CN104402162A - Heat pump evaporation system for recycling flue gas purification byproducts - Google Patents
Heat pump evaporation system for recycling flue gas purification byproducts Download PDFInfo
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- CN104402162A CN104402162A CN201410716684.5A CN201410716684A CN104402162A CN 104402162 A CN104402162 A CN 104402162A CN 201410716684 A CN201410716684 A CN 201410716684A CN 104402162 A CN104402162 A CN 104402162A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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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)
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
Abstract
The invention provides a heat pump evaporation system for recycling flue gas purification byproducts. The system comprises a crystallizing reactor, a solid-liquid separator I, a feeding pump, a preheater, a heat exchanger I, a crystallizing separator and a compressor, wherein the discharging hole of the crystallizing reactor is connected with the solid-liquid separator I; the liquid outlet of the solid-liquid separator I is connected with the feeding pump; the feeding pump is connected with the preheater; the liquid outlet of the preheater is connected with the heat exchanger I; the heat exchanger I is connected with the liquid inlet of the crystallizing separator through a forced circulation pump; the gas outlet of the crystallizing separator is connected with the gas inlet of the compressor through a steam pipeline; the gas outlet of the compressor is connected with the gas inlet of a housing layer of the heat exchanger I.
Description
Technical field
The present invention relates to flue gases purification field, be 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, the patent of invention that name is called " ammonium sulfate after desulfurization/magnesium sulfate recovery technology ", 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.
Summary of the invention
In order to solve the problems of the technologies described above, the invention 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 desulfurization or 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 gas cleaning workshop section, water saving.
For achieving the above object, the present invention adopts following technical scheme:
Recycle a thermo-compression evaporation system for gas cleaning by product, it is characterized in that: comprise crystallization reactor, solid-liquid separator one, fresh feed pump, preheater, interchanger one, crystal separator, compressor; The discharge port of described crystallization reactor connects solid-liquid separator one, the liquid outlet of solid-liquid separator one connects fresh feed pump, fresh feed pump connects preheater, the liquid outlet of preheater connects interchanger one, interchanger one 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 one 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 one, raised by shell side steam heating temperature in the tube side of interchanger one, 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 one after compressor compression as thermal source.
Wet purification of the present invention 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 one forced circulation evaporation as thermal source.
Preferably, the phlegma liquid outlet of described interchanger one 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 one 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 of the present invention 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 present invention 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 of the present invention 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 of the present invention 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.
The venting port of distillation tower of the present invention 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 two.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.
Crystal separator of the present invention connects solid-liquid separator four, and the liquid outlet of solid-liquid separator four 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 of the present invention and the selection for pipeline TA2 material with material contact part.
Beneficial effect of the present invention is:
1, in order to adapt to the crystallization and evaporation process of gas cleaning waste liquid, the present invention adopts forced circulation evaporation system.Material is raised by shell side steam heating temperature in the tube side of interchanger one, 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 invention 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, because material contains a large amount of acid ion (Cl
-, NO3
-), therefore adopt forced circulation evaporation crystallization processes, effectively can avoid pipe plugging by crystallization, equipment and materials and the selection for pipeline TA2 material with material contact part, ensure service life of equipment.
4, the present invention 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.
5, present system 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.
6, solid-liquid separator two of the present invention 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.
7, because the leakage fluid dram of distillation tower is by the shell side connecting secondary cooling crystallizer of interchanger two, 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.
8, because the venting port of distillation tower connects the bottom of crystallization reactor by booster fan, distill in the ammonia and carbonic acid gas Returning reactor obtained and continue reaction, the bottom of gas from crystallizer is sent into, be distributed to bottom, from the bottom up, crystallizer solution and ammonia and carbon dioxide are fully reacted, reclaims ammonia and carbonic acid gas.While reducing supplies consumption, reduce the pollution to environment.
Accompanying drawing explanation
Fig. 1 is the thermo-compression evaporation system construction drawing of gas cleaning by product of the present invention.
Fig. 2 is the thermo-compression evaporation system construction drawing of embodiments of the invention 7.
Fig. 3 is the thermo-compression evaporation system construction drawing of embodiments of the invention 9.
Fig. 4 is the thermo-compression evaporation system construction drawing of embodiments of the invention 11-13.
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, 18, solid-liquid separator four.
Embodiment
Below in conjunction with embodiment, essentiality content of the present invention is described in further detail.
Embodiment 1
Recycle a thermo-compression evaporation system for gas cleaning by product, it is characterized in that: 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 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 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 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:
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 7, on this basis:
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:
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 6, on this basis:
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.
Embodiment 11
The present embodiment is substantially the same manner as Example 6, on this basis:
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.
