CN104402162B - A kind of thermo-compression evaporation system of recycling gas cleaning accessory substance - Google Patents
A kind of thermo-compression evaporation system of recycling gas cleaning accessory substance Download PDFInfo
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- CN104402162B CN104402162B CN201410716684.5A CN201410716684A CN104402162B CN 104402162 B CN104402162 B CN 104402162B CN 201410716684 A CN201410716684 A CN 201410716684A CN 104402162 B CN104402162 B CN 104402162B
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Abstract
The invention provides a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance, comprise crystallization reactor, solid-liquid separator one, feed pump, preheater, heat exchanger one, crystal separator, compressor; The liquid outlet that the discharging opening of described crystallization reactor connects solid-liquid separator one, solid-liquid separator one connects feed pump, feed pump connects preheater, the liquid outlet of preheater connects heat exchanger one, heat exchanger one is connected with the inlet of crystal separator by forced circulation pump, the exhaust outlet of crystal separator is connected with the air inlet of compressor by jet chimney, and the exhaust outlet of compressor is connected with the air inlet of heat exchanger one shell.
Description
Technical field
The present invention relates to flue gases purification field, be specifically related to a kind of heat pump of recycling gas cleaning accessory substance and steamThe system of sending out.
Background technology
In recent years along with air-polluting is more and more serious, people to flue gas particularly the improvement of coal-fired flue-gas proposed moreHigh requirement; National environmental protection portion has issued new " fossil-fuel power plant atmospheric pollutant emission standard " (GB on July 29th, 201113223-2011), the flue dust to flue gas, sulfur dioxide, nitrogen oxide have proposed new emission limit. At present, flue gas desulfurizationEffective means is the wet process of FGD such as ammonia process, sodium method. Above sulfur method all will produce certain density containing sulfate, nitreThe waste liquid of hydrochlorate. Have the characteristics such as salt content is high, slant acidity, while adopting commonsense method to process, effluent quality is difficult to reach discharge markStandard, seems particularly important for the exploitation of the novel process technology of gas cleaning waste water. Especially for the higher ground of environmental requirementDistrict, often requires high slat-containing wastewater " zero-emission ", and this just has higher requirement to high slat-containing wastewater treatment technology. Need be to itProcess, reclaim utility simultaneously, avoid waste. Traditional processing method is to adopt multiple-effect evaporation, causes energy consumption higher.
201110155630.2, name is called the patent of invention of " ammonium sulfate/magnesium sulfate recovery technology after desulfurization ", process flowCheng Wei: raw material → feedstock pump → preheater → 1st effective evaporator → 2nd effect evaporator → triple effect evaporator → condenser → liquid seal trough→ discharge; Admittedly expect part technological process: triple effect evaporator → discharging pump → crystallizer → centrifuge → drying machine → feed bin → bagInstallation. The indirect steam of a certain effect of evaporimeter of this patent can not be directly as this effect thermal source, can only serve as inferior effect or inferior a few effectThermal source. As must be additionally given its energy 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 of recycling gas cleaning accessory substanceSystem. Using the waste liquid after flue gas desulfurization and denitrification as raw material, first reclaim absorbent by crystallization reactor, liquid again through preheating,After forced circulation heating, condensing crystallizing, recycle. This technique is particularly suitable for giving up containing ammonium after smoke treatment desulfurization or denitrationLiquid, reaches the object turning waste into wealth, and has saved the consumption of steam; Meanwhile, the water distilling is capable of circulation to gas cleaning workshop sectionUse using water wisely as moisturizing.
For achieving the above object, the present invention adopts following technical scheme:
A thermo-compression evaporation system of recycling gas cleaning accessory substance, is characterized in that: comprise crystallization reactor, solidLiquid/gas separator one, feed pump, preheater, heat exchanger one, crystal separator, compressor; The discharging opening of described crystallization reactorThe liquid outlet that connects solid-liquid separator one, solid-liquid separator one connects feed pump, and feed pump connects preheater, the fluid of preheaterMouth connection heat exchanger one, heat exchanger one is connected with the inlet of crystal separator by forced circulation pump, the row of crystal separatorGas port is connected with the air inlet of compressor by jet chimney, and the air inlet of the exhaust outlet of compressor and heat exchanger one shell connectsConnect.
