discharged through a fresh water pipe, and the concentrated brine enters an ammonia process alkali preparation unit for alkali preparation. The ammonia process alkali preparing unit consists of a brine heater, saturated salt water equipment, alkali preparing equipment and ammonia distilling equipment, and brine from the flash evaporator sequentially passes through the brine heater, the alkali preparing equipment and the ammonia distilling equipment and then enters a brine heater heat source medium channel as ammonia distilling waste liquid.
Because the evaporation concentration unit, the ammonia distillation waste liquid heat exchanger and the flash evaporator are arranged, the circulating water is heated by utilizing the waste heat of the ammonia distillation waste liquid, flash evaporation steam is generated in the flash evaporator, and the flash evaporation steam is input into the evaporation concentration unit for heating and concentrating the brine, so that an additional heat source is not required to be arranged in the ammonia process alkali preparation unit for heating and concentrating the brine, the consumption of the heat source is reduced while the waste heat of the ammonia distillation waste liquid is recovered, and the operation cost of a system is reduced.
As shown in fig. 2, the evaporation concentration unit comprises a brine multi-stage concentration pipeline and a steam multi-stage condensation pipeline which is arranged in a cross flow with the brine multi-stage concentration pipeline, and a steam-brine heat exchanger, a steam-brine evaporator and a flash steam-brine evaporator are sequentially arranged along the fluid trend of the brine multi-stage concentration pipeline,
the steam-brine heat exchanger is used for introducing steam output by the steam-brine evaporator and heating the introduced brine by taking the steam output by the steam-brine evaporator as a heat source, and is provided with a cold source medium channel for passing through the brine and a heat source medium channel for outputting steam by the steam-brine evaporator;
the steam-brine evaporator is introduced into the ammonia distillation waste liquid-brine evaporator to output steam, the steam is used as a heat source, the brine output by the introduced steam-brine heat exchanger is evaporated, and the steam generated by evaporation is output; the device is provided with a steam inlet for introducing ammonia distillation waste liquid-brine evaporator to output steam, a liquid anticipating inlet for introducing steam-brine heat exchanger to input brine, a finished liquid outlet for outputting evaporated brine, a steam outlet arranged at the top, a heat source medium channel between the steam inlet and the steam outlet, and a cold source medium channel between the liquid anticipating inlet and the finished liquid outlet;
the flash evaporation steam-brine evaporator is used for introducing the flash evaporation steam output by the flash evaporator as a heat source, evaporating the brine output by the introduced steam-brine evaporator, outputting the steam generated by evaporation, and introducing the evaporated brine into ammonia process alkali preparing equipment; the device is provided with a heat source medium channel for flash evaporation steam output by a flash evaporator, a steam outlet is arranged at the top of the heat source medium channel, a liquid anticipating inlet for introducing the brine of the steam-brine evaporator to complete liquid is arranged, a liquid anticipating outlet for outputting the evaporated concentrated brine is arranged, and a cold source medium channel is arranged between the liquid anticipating inlet and the liquid completing outlet.
Condensed water output by the steam-brine evaporator and the steam-brine heat exchanger is discharged through a fresh water pipe;
brine multistage concentration pipeline: the brine firstly passes through a cold source medium channel of a steam-brine heat exchanger, then is evaporated by a steam-brine evaporator, is evaporated by a flash evaporation steam-brine evaporator, and finally, the evaporated concentrated brine is input into an ammonia process alkali preparation unit;
steam multistage condensation pipeline: the flash steam generated by the flash steam-brine evaporator is used as a heat source to pass through the steam-brine evaporator, and the steam generated by the steam-brine evaporator passes through a heat source medium channel of the steam-brine heat exchanger and is finally discharged through a fresh water pipe.
The two ends of the heat source medium channel of the steam-brine heat exchanger are connected with a condenser in parallel to condense the steam generated by the steam-brine evaporator, and the generated condensed water is discharged through a fresh water pipe.
The steam-brine evaporator can be designed into a first stage or a second stage or multiple stages according to the requirements, the steam generated by the ammonia evaporation waste liquid-brine evaporator is used as a heat source to enter the first stage evaporator, the steam generated by the first stage evaporator is used as a heat source to enter the second stage evaporator, the steam generated by the second stage evaporator is used as a heat source to enter the third stage evaporator, … …, correspondingly, the brine evaporation completion liquid of the third stage evaporator enters the second stage evaporator to continue to be evaporated and concentrated, the brine evaporation completion liquid of the second stage evaporator enters the first stage evaporator to continue to be evaporated and concentrated, the brine evaporation completion liquid of the first stage evaporator enters the ammonia evaporation waste liquid evaporator to continue to be evaporated and concentrated, and the brine completion liquid enters ammonia process alkali equipment to be used for alkali production.
As shown in fig. 4, in combination with fig. 2, an ejector pump is disposed at the vapor outlet of the flash vapor, and by introducing high-quality vapor to mix with the flash vapor, the amount of vapor and the quality of vapor entering the evaporation and concentration unit are improved, so that the efficiency of the evaporation and concentration unit is improved.
As shown in fig. 5, in combination with fig. 2 and 4, a two-stage flash evaporator is arranged at the circulating liquid outlet of the ammonia distillation waste liquid heat exchanger, an ejector pump is arranged at the steam outlet of the flash evaporator, high-quality steam is introduced to be mixed with the flash steam, the steam quantity and the steam quality of the steam entering the evaporation concentration unit are improved, and the efficiency of the evaporation concentration unit is further improved.