The venting port of described distillation tower 14 connects the bottom of crystallization reactor 1 by booster fan.
Described crystal separator 6 connects solid-liquid separator 4 18, and the liquid outlet of solid-liquid separator 4 18 connects gets back to cooling twice crystallizer 15.
Described equipment and materials and the selection for pipeline TA2 material with material contact part.
Embodiment 12
The present embodiment is substantially the same manner as Example 6, on this basis:
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.
The venting port of described distillation tower 14 connects the bottom of crystallization reactor 1 by booster fan.
Described is once DTB cooling crystallizer with cooling twice crystallizer.
Described crystal separator 6 connects solid-liquid separator 4 18, and the liquid outlet of solid-liquid separator 4 18 connects gets back to cooling twice crystallizer 15.
Described equipment and materials and the selection for pipeline TA2 material with material contact part.
Embodiment 13
The present embodiment is substantially the same manner as Example 6, on this basis:
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.
The venting port of described distillation tower 14 connects the bottom of crystallization reactor 1 by booster fan.
Described is once DTB cooling crystallizer with cooling twice crystallizer.
Described crystal separator 6 connects solid-liquid separator 4 18, and the liquid outlet of solid-liquid separator 4 18 connects gets back to cooling twice crystallizer 15.
Described equipment and materials and the selection for pipeline TA2 material with material contact part.
Embodiment 14
Wet gas purifying waste of being fuming using sodium bicarbonate as absorption agent, as initial stock liquid, adopts thermo-compression evaporation system of the present invention, obtains ammonium sulfate by-product volume as following table:
Table 1
The waste liquid that flue gas of the present invention 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 one, raised by shell side steam heating temperature in the tube side of interchanger one, 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 one after compressor compression as thermal source.
The flow velocity of described stock liquid in preheater is 0.5-3m/s, convective heat-transfer coefficient can be strengthened under this flow velocity, improve heat transfer efficiency, reduce the possibility that dirt deposits at tube surface, be avoid flow velocity to increase to cause power consumption to cross the optimum flow rate of more options simultaneously.
In described one-level preheater, stock liquid is heated to 50-70 DEG C, utilizes distilled water waste heat that raw material is heated to 50-70 DEG C by 25 DEG C, and heat transfer efficiency is best.
In described secondary preheater, stock liquid is heated to 90-100 DEG C, utilizes steam to improve the material temperature entering circulating evaporator, improves circulating evaporator heat transfer efficiency, reduce energy consumption.
In described interchanger one, stock liquid is heated to 105-108 DEG C, reaches material boiling point, enters evaporative crystallizer, and directly evaporation produces secondary steam.
The gauge pressure of described forced circulation pump is 0.03-0.05MPa, can ensure the temperature of secondary steam at this pressure.
The flow velocity that stock liquid enters crystal separator is 1-2.5m/s, neither destroys crystal, again in rational flow rates.
Stock liquid produces flash distillation in crystal separator, and the temperature of the secondary steam that flash distillation produces is 80-85 DEG C, and pressure is 40-50kPa, provides stable vapor temperature and pressure, enables the steady running of subsequent compression machine.
The temperature out of described compressor is 106 DEG C, returns to interchanger one realize forced circulation evaporation as thermal source.
Described is once-2 ~ 0 DEG C with the temperature of cooling twice crystallization.
The distillation temperature of described distillation tower is 98 ~ 105 DEG C, the free ammonia in removing solution and carbonic acid gas.
The pressure of described booster fan exit gas is 0.05-0.08Mpa, ensures that gas fully contacts with solution, reacts completely.
Embodiment 16
The present embodiment is substantially the same manner as Example 1, on this basis:
The flow velocity of stock liquid in preheater is 0.6m/s.
Embodiment 17
The present embodiment is substantially the same manner as Example 4, on this basis:
The flow velocity of stock liquid in preheater is 0.5m/s.
In described one-level preheater, stock liquid is heated to 50 DEG C, and in secondary preheater, stock liquid is heated to 90 DEG C.
Embodiment 18
The present embodiment is substantially the same manner as Example 4, on this basis:
The flow velocity of stock liquid in preheater is 3m/s.
In described one-level preheater, stock liquid is heated to 70 DEG C, and in secondary preheater, stock liquid is heated to 100 DEG C.
In described interchanger one, stock liquid is heated to 108 DEG C,
Embodiment 19
The present embodiment is substantially the same manner as Example 7, on this basis:
The flow velocity of stock liquid in preheater is 1m/s.
In described one-level preheater, stock liquid is heated to 55 DEG C, and in secondary preheater, stock liquid is heated to 92 DEG C.