The waste liquid that flue gas obtains after wet cleaning reacts with carbonic hydroammonium in crystallization reactor, passes through solid-liquid separatorThe absorbent that solid in one recovery reactant liquor can be used as flue gas is back to gas cleaning workshop section, and liquid, as material liquid, pumps intoPreheater, the material liquid after preheating enters heat exchanger one, in the tube side of heat exchanger one, raise by shell side Steam Heating temperature,Material liquid enters crystal separator under the promotion of forced circulation pump, and crystal separator internal pressure reduces, and material liquid produces flash distillation,The indirect steam that flash distillation produces rises and discharges from jet chimney in crystal separator, and material liquid produces supersaturation becomes nucleusLong, in the time that growing to compared with megacryst, nucleus is deposited to crystal separator bottom; Described indirect steam is done after compressor compressionFor thermal source enters the shell side of heat exchanger one.
Wet cleaning of the present invention refers to wet desulphurization or denitration.
Described preheater is divided into one-level preheater and secondary preheater, effectively utilizes more than boiler afterheat and steam condensate (SC)Heat.
Described compressor is centrifugal compressor, the compact conformation of centrifugal compressor, and size is little, lightweight; Exhaust continuously,Evenly, do not need the devices such as pans; Vibrate littlely, few easy workout part, does not need huge and heavy basic part; Except bearing, machineDevice inside does not need to lubricate, fuel-efficient, and does not pollute compressed gas; Rotating speed is high; A little repair, easy to adjust.
Preferably, described centrifugal compressor is three grades of series connection, and compressor electric motor is joined 160Kw. Compressor series connection can obtainTo higher pressure head, improve indirect steam temperature simultaneously, return to heat exchanger one forced-circulation evaporation as thermal source.
Preferably, the condensate liquid liquid outlet of described heat exchanger one and the condensate liquid liquid outlet of secondary preheater are connected liquid storageTank, the liquid outlet of fluid reservoir connects the inlet of one-level preheater shell. The condensate liquid of heat exchanger one and secondary preheater is doneFor the thermal source of one-level preheater, save the energy.
The condensate liquid liquid outlet connection of described one-level preheater is got back to gas cleaning workshop section and is used and realized as moisturizingZero-emission.
Between solid-liquid separator one of the present invention and feed pump, being also connected with cooler crystallizer, a solid-liquid in turn dividesFrom device two, destilling tower, secondary cooler crystallizer and solid-liquid separator three, described solid-liquid separator two connects by heat exchanger twoDestilling tower, described solid-liquid separator three connects feed pump by heat exchanger three.
The waste liquid of flue gas after wet cleaning sent into crystallization reactor and reacted with carbonic hydroammonium, and after having reacted, liquid entersEnter a cooler crystallizer crystallization, solid-liquid separator two is sent into destilling tower by clear liquid after heat exchanger heating, then distillation is obtainedClear liquid send into the crystallization of secondary cooler crystallizer, solid-liquid separator three is sent into vapo(u)rization system by clear liquid and is removed after heat exchanger heatingExcessive moisture, obtains highly purified ammonium salt solution.
The present invention adopts the system of cooler crystallizer-destilling tower-secondary cooler crystallizer to process ammonium salt mother liquor, secondaryCrystallization is in order to separate out the unreacted impurity such as carbonic hydroammonium and sodium sulphate completely in solution, to reduce supplies consumption simultaneously; DistillationIn order to remove free ammonia and the carbon dioxide in solution.
Solid-liquid separator two of the present invention connects gets back to crystallization reactor. The solid that crystallisation by cooling is separated out is separated outA large amount of sal glauberi, sodium acid carbonate and carbonic hydroammonium, turn back in crystallization reactor and continue to react.
