CN204325056U - A kind of thermo-compression evaporation system recycling gas cleaning by product - Google Patents
A kind of thermo-compression evaporation system recycling gas cleaning by product Download PDFInfo
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- CN204325056U CN204325056U CN201420741511.4U CN201420741511U CN204325056U CN 204325056 U CN204325056 U CN 204325056U CN 201420741511 U CN201420741511 U CN 201420741511U CN 204325056 U CN204325056 U CN 204325056U
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- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
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- 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
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a kind of thermo-compression evaporation system recycling gas cleaning by product, comprises crystallization reactor, solid-liquid separator, fresh feed pump, preheater, interchanger, forced circulation pump, crystal separator, compressor; Described crystallization reactor connects solid-liquid separator, solid-liquid separator connects fresh feed pump, fresh feed pump connects the fluid inlet of preheater, the liquid outlet of preheater connects the fluid inlet of interchanger, interchanger is connected with the fluid inlet of crystal separator by forced circulation pump, the venting port of crystal separator is connected with the inlet mouth of compressor by steam-pipe, and the venting port of compressor is connected with the inlet mouth of interchanger shell.Using the waste liquid after flue gas desulfurization and denitrification as raw material, recycle after preheating, pump circulation heating, condensing crystal.This technique is particularly suitable for the waste liquid after smoke treatment desulphurization denitration, reaches the object turned waste into wealth, and has saved the consumption of steam.
Description
Technical field
The utility model relates to flue gases purification field, is specifically related to a kind of thermo-compression evaporation system recycling gas cleaning by product.
Background technology
In recent years along with air-polluting is more and more serious, the improvement of people to flue gas particularly coal-fired flue-gas is had higher requirement; National environmental protection portion has issued new " fossil-fuel power plant atmospheric pollutant emission standard " (GB 13223-2011) on July 29th, 2011, proposes new emission limit to the flue dust of flue gas, sulfurous gas, oxynitride.At present, the effective means of flue gas desulfurization is the wet process of FGD such as ammonia process, sodium method.Above sulfur method all will produce the waste liquid of certain density containing sulfate, nitrate.Have the characteristics such as saltiness is high, slant acidity, during employing usual way process, effluent quality is difficult to reach emission standard, and the exploitation for the novel treatment technology of gas cleaning waste water seems particularly important.Especially for the area that environmental requirement is higher, often require high slat-containing wastewater " zero release ", this just has higher requirement to high slat-containing wastewater treatment technology.Need process it, reclaim useful matter simultaneously, avoid waste.Traditional treatment process adopts multiple-effect evaporation, causes energy consumption higher.
201110155630.2, name is called the utility model patent of " ammonium sulfate after desulfurization/magnesium sulfate recovery technology ", and technical process is: raw material → feedstock pump → preheater → 1st effective evaporator → 2nd effect evaporator → triple-effect evaporator → condenser → liquid seal trough → discharge; Admittedly material some processes flow process: triple-effect evaporator → discharging pump → crystallizer → whizzer → drying machine → feed bin → wrapping machine.The secondary steam of a certain effect of vaporizer of this patent can not directly as this effect thermal source, can only as the thermal source of secondary effect or secondary a few effect.As additionally its energy must be given as this effect thermal source, its temperature (pressure) is improved.
Utility model content
In order to solve the problems of the technologies described above, the utility model provides a kind of thermo-compression evaporation system recycling gas cleaning by product.Using the waste liquid after flue gas desulfurization and denitrification as raw material, first reclaim absorption agent by crystallization reactor, liquid is recycled after preheating, pump circulation heating, condensing crystal again.This technique be particularly suitable for after smoke treatment desulphurization denitration containing waste liquor of ammonium, reach the object turned waste into wealth, saved the consumption of steam; Meanwhile, the water distilled is capable of circulation to be used as moisturizing to desulphurization denitration workshop section, water saving.
For achieving the above object, the utility model adopts following technical scheme:
Recycle the system that gas cleaning by product prepares ammonium salt, it is characterized in that: comprise crystallization reactor, solid-liquid separator, fresh feed pump, preheater, interchanger, crystal separator, compressor; The discharge port of described crystallization reactor connects solid-liquid separator, solid-liquid separator connects fresh feed pump, fresh feed pump connects preheater, the liquid outlet of preheater connects the fluid inlet of interchanger, interchanger is connected with the fluid inlet of crystal separator by forced circulation pump, the venting port of crystal separator is connected with the inlet mouth of compressor by steam-pipe, and the venting port of compressor is connected with the inlet mouth of interchanger shell.