In described interchanger one, stock liquid is heated to 105 DEG C,
The gauge pressure of described forced circulation pump is 0.03MPa,
Embodiment 20
The present embodiment is substantially the same manner as Example 7, on this basis:
The flow velocity of stock liquid in preheater is 2m/s.
In described one-level preheater, stock liquid is heated to 65 DEG C, and in secondary preheater, stock liquid is heated to 98 DEG C.
In described interchanger one, stock liquid is heated to 107 DEG C,
The gauge pressure of described forced circulation pump is 0.05MPa,
The flow velocity that stock liquid enters crystal separator is 2.5m/s,
Stock liquid produces flash distillation in crystal separator, and the temperature of the secondary steam that flash distillation produces is 85 DEG C, and pressure is 50kPa,
Embodiment 21
The present embodiment is substantially the same manner as Example 13, on this basis:
The flow velocity of stock liquid in preheater is 2.2m/s.
In described one-level preheater, stock liquid is heated to 60 DEG C, and in secondary preheater, stock liquid is heated to 95 DEG C.
In described interchanger one, stock liquid is heated to 106 DEG C,
The gauge pressure of described forced circulation pump is 0.04MPa,
The flow velocity that stock liquid enters crystal separator is 1m/s,
Stock liquid produces flash distillation in crystal separator, and the temperature of the secondary steam that flash distillation produces is 80 DEG C, and pressure is 40kPa,
Embodiment 22
The present embodiment is substantially the same manner as Example 14, on this basis:
The flow velocity of stock liquid in preheater is 1.8m/s.
In described one-level preheater, stock liquid is heated to 62 DEG C, and in secondary preheater, stock liquid is heated to 96 DEG C.
In described interchanger one, stock liquid is heated to 106.5 DEG C,
The gauge pressure of described forced circulation pump is 0.042MPa,
The flow velocity that stock liquid enters crystal separator is 1.8m/s,
Stock liquid produces flash distillation in crystal separator, and the temperature of the secondary steam that flash distillation produces is 82 DEG C, and pressure is 45kPa,
The temperature out of described compressor is 106 DEG C.
Embodiment 23
The present embodiment is substantially the same manner as Example 8, on this basis:
Described is once-2 DEG C with the temperature of cooling twice crystallization.
Embodiment 24
The present embodiment is substantially the same manner as Example 10, on this basis:
Described is once 0 DEG C with the temperature of cooling twice crystallization.
The distillation temperature of described distillation tower is 105 DEG C, the free ammonia in removing solution and carbonic acid gas.
Embodiment 25
The present embodiment is substantially the same manner as Example 11, on this basis:
Described is once-1.8 DEG C with the temperature of cooling twice crystallization.
The distillation temperature of described distillation tower is 98 DEG C, the free ammonia in removing solution and carbonic acid gas.
The pressure of described booster fan exit gas is 0.05Mpa, ensures that gas fully contacts with solution, reacts completely.
Embodiment 26
The present embodiment is substantially the same manner as Example 12, on this basis:
Described is once-1.5 DEG C with the temperature of cooling twice crystallization.
The distillation temperature of described distillation tower is 100 DEG C, the free ammonia in removing solution and carbonic acid gas.
The pressure of described booster fan exit gas is 0.08Mpa, ensures that gas fully contacts with solution, reacts completely.
Embodiment 27
The present embodiment is substantially the same manner as Example 13, on this basis:
Described is once-1 DEG C with the temperature of cooling twice crystallization.
The distillation temperature of described distillation tower is 102 DEG C, the free ammonia in removing solution and carbonic acid gas.
The pressure of described booster fan exit gas is 0.06Mpa, ensures that gas fully contacts with solution, reacts completely.
Claims (13)
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 as moisturizing.
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); Described solid-liquid separator three (17) connects gets back to a cooling crystallizer (11).
9. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 7, is characterized in that: the venting port of described distillation tower (14) connects the bottom of crystallization reactor (1) by booster fan.
10. a kind of thermo-compression evaporation system recycling gas cleaning by product according to claim 7, is characterized in that: described is once DTB cooling crystallizer with cooling twice crystallizer.
11. a kind of thermo-compression evaporation systems 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 (17).
12. a kind of thermo-compression evaporation systems recycling gas cleaning by product according to claim 7, it is characterized in that: described crystal separator (6) connects solid-liquid separator four (18), the liquid outlet of solid-liquid separator four (18) connects gets back to cooling twice crystallizer (15).
13. a kind of thermo-compression evaporation systems recycling gas cleaning by product according to any one of claim 1-12, is characterized in that: described equipment and materials and the selection for pipeline TA2 material with material contact part.
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