Solid-liquid separator three of the present invention connects gets back to cooler crystallizer No. one time. Secondary crystallisation by cooling is separated out four water sulphurThe mixture of acid sodium and ammonium sulfate, further reduces the sodium sulphate content in ammonium sulfate liquor; Turn back to once cooling knot simultaneouslyFurther crystallisation by cooling in brilliant operation, to improve the product purity of ammonium sulfate.
The exhaust outlet of destilling tower of the present invention connects the bottom of crystallization reactor by booster fan.
In the ammonia that obtains of distillation and carbon dioxide Returning reactor, continue reaction, reduce supplies consumption, and reduce rightThe pollution of environment; By booster fan, gas dispersion is arrived to crystallizer bottom, from the bottom up, utilize crystallizer solution fully to reclaimAmmonia and carbon dioxide.
The leakage fluid dram of described destilling tower is by the shell side connecting secondary cooler crystallizer of heat exchanger two. After a crystallisation by coolingClear liquid reach more than 60 DEG C by carrying out heat exchange with destilling tower bottom fluid, then send into destilling 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 twoInferior cooler crystallizer. The liquid that separation obtains, before sodium sulphate reaches capacity, is sent to secondary cooler crystallizer by filtrate and entersRow crystallisation by cooling, the vapo(u)rization system that enters again postorder after sodium sulphate is separated out, thereby the purity of guarantee ammonium sulfate product.
Preferably, described is once DTB cooler crystallizer with secondary cooler crystallizer, and the ability of crystallization is high.
Described solid-liquid separator one is centrifugal separator or band filter.
Equipment and materials of the present invention and with the selection for pipeline TA2 material of material contact portion.
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. MaterialIn the tube side of heat exchanger one, raise by shell side Steam Heating temperature, under the promotion of forced circulation pump, enter after crystal separatorPressure decreased produces flash distillation, and the indirect steam of generation is discharged from steam pipework, and material produces supersaturation crystallization sedimentation, forced circulationEvaporate the indirect steam producing thermal source as heat exchanger after compressor compresses. Save the consumption of steam, saved every yearRaw steam 7000t left and right, has realized energy-conservation. Reduce more than 50% floor space simultaneously.
2, the condensate liquid of secondary preheater of the present invention and heat exchanger is as the thermal source of one-level preheater, and meanwhile, one-level is pre-The condensate liquid of hot device is got back to gas cleaning workshop section and is used as moisturizing, the water-saving while, has realized zero-emission.
3, because material contains a large amount of acid ion (Cl-，NO3-), therefore adopt forced-circulation evaporation crystallization processes, can be effectiveAvoid pipe plugging by crystallization, equipment and materials and with the selection for pipeline TA2 material of material contact portion, ensure service life of equipment.
4, the present invention adopts centrifugal compressor as heat pump, and the little a part of electric energy of itself consumption when work but can be fromIn indirect steam, extract 4-7 doubly to electric energy, promote temperature and utilize. The compact conformation of compression centrifuge own, size is little, weightGently; Exhaust continuously, evenly, does not need the devices such as pans; Vibrate littlely, few easy workout part, does not need huge and heavy basic part;Except bearing, machine intimate does not need to lubricate, fuel-efficient, and does not pollute compressed gas; Rotating speed is high; A little repair, easy to adjust.
5, system of the present invention, by the waste liquid of gas cleaning, comprises that the waste liquid of desulfurization or denitration reacts with carbonic hydroammonium, anti-Answer and in liquid, contain the ammonium salt such as ammonium sulfate and ammonium nitrate, solid-liquid separator one separates the absorbent that the solid obtaining can be used as flue gas and returnsFor gas cleaning workshop section. Adopt the system of cooler crystallizer-destilling tower-secondary cooler crystallizer to process ammonium salt mother liquor,Secondary crystallization is in order to separate out the unreacted impurity such as carbonic hydroammonium and sodium sulphate completely in solution, to reduce supplies consumption simultaneously;Distillation is in order to remove free ammonia and the carbon dioxide in solution. Obtain highly purified ammonium salt solution. The nitrogen content of final productsMeet the producing ammonium sulfate byproduct product requirement of electric power standard: total nitrogen >=18%, appearance white particle.