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (5)
1. An ammonia process alkali preparation system utilizing ammonia distillation waste liquid flash evaporation circulating water is characterized by comprising an ammonia process alkali preparation unit, an evaporation concentration unit arranged at the front end of a brine liquid inlet of the ammonia process alkali preparation unit, an ammonia distillation waste liquid heat exchange arranged at the rear end of an ammonia distillation waste liquid outlet of the ammonia process alkali preparation unit, a flash evaporator arranged at the front end of a steam inlet of the evaporation concentration unit and an ammonia distillation waste liquid heat exchanger; wherein,,
ammonia distillation waste liquid heat exchanger: the ammonia distillation device is provided with a cold source medium channel for circulating water and a heat source medium channel for ammonia distillation waste liquid output by an ammonia process alkali preparation unit, and is used for heating the introduced circulating water by taking the ammonia distillation waste liquid output by the ammonia process alkali preparation unit as a heat source;
flash evaporator: introducing circulating water output by an ammonia distillation waste liquid heat exchanger, flashing the circulating water serving as a flash evaporation raw liquid, and inputting flash evaporation steam generated by flashing into an evaporation concentration unit;
the evaporation concentration unit comprises a brine multi-stage concentration pipeline and a steam multi-stage condensation pipeline which is arranged in a staggered flow with the brine multi-stage concentration pipeline, wherein a steam-brine heat exchanger, a steam-brine evaporator and a flash steam-brine evaporator are sequentially arranged along the fluid trend of the brine multi-stage concentration pipeline,
the steam-brine heat exchanger is provided with a cold source medium channel for passing through brine and a heat source medium channel for outputting steam through the steam-brine evaporator, and is used for introducing the steam output by the steam-brine evaporator and heating the introduced brine by taking the steam-brine evaporator as a heat source;
the steam-brine evaporator is introduced into the ammonia distillation waste liquid-brine evaporator to output steam, the steam is used as a heat source, the brine output by the introduced steam-brine heat exchanger is evaporated and concentrated, and the steam generated by evaporation is output;
the method comprises the steps of (1) a flash evaporation steam-brine evaporator, introducing flash evaporation steam output by the flash evaporator, taking the flash evaporation steam as a heat source, evaporating and concentrating brine output by the introduced steam-brine evaporator, outputting steam generated by evaporation, and introducing the evaporated and concentrated brine into an ammonia process alkali preparation unit;
condensed water output by the steam-brine evaporator and the steam-brine heat exchanger is discharged through a fresh water pipe;
brine multistage concentration pipeline: the brine firstly passes through a cold source medium channel of a steam-brine heat exchanger, then is evaporated by a steam-brine evaporator, then is evaporated by a flash evaporation steam-brine evaporator, and finally, the evaporated concentrated brine is input into an ammonia process alkaline equipment unit;
steam multistage condensation pipeline: the flash steam generated by the flash steam-brine evaporator is used as a heat source to pass through the steam-brine evaporator, and the steam generated by the steam-brine evaporator passes through a heat source medium channel of the steam-brine heat exchanger and is finally discharged through a fresh water pipe.
2. The ammonia process alkaline system utilizing ammonia still waste liquid to flash recycle water according to claim 1, wherein the steam-brine evaporator is multistage.
3. An ammonia process alkaline system using ammonia distillation waste liquid to flash recycle water according to any one of claims 1 or 2 wherein the flash evaporator is multistage.
4. An ammonia process alkaline system utilizing ammonia distillation waste liquid to flash evaporating circulating water according to any one of claims 1 or 2, wherein the flash evaporator is provided with a flash evaporation steam outlet provided with an ejector pump for introducing flash evaporation steam into the evaporation concentration unit.
5. The ammonia process alkaline system utilizing ammonia distillation waste liquid to flash evaporate circulating water according to any one of claims 1 or 2, wherein two ends of a heat source medium channel of the steam-brine heat exchanger are connected with condensers in parallel, steam output by the steam-brine evaporator passes through the heat source medium channel of the condenser, and condensed water generated by the condenser is discharged through a fresh water pipe.
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| DE891059C (en) * | 1942-09-12 | 1953-09-24 | Atlas Werke Ag | Circulation evaporator, especially for seawater evaporation |
| CN203411359U (en) * | 2013-07-31 | 2014-01-29 | 张卫东 | Device for processing residual ammonia water of coke oven with negative pressure flash evaporation method |
| CN203642781U (en) * | 2013-12-04 | 2014-06-11 | 北京国奥时代新能源技术发展有限公司 | Ultrasonic scale preventing and removing device of heating chamber of evaporator |
| CN103864116A (en) * | 2014-03-03 | 2014-06-18 | 北京科技大学 | Method of producing potassium chloride and co-producing calcium carbonate by utilizing cement kiln ash |
| CN204840972U (en) * | 2015-07-28 | 2015-12-09 | 山东伯仲真空设备股份有限公司 | Doublestage MVR evaporimeter |
| CN205709905U (en) * | 2016-04-22 | 2016-11-23 | 天津华赛尔传热设备有限公司 | A kind of ammonia process alkaline system utilizing evaporated waste ammonia liquid flash distillation recirculated water |
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| CN107304057A (en) | 2017-10-31 |
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