The waste liquid that flue gas obtains after wet purification reacts with bicarbonate of ammonia in crystallization reactor, the absorption agent that the solid reclaimed in reaction solution by solid-liquid separator one can be used as flue gas is back to gas cleaning workshop section, liquid is as stock liquid, pump into preheater, stock liquid after preheating enters interchanger, raised by shell side steam heating temperature in the tube side of interchanger, stock liquid enters crystal separator under the promotion of forced circulation pump, crystal separator internal pressure reduces, stock liquid produces flash distillation, the secondary steam that flash distillation produces rises from steam-pipe and discharges in crystal separator, stock liquid produces supersaturation and makes nuclei grow, when nuclei grow is deposited to bottom crystal separator to during comparatively macrocrystal, described secondary steam enters the shell side of interchanger after compressor compression as thermal source.
Wet purification described in the utility model refers to wet desulphurization or denitration.
Described preheater is divided into one-level preheater and secondary preheater, effectively utilizes boiler afterheat and steam condensed water waste heat.
Described compressor is the compact construction of centrifugal compressor, centrifugal compressor, and size is little, lightweight; Exhaust is continuous, even, does not need the devices such as tundish; Vibrate little, few easy workout part, do not need the huge and basic part of heaviness; Except bearing, machine intimate does not need lubrication, fuel-efficient, and does not pollute by the gas compressed; Rotating speed is high; A little repair, easy to adjust.
Preferably, described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.Compressor tandem energy accesses higher pressure head, improves secondary steam temperature simultaneously, returns to interchanger three forced circulation evaporation as thermal source.
Preferably, the phlegma liquid outlet of described interchanger three is connected container for storing liquid with the phlegma liquid outlet of secondary preheater, and the liquid outlet of container for storing liquid connects the fluid inlet of one-level preheater shell.Using the thermal source of the phlegma of interchanger three and secondary preheater as one-level preheater, save energy.
The phlegma liquid outlet connection of described one-level preheater is got back to gas cleaning workshop section and is achieved zero release as moisturizing use.
Cooling crystallizer, solid-liquid separator two, distillation tower, cooling twice crystallizer and a solid-liquid separator three is also connected with in turn between solid-liquid separator one described in the utility model and fresh feed pump, described solid-liquid separator two connects distillation tower by interchanger two, and described solid-liquid separator three connects fresh feed pump by interchanger three.
The waste liquid of flue gas after wet purification sends into crystallization reactor and bicarbonate of ammonia reacts, after having reacted, liquid enters a cooling crystallizer crystallization, clear liquid is sent into distillation tower by solid-liquid separator two after interchanger heating, send distilling the clear liquid obtained into the crystallization of cooling twice crystallizer again, clear liquid is sent into vapo(u)rization system removing excessive moisture by solid-liquid separator three after interchanger heating, obtains highly purified ammonium salt solution.
The utility model adopts the system process ammonium salt mother liquor of a cooling crystallizer-distillation tower-cooling twice crystallizer, and secondary crystal is to separate out the unreacted impurity such as bicarbonate of ammonia and sodium sulfate completely in solution, reduce supplies consumption simultaneously; Distillation is to remove free ammonia in solution and carbonic acid gas.
Solid-liquid separator two described in the utility model connects gets back to crystallization reactor.The solid of a crystallisation by cooling precipitation separates out a large amount of sal glauberis, sodium bicarbonate and bicarbonate of ammonia, turns back in crystallization reactor and continues reaction.
Solid-liquid separator three described in the utility model connects gets back to a cooling crystallizer.The mixture of cooling twice crystallization four aqueous sodium persulfate and ammonium sulfate, reduces the sodium sulphate content in ammonium sulfate liquor further; Turn back to further crystallisation by cooling in a crystallisation by cooling operation, to improve the product purity of ammonium sulfate simultaneously.
Described is once-2 ~ 0 DEG C with the temperature of cooling twice crystallization.
The venting port of distillation tower described in the utility model connects the bottom of crystallization reactor by booster fan.
Distill in the ammonia and carbonic acid gas Returning reactor obtained and continue reaction, reduce supplies consumption, and reduce the pollution to environment; By booster fan by gas dispersion to crystalliser feet, from the bottom up, utilize crystallizer solution fully to reclaim ammonia and carbonic acid gas.
The leakage fluid dram of described distillation tower passes through the shell side connecting secondary cooling crystallizer of interchanger one.Clear liquid after a crystallisation by cooling by with distillation tower bottom fluid carry out heat exchange and reach more than 60 DEG C, then send into distillation tower, save distillation steam consumption, reduce plant energy consumption.