6, solid-liquid separator of the present invention two connects and gets back to crystallization reactor, the ten water sulphur that crystallisation by cooling is separated outAcid sodium, sodium acid carbonate and carbonic hydroammonium solid turn back in crystallization reactor and continue to react; Solid-liquid separator three connects gets back to oneInferior cooler crystallizer, the mixture solid of what secondary crystallisation by cooling was separated out separate out four aqueous sodium persulfates and ammonium sulfate turns back to once coldBut crystallisation by cooling in Crystallization Procedure; Solid-liquid separator four connects gets back to secondary cooler crystallizer, contains large in the solution after separationThe ammonium sulfate of amount, gets back to crystallisation by cooling in secondary crystallisation by cooling operation and separates out. More than operation is the strong guarantee of ammonium sulfate yield,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 destilling tower passes through the shell side connecting secondary cooler crystallizer of heat exchanger two, make once cooling knotClear liquid after crystalline substance is by carrying out heat exchange with destilling tower bottom fluid, and temperature reaches more than 60 DEG C, then sends into destilling tower, saves distillationSteam consumption, reduces plant energy consumption.
8, connect the bottom of crystallization reactor by booster fan due to the exhaust outlet of destilling tower, the ammonia that obtains of distillation andIn carbon dioxide Returning reactor, continue reaction, gas is sent into from the bottom of crystallizer, be distributed to bottom, from the bottom up, makeCrystallizer solution fully reacts with ammonia and carbon dioxide, reclaims ammonia and carbon dioxide. When reducing supplies consumption,Reduce the pollution to environment.
Brief description of the drawings
Fig. 1 is the thermo-compression evaporation system construction drawing of gas cleaning accessory substance 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.
In figure, be labeled as: 1, crystallization reactor, 2, solid-liquid separator one, 3, feed pump, 4, preheater, 5, heat exchanger one,6, crystal separator, 7, compressor, 8, one-level preheater, 9, secondary preheater, 10, fluid reservoir, 11, a cooler crystallizer,12, solid-liquid separator two, 13, heat exchanger two, 14, destilling tower, 15, secondary cooler crystallizer, 16, solid-liquid separator three, 17, changeHot device three, 18, solid-liquid separator four.
Detailed description of the invention
Below in conjunction with detailed description of the invention, essentiality content of the present invention is described in further detail.
Embodiment 1
A thermo-compression evaporation system of recycling gas cleaning accessory substance, is characterized in that: comprise crystallization reactor 1,Solid-liquid separator 1, feed pump 3, preheater 4, heat exchanger 1, crystal separator 6, compressor 7; Described crystallization reactor 1The discharging opening liquid outlet that connects solid-liquid separator 1, solid-liquid separator 1 connect feed pump 3, feed pump 3 connects preheater4, the liquid outlet of preheater 4 connects heat exchanger 1, and heat exchanger 1 connects by the inlet of forced circulation pump and crystal separator 6Connect, the exhaust outlet of crystal separator 6 is connected with the air inlet of compressor 7 by jet chimney, the exhaust outlet of compressor 7 and heat exchangeThe air inlet of device one 5 shells connects.
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 three grades of series connection, and compressor electric motor is joined 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 three grades of series connection, and compressor electric motor is joined 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 three grades of series connection, and compressor electric motor is joined 160Kw.
Described preheater is divided into one-level preheater 8 and secondary preheater 9.
The condensate liquid liquid outlet of described heat exchanger 1 is connected fluid reservoir 10 with the condensate liquid liquid outlet of secondary preheater 9, storageThe liquid outlet of flow container 10 connects the inlet of one-level preheater 8 shells.
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 three grades of series connection, and compressor electric motor is joined 160Kw.
Described preheater is divided into one-level preheater 8 and secondary preheater 9.
The condensate liquid liquid outlet of described heat exchanger 1 is connected fluid reservoir 10 with the condensate liquid liquid outlet of secondary preheater 9, storageThe liquid outlet of flow container 10 connects the inlet of one-level preheater 8 shells.
The condensate liquid 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:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 3 17.
Embodiment 8
The present embodiment is substantially the same manner as Example 7, on this basis:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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 cooler crystallizer 11 No. one time.
Embodiment 10
The present embodiment is substantially the same manner as Example 6, on this basis:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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 cooler crystallizer 11 No. one time.
The leakage fluid dram of described destilling tower 14 is by the shell side connecting secondary cooler crystallizer 15 of heat exchanger 2 13.
Embodiment 11
The present embodiment is substantially the same manner as Example 6, on this basis:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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 cooler crystallizer 11 No. one time.
The leakage fluid dram of described destilling tower 14 is by the shell side connecting secondary cooler crystallizer 15 of heat exchanger 2 13.
The exhaust outlet of described destilling 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 twoInferior cooler crystallizer 15.
Described equipment and materials and with the selection for pipeline TA2 material of material contact portion.
Embodiment 12
The present embodiment is substantially the same manner as Example 6, on this basis:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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 cooler crystallizer 11 No. one time.
The leakage fluid dram of described destilling tower 14 is by the shell side connecting secondary cooler crystallizer 15 of heat exchanger 2 13.
The exhaust outlet of described destilling tower 14 connects the bottom of crystallization reactor 1 by booster fan.
Described is once DTB cooler crystallizer with secondary cooler 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 twoInferior cooler crystallizer 15.
Described equipment and materials and with the selection for pipeline TA2 material of material contact portion.
Embodiment 13
The present embodiment is substantially the same manner as Example 6, on this basis:
Between described solid-liquid separator 1 and feed pump 3, be also connected with cooler crystallizer 11, Separation of Solid and Liquid in turnDevice 2 12, destilling tower 14, secondary cooler crystallizer 15 and solid-liquid separator 3 16, described solid-liquid separator 2 12 is by heat exchangeDevice 2 13 connects destilling tower 14, and described solid-liquid separator 3 16 connects feed pump 3 by heat exchanger 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 cooler crystallizer 11 No. one time.
The leakage fluid dram of described destilling tower 14 is by the shell side connecting secondary cooler crystallizer 15 of heat exchanger 2 13.
The exhaust outlet of described destilling tower 14 connects the bottom of crystallization reactor 1 by booster fan.
Described is once DTB cooler crystallizer with secondary cooler 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 twoInferior cooler crystallizer 15.
Described equipment and materials and with the selection for pipeline TA2 material of material contact portion.
Embodiment 14
The wet gas purifying waste of being fuming using sodium acid carbonate as absorbent, as initial material liquid, adopts heat of the present inventionPump vapo(u)rization system, obtains ammonium sulfate by-product volume as following table:
Table 1
The waste liquid that flue gas of the present invention obtains after wet cleaning reacts with carbonic hydroammonium in crystallization reactor, passes through solid-liquidSeparator one reclaims the absorbent that solid in reactant liquor can be used as flue gas and is back to gas cleaning workshop section, and liquid is as raw materialLiquid, pumps into preheater, and the material liquid after preheating enters heat exchanger one, in the tube side of heat exchanger one by shell side Steam Heating temperatureDegree raises, and material liquid enters crystal separator under the promotion of forced circulation pump, and crystal separator internal pressure reduces, and material liquid producesRaw flash distillation, the indirect steam that flash distillation produces rises and discharges from jet chimney in crystal separator, and material liquid produces supersaturation and makesNucleus is grown up, and is deposited to crystal separator bottom in the time that nucleus grows to compared with megacryst; Described indirect steam is pressed through compressorAfter contracting, enter the shell side of heat exchanger one as thermal source.
The flow velocity of described material liquid in preheater is 0.5-3m/s, can strengthen convection heat transfer' heat-transfer by convection system under this flow velocityNumber, improves heat transfer efficiency, reduces the possibility of dirt in tube surface deposition, is to avoid flow velocity to increase to cause power consumption simultaneouslyCross the optimum flow rate of more options.
In described one-level preheater, material liquid is heated to 50-70 DEG C, utilizes distilled water waste heat that raw material is added by 25 DEG CHeat is to 50-70 DEG C, and heat transfer efficiency is best.