Solid-liquid separator four described in the utility model connects gets back to cooling twice crystallizer.Be separated the liquid that obtains before sodium sulfate reaches capacity, filtrate be sent to cooling twice crystallizer and carry out crystallisation by cooling, will sodium sulfate separate out after enter the vapo(u)rization system of postorder again, thus ensure the purity of ammonium sulfate product.
Preferably, described is once DTB cooling crystallizer with cooling twice crystallizer, and the ability of crystallization is high.
Described solid-liquid separator one is separating centrifuge or band filter.
Equipment and materials described in the utility model and the selection for pipeline TA2 material with material contact part.
The beneficial effects of the utility model are:
1, in order to adapt to the crystallization and evaporation process of gas cleaning waste liquid, the utility model adopts forced circulation evaporation system.Material is raised by shell side steam heating temperature in the tube side of interchanger, the low generation flash distillation of Pressure Drop enter crystal separator under the promotion of forced circulation pump after, the secondary steam produced is discharged from vapour line, material produces supersaturation crystallization sedimentation, the secondary steam that forced circulation evaporation produces after compressor compresses as the thermal source of interchanger.Saved the consumption of steam, raw steam about the 7000t of annual saving, achieves energy-conservation.Reduce by the floor space of more than 50% simultaneously.
2, the phlegma of secondary preheater of the present utility model and interchanger is as the thermal source of one-level preheater, and meanwhile, the phlegma of one-level preheater is got back to gas cleaning workshop section and used as moisturizing, the while of water-saving, achieves zero release.
3, the utility model adopts centrifugal compressor as heat pump, itself consumption little a part of electric energy during work, but can extract 4-7 doubly to electric energy from secondary steam, promotes temperature and utilizes.The compact construction of compression whizzer own, size is little, lightweight; Exhaust is continuous, even, does not need the devices such as tundish; Vibrate little, few easy workout part, do not need the huge and basic part of heaviness; Except bearing, machine intimate does not need lubrication, fuel-efficient, and does not pollute by the gas compressed; Rotating speed is high; A little repair, easy to adjust.
4, the utility model is by the waste liquid of gas cleaning, the waste liquid and the bicarbonate of ammonia that comprise desulfurization or denitration react, containing the ammonium salt such as ammonium sulfate and ammonium nitrate in reaction solution, solid-liquid separator one is separated the absorption agent that the solid obtained can be used as flue gas and is back to gas cleaning workshop section.Adopt the system process ammonium salt mother liquor of a cooling crystallizer-distillation tower-cooling twice crystallizer, secondary crystal is to separate out the unreacted impurity such as bicarbonate of ammonia and sodium sulfate completely in solution, reduce supplies consumption simultaneously; Distillation is to remove free ammonia in solution and carbonic acid gas.Obtain highly purified ammonium salt solution.The nitrogen content of the finished product meets the producing ammonium sulfate byproduct product requirement of electric power standard: total nitrogen >=18%, appearance white particle.
5, solid-liquid separator two described in the utility model connects and gets back to crystallization reactor, and sal glauberi, sodium bicarbonate and bicarbonate of ammonia solid that crystallisation by cooling is separated out turn back in crystallization reactor and continue reaction; Solid-liquid separator three connects gets back to a cooling crystallizer, and precipitation four aqueous sodium persulfate of cooling twice crystallization and the mixture solid of ammonium sulfate turn back to crystallisation by cooling in a crystallisation by cooling operation; Solid-liquid separator four connects gets back to cooling twice crystallizer, containing a large amount of ammonium sulfate in the solution after separation, gets back to crystallisation by cooling in cooling twice Crystallization Procedure and separates out.More than operation is the strong guarantee of yield coefficient of ammonium sulfate, and the yield that system obtains ammonium salt product reaches more than 99%, and waste liquid per ton can by-product 0.25-0.35 ton ammonium salt product.
6, because the leakage fluid dram of distillation tower is by the shell side connecting secondary cooling crystallizer of interchanger one, make the clear liquid after a crystallisation by cooling by with distillation tower bottom fluid carry out heat exchange, temperature reaches more than 60 DEG C, then sends into distillation tower, save distillation steam consumption, reduce plant energy consumption.
Accompanying drawing explanation
Fig. 1 is the thermo-compression evaporation system construction drawing of gas cleaning by product of the present utility model.
Fig. 2 is the thermo-compression evaporation system construction drawing of embodiment 4 of the present utility model.
Fig. 3 is the thermo-compression evaporation system construction drawing of embodiment 8 of the present utility model.
Fig. 4 is the thermo-compression evaporation system construction drawing of embodiment 10 of the present utility model.