In described secondary preheater, material liquid is heated to 90-100 DEG C, utilizes steam to improve and enters circulating evaporatorMaterial temperature, improve circulating evaporator heat transfer efficiency, reduce energy consumption.
In described heat exchanger one, material liquid is heated to 105-108 DEG C, reaches material boiling point, enters crystallizing evaporator,Directly evaporation produces indirect steam.
The gauge pressure of described forced circulation pump is 0.03-0.05MPa, can ensure the temperature of indirect steam under this pressure.
The flow velocity that material liquid enters crystal separator is 1-2.5m/s, neither destroys crystal, again in rational flow rates.
Material liquid produces flash distillation in crystal separator, and the temperature of the indirect steam that flash distillation produces is 80-85 DEG C, and pressure is40-50kPa, provides stable vapor (steam) temperature and pressure, makes the subsequent compression machine can stable operation.
The outlet temperature of described compressor is 106 DEG C, returns to heat exchanger one realize forced-circulation evaporation as thermal source.
Described is once-2 ~ 0 DEG C with the temperature of secondary crystallisation by cooling.
The vapo(u)rizing temperature of described destilling tower is 98 ~ 105 DEG C, removes free ammonia and carbon dioxide in solution.
The pressure of described booster fan exit gas is 0.05-0.08Mpa, ensures that gas fully contacts with solution, reactionCompletely.
Embodiment 16
The present embodiment is substantially the same manner as Example 1, on this basis:
The flow velocity of material 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 material liquid in preheater is 0.5m/s.
In described one-level preheater, material liquid is heated to 50 DEG C, and in secondary preheater, material liquid is heated to 90℃。
Embodiment 18
The present embodiment is substantially the same manner as Example 4, on this basis:
The flow velocity of material liquid in preheater is 3m/s.
In described one-level preheater, material liquid is heated to 70 DEG C, and in secondary preheater, material liquid is heated to 100 DEG C.
In described heat exchanger one, material 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 material liquid in preheater is 1m/s.
In described one-level preheater, material liquid is heated to 55 DEG C, and in secondary preheater, material liquid is heated to 92 DEG C.
In described heat exchanger one, material 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 material liquid in preheater is 2m/s.
In described one-level preheater, material liquid is heated to 65 DEG C, and in secondary preheater, material liquid is heated to 98 DEG C.
In described heat exchanger one, material liquid is heated to 107 DEG C,
The gauge pressure of described forced circulation pump is 0.05MPa,
The flow velocity that material liquid enters crystal separator is 2.5m/s,
Material liquid produces flash distillation in crystal separator, and the temperature of the indirect 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 material liquid in preheater is 2.2m/s.
In described one-level preheater, material liquid is heated to 60 DEG C, and in secondary preheater, material liquid is heated to 95 DEG C.
In described heat exchanger one, material liquid is heated to 106 DEG C,
The gauge pressure of described forced circulation pump is 0.04MPa,
The flow velocity that material liquid enters crystal separator is 1m/s,
Material liquid produces flash distillation in crystal separator, and the temperature of the indirect 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 material liquid in preheater is 1.8m/s.
In described one-level preheater, material liquid is heated to 62 DEG C, and in secondary preheater, material liquid is heated to 96 DEG C.
In described heat exchanger one, material liquid is heated to 106.5 DEG C,
The gauge pressure of described forced circulation pump is 0.042MPa,
The flow velocity that material liquid enters crystal separator is 1.8m/s,
Material liquid produces flash distillation in crystal separator, and the temperature of the indirect steam that flash distillation produces is 82 DEG C, and pressure is 45kPa,
The outlet temperature 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 secondary crystallisation by cooling.
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 secondary crystallisation by cooling.
The vapo(u)rizing temperature of described destilling tower is 105 DEG C, removes free ammonia and carbon dioxide in solution.
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 secondary crystallisation by cooling.
The vapo(u)rizing temperature of described destilling tower is 98 DEG C, removes free ammonia and carbon dioxide in solution.
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 secondary crystallisation by cooling.
The vapo(u)rizing temperature of described destilling tower is 100 DEG C, removes free ammonia and carbon dioxide in solution.
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 secondary crystallisation by cooling.
The vapo(u)rizing temperature of described destilling tower is 102 DEG C, removes free ammonia and carbon dioxide in solution.
The pressure of described booster fan exit gas is 0.06Mpa, ensures that gas fully contacts with solution, reacts completely.
Claims (11)
1. a thermo-compression evaporation system of recycling gas cleaning accessory substance, is characterized in that: comprise crystallization reactor (1),Solid-liquid separator one (2), feed pump (3), preheater (4), heat exchanger one (5), crystal separator (6), compressor (7); DescribedThe discharging opening of crystallization reactor (1) liquid outlet that connects solid-liquid separator one (2), solid-liquid separator one (2) connect feed pump(3), feed pump (3) connects preheater (4), and the liquid outlet of preheater (4) connects heat exchanger one (5), and heat exchanger one (5) is by strongCirculating pump processed is connected with the inlet of crystal separator (6), and the exhaust outlet of crystal separator (6) is by jet chimney and compressor(7) air inlet connects, and the exhaust outlet of compressor (7) is connected with the air inlet of heat exchanger one (5) shell;
Between described solid-liquid separator one (2) and feed pump (3), be also connected with a cooler crystallizer (11) in turn, solid-liquid dividesFrom device two (12), destilling tower (14), secondary cooler crystallizer (15) and solid-liquid separator three (16), described solid-liquid separator two(12) connect destilling tower (14) by heat exchanger two (13), described solid-liquid separator three (16) connects by heat exchanger three (17)Feed pump (3).
2. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 1, is characterized in that:Described compressor (7) is centrifugal compressor.
3. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 2, is characterized in that:Described centrifugal compressor is three grades of series connection, and compressor electric motor is joined 160Kw.
4. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance 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 of recycling gas cleaning accessory substance according to claim 4, is characterized in that:The condensate liquid liquid outlet of described heat exchanger one (5) is connected fluid reservoir (10), liquid storage with the condensate liquid liquid outlet of secondary preheater (9)The liquid outlet of tank (10) connects the inlet of one-level preheater (8) shell.
6. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 4, is characterized in that:The condensate liquid 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 of recycling gas cleaning accessory substance according to claim 1, is characterized in that:Described solid-liquid separator two (12) connects gets back to crystallization reactor (1); Described solid-liquid separator three (16) connects gets back to oneInferior cooler crystallizer (11).
8. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 1, is characterized in that:The exhaust outlet of described destilling tower (14) connects the bottom of crystallization reactor (1) by booster fan.
9. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 1, is characterized in that:Described is once DTB cooler crystallizer with secondary cooler crystallizer.
10. a kind of thermo-compression evaporation system of recycling gas cleaning accessory substance according to claim 1, its feature existsIn: the leakage fluid dram of described destilling tower (14) is by the shell side connecting secondary cooler crystallizer (15) of heat exchanger two (13).
11. a kind of thermo-compression evaporation systems of recycling gas cleaning accessory substance according to claim 1, its feature existsIn: described crystal separator (6) connects solid-liquid separator four (18), and the liquid outlet of solid-liquid separator four (18) connects gets back to twoInferior cooler crystallizer (15).
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| JPS6466826A (en) * | 1987-09-07 | 1989-03-13 | Hitachi Ltd | Misrecording preventing circuit for optical disk device |
| JPH1066826A (en) * | 1996-08-29 | 1998-03-10 | Chiyoda Corp | Flue gas desulfurization method and apparatus therefor |
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| CN101327937A (en) * | 2008-06-19 | 2008-12-24 | 娄爱娟 | Method for reclaiming sulfuric dioxide from flue gas to produce solid ammonium sulfate |
| CN101456635A (en) * | 2008-12-17 | 2009-06-17 | 深圳市能源环保有限公司 | Process and system for treating electric power plant waste water |
| CN102160960A (en) * | 2011-02-25 | 2011-08-24 | 中冶华天工程技术有限公司 | Soda wet desulphurization process and system for sintering flue gas |
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