Be labeled as in figure: 1, crystallization reactor, 2, solid-liquid separator one, 3, fresh feed pump, 4, preheater, 5, interchanger one, 6, crystal separator, 7, compressor, 8, one-level preheater, 9, secondary preheater, 10, container for storing liquid, 11, cooling crystallizer, 12, solid-liquid separator two, 13, interchanger two, 14, distillation tower, 15, cooling twice crystallizer, 16, solid-liquid separator three, 17, interchanger three.
Embodiment
Below in conjunction with embodiment, essentiality content of the present utility model is described in further detail.
Embodiment 1
Recycle a thermo-compression evaporation system for gas cleaning by product, comprise crystallization reactor 1, solid-liquid separator 1, fresh feed pump 3, preheater 4, interchanger 1, crystal separator 6, compressor 7; The discharge port of described crystallization reactor 1 connects solid-liquid separator 1, the liquid outlet of solid-liquid separator 1 connects fresh feed pump 3, fresh feed pump 3 connects preheater 4, the liquid outlet of preheater 4 connects interchanger 1, interchanger 1 is connected by the fluid inlet of forced circulation pump with crystal separator 6, the venting port of crystal separator 6 is connected by the inlet mouth of steam-pipe with compressor 7, and the venting port of compressor 7 is connected with the inlet mouth of interchanger 1 shell.
Embodiment 2
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Embodiment 3
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Embodiment 4
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
Embodiment 5
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
Embodiment 6
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
The phlegma liquid outlet of described one-level preheater 8 connects gets back to gas cleaning workshop section.
Embodiment 7
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
The phlegma liquid outlet of described one-level preheater 8 connects gets back to gas cleaning workshop section.
Cooling crystallizer 11, solid-liquid separator 2 12, distillation tower 14, cooling twice crystallizer 15 and a solid-liquid separator 3 16 is also connected with in turn between described solid-liquid separator 1 and fresh feed pump 3, described solid-liquid separator 2 12 connects distillation tower 14 by interchanger 2 13, and described solid-liquid separator 3 16 connects fresh feed pump 3 by interchanger 3 17.
Embodiment 8
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
The phlegma liquid outlet of described one-level preheater 8 connects gets back to gas cleaning workshop section.
Cooling crystallizer 11, solid-liquid separator 2 12, distillation tower 14, cooling twice crystallizer 15 and a solid-liquid separator 3 16 is also connected with in turn between described solid-liquid separator 1 and fresh feed pump 3, described solid-liquid separator 2 12 connects distillation tower 14 by interchanger 2 13, and described solid-liquid separator 3 16 connects fresh feed pump 3 by interchanger 3 17.
Described solid-liquid separator 2 12 connects gets back to crystallization reactor 1.
Embodiment 9
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
The phlegma liquid outlet of described one-level preheater 8 connects gets back to gas cleaning workshop section.
Cooling crystallizer 11, solid-liquid separator 2 12, distillation tower 14, cooling twice crystallizer 15 and a solid-liquid separator 3 16 is also connected with in turn between described solid-liquid separator 1 and fresh feed pump 3, described solid-liquid separator 2 12 connects distillation tower 14 by interchanger 2 13, and described solid-liquid separator 3 16 connects fresh feed pump 3 by interchanger 3 17.
Described solid-liquid separator 2 12 connects gets back to crystallization reactor 1.
Described solid-liquid separator 3 16 connects gets back to a cooling crystallizer 11.
Embodiment 10
The present embodiment is substantially the same manner as Example 1, on this basis:
Described compressor 7 is centrifugal compressor.
Described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
Described preheater 4 is divided into one-level preheater 8 and secondary preheater 9.
The phlegma liquid outlet of described interchanger 1 is connected container for storing liquid 10 with the phlegma liquid outlet of secondary preheater 9, and the liquid outlet of container for storing liquid 10 connects the fluid inlet of one-level preheater 8 shell.
The phlegma liquid outlet of described one-level preheater 8 connects gets back to gas cleaning workshop section.
Cooling crystallizer 11, solid-liquid separator 2 12, distillation tower 14, cooling twice crystallizer 15 and a solid-liquid separator 3 16 is also connected with in turn between described solid-liquid separator 1 and fresh feed pump 3, described solid-liquid separator 2 12 connects distillation tower 14 by interchanger 2 13, and described solid-liquid separator 3 16 connects fresh feed pump 3 by interchanger 3 17.
Described solid-liquid separator 2 12 connects gets back to crystallization reactor 1.
Described solid-liquid separator 3 16 connects gets back to a cooling crystallizer 11.
The leakage fluid dram of described distillation tower 14 passes through the shell side connecting secondary cooling crystallizer 15 of interchanger 2 13.
Claims (10)
1. recycle a thermo-compression evaporation system for gas cleaning by product, it is characterized in that: comprise crystallization reactor (1), solid-liquid separator one (2), fresh feed pump (3), preheater (4), interchanger one (5), crystal separator (6), compressor (7); The discharge port of described crystallization reactor (1) connects solid-liquid separator one (2), the liquid outlet of solid-liquid separator one (2) connects fresh feed pump (3), fresh feed pump (3) connects preheater (4), the liquid outlet of preheater (4) connects interchanger one (5), interchanger one (5) is connected by the fluid inlet of forced circulation pump with crystal separator (6), the venting port of crystal separator (6) is connected by the inlet mouth of steam-pipe with compressor (7), and the venting port of compressor (7) is connected with the inlet mouth of interchanger one (5) shell.
2. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 1, is characterized in that: described compressor (7) is centrifugal compressor.
3. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 2, is characterized in that: described centrifugal compressor is thtee-stage shiplock, and compressor electric motor joins 160Kw.
4. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 1, is characterized in that: described preheater (4) is divided into one-level preheater (8) and secondary preheater (9).
5. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 4, it is characterized in that: the phlegma liquid outlet of described interchanger one (5) is connected container for storing liquid (10) with the phlegma liquid outlet of secondary preheater (9), the liquid outlet of container for storing liquid (10) connects the fluid inlet of one-level preheater (8) shell.
6. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 4, is characterized in that: the phlegma liquid outlet of described one-level preheater (8) connects gets back to gas cleaning workshop section.
7. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 1, it is characterized in that: between described solid-liquid separator one (2) and fresh feed pump (3), be also connected with cooling crystallizer (11), solid-liquid separator two (12), distillation tower (14), cooling twice crystallizer (15) and a solid-liquid separator three (16) in turn, described solid-liquid separator two (12) connects distillation tower (14) by interchanger two (13), and described solid-liquid separator three (16) connects fresh feed pump (3) by interchanger three (17).
8. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 7, is characterized in that: described solid-liquid separator two (12) connects gets back to crystallization reactor (1).
9. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 7, is characterized in that: described solid-liquid separator three (16) connects gets back to a cooling crystallizer (11).
10. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 7, is characterized in that: the leakage fluid dram of described distillation tower (14) passes through the shell side connecting secondary cooling crystallizer (15) of interchanger two (13).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420741511.4U CN204325056U (en) | 2014-12-02 | 2014-12-02 | A kind of thermo-compression evaporation system recycling gas cleaning by product |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420741511.4U CN204325056U (en) | 2014-12-02 | 2014-12-02 | A kind of thermo-compression evaporation system recycling gas cleaning by product |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104402162A (en) * | 2014-12-02 | 2015-03-11 | 成都华西堂投资有限公司 | Heat pump evaporation system for recycling flue gas purification byproducts |
| CN106430778A (en) * | 2016-10-18 | 2017-02-22 | 成都华西堂环保科技有限公司 | Treatment method of salt-containing wastewater and production process for preparing sodium chloride, ammonium sulfate and compound fertilizer from salt-containing wastewater |
| CN108455633A (en) * | 2018-01-13 | 2018-08-28 | 安徽金禾实业股份有限公司 | A kind of the salt extraction recovery method and device of synthesis ammonia desulfurization raffinate |
| CN117029087A (en) * | 2023-08-08 | 2023-11-10 | 山东京清节能环保科技有限公司 | Desulfurization slurry waste heat utilization treatment device |
-
2014
- 2014-12-02 CN CN201420741511.4U patent/CN204325056U/en not_active Withdrawn - After Issue
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104402162A (en) * | 2014-12-02 | 2015-03-11 | 成都华西堂投资有限公司 | Heat pump evaporation system for recycling flue gas purification byproducts |
| CN104402162B (en) * | 2014-12-02 | 2016-06-08 | 成都华西堂投资有限公司 | A kind of thermo-compression evaporation system of recycling gas cleaning accessory substance |
| CN106430778A (en) * | 2016-10-18 | 2017-02-22 | 成都华西堂环保科技有限公司 | Treatment method of salt-containing wastewater and production process for preparing sodium chloride, ammonium sulfate and compound fertilizer from salt-containing wastewater |
| CN108455633A (en) * | 2018-01-13 | 2018-08-28 | 安徽金禾实业股份有限公司 | A kind of the salt extraction recovery method and device of synthesis ammonia desulfurization raffinate |
| CN117029087A (en) * | 2023-08-08 | 2023-11-10 | 山东京清节能环保科技有限公司 | Desulfurization slurry waste heat utilization treatment device |
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