CN105967425A - Coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation - Google Patents
Coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation Download PDFInfo
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- CN105967425A CN105967425A CN201610514201.2A CN201610514201A CN105967425A CN 105967425 A CN105967425 A CN 105967425A CN 201610514201 A CN201610514201 A CN 201610514201A CN 105967425 A CN105967425 A CN 105967425A
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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
- 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
- C02F1/06—Flash 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
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- Hydrology & Water Resources (AREA)
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- Environmental & Geological Engineering (AREA)
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Abstract
The invention discloses a coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and a coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation. The coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation comprises a medium-pressure flashing tower, a low-pressure flash tank, a vacuum flash tank, a clarifying tank, a grey water groove, a deaerator, a mortar trough, a vacuum flashing top condenser, a vacuum gas-liquid separation tank, a rectifying tower, a waste heat boiler, a medium-pressure flashing gas condenser, a medium-pressure flash separation tank, an acidic gas cooler, a rich ammonia condenser and a rich ammonia condensation separation tank. The coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and the coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation can be used for effectively solving the problems of high ammonia content, energy source waste, environmental pollution and complicated operation of an existing grey water system.
Description
Technical field
The present invention relates to Coal Chemical Industry ash water-treatment technology field, particularly relate to a kind of coal reducing ammonia accumulation
Chemical industry buck flash distillation processing system and technique.
Background technology
At present, representative entrained flow bed gasification technology includes that using water-coal-slurry is the texaco gasification of raw material
Stove and the GSP gasification furnace and the space flight stove that use dried coal powder to be raw material, all things considered, both technique all has
Safe and stable, the feature of long-term operation, but due to ash water system, to there is ammonia content too high, a large amount of ammonia
Circulative accumulation in systems, the irrational problem of Energy harvesting needs to solve further.
Coal-water slurry gasification is a kind of flow process that the most domestic coal gasification is commonly used, and its buck processes system
System is as shown in Figure 1.Gasification workshop section carbon washes tower and the High Temperature High Pressure Heisui River of gasification furnace generation, enters through choke valve
Entering middle pressure flash column 1, the top flashed vapour of middle pressure flash column 1 is by ash water-to-water heat exchanger 11 and oxygen-eliminating device 6
Water outlet heat exchange after, in entrance press flash separation tank 10, middle pressure flash separation tank 10 separate gas phase be sent to
C0 conversion section, liquid phase enters oxygen-eliminating device 6, and middle pressure flash column 1 lower liquid phase enters low pressure flash chamber 2；
The top flashed vapour of low pressure flash chamber 2 enters oxygen-eliminating device 6, the lower liquid of low pressure flash chamber 2 with from slag
Water pump enters vacuum flasher 3 together with the Heisui River of gasification furnace start-stop car；The upper gaseous phase of vacuum flasher 3
The port of export is connected to the entrance point of vacuum knockout drum 9, vacuum gas through vacuum flashing evaporator overhead condenser 8
The upper gaseous phase port of export of liquid knockout drum 9 connects vacuum pump, the vacuum knockout drum 9 lower liquid phase port of export
Connecting oxygen-eliminating device 6 entrance point, the lower liquid phase port of export of vacuum flasher 3 is connected to the import of defecator 4
End, the top clear liquor port of export of described defecator 4 is connected to the entrance point of ash water tank 5, under defecator
Portion's mortar port of export connects mortar-trough 7；Bottom described mortar-trough 7, mortar outlet connects mortar processed
Device；The port of export of described ash water tank 5 connects sewage disposal system and oxygen-eliminating device 6；Middle pressure flash separation tank
The bottom liquid of 10, the top flashed vapour of low pressure flash chamber 2, vacuum knockout drum 9 bottom liquid phases,
Ash water tank 5 water outlet and low pressure flash vapour are all sent to deoxygenation groove 6, and the buck in deoxygenation groove is through bottom line and divides
Powder mixing after enter centrifugal pump, after pressurization through ash water-to-water heat exchanger 11 heating after degassing chemical industry section scrubbing tower.
Described coal-water slurry gasification has the disadvantage in that
Middle pressure flash column 1, low pressure flash chamber 2, vacuum flasher 3 flashed vapour in contain ammonia the most in a large number,
Middle pressure flash column 1, vacuum flasher 3 flashed vapour condensed after, then after gas-liquid separation, liquid after separation
Entering deoxygenation groove 6, the flashed vapour of low pressure flash chamber 2 is directly entered deoxygenation groove.Necessarily substantial amounts of ammonia is brought into
Deoxygenation groove 6, deoxygenation groove 6 buck circulating and recovering, to scrubbing tower, causes ammonia and constantly follows in ash water system
Ring adds up, and causes ammonia density in ash water system high, not only increases the magnitude of recruitment of fresh water, and after increasing
Continuous biochemical treatment system intractability and expense.
It is desirable to have a kind of reduce ammonia accumulation Coal Chemical Industry buck flash distillation processing system and technique, described in subtract
Coal Chemical Industry buck flash distillation processing system and the technique of few ammonia accumulation can effectively solve in existing ash water system
Ammonia content is too high, energy waste, environmental pollution and the problem of complex operation.
Summary of the invention
It is an object of the invention to provide a kind of Coal Chemical Industry buck flash distillation processing system reducing ammonia accumulation and work
Skill overcomes the above-mentioned problems in the prior art.
For achieving the above object, the present invention provide a kind of reduce ammonia accumulation Coal Chemical Industry buck flash distillation process be
System, the system that the Coal Chemical Industry buck flash distillation of described minimizing ammonia accumulation processes includes: middle pressure flash column, low pressure are dodged
Steaming pot, vacuum flasher, defecator, ash water tank, oxygen-eliminating device, mortar-trough, vacuum flashing evaporator overhead condenser,
Vacuum knockout drum, rectifying column, waste heat boiler, middle pressure flashed vapour condenser, middle pressure flash separation tank,
Sour gas cooler, rich ammonia condenser, rich ammonia condensing knockout drum；The upper gaseous phase of medium pressure flash column
The port of export is connected with the entrance point of described waste heat boiler by pipeline, and the port of export of described waste heat boiler is through described
Middle pressure flashed vapour condenser connects medium pressure flash separation tank and carries out gas-liquid separation, medium pressure flash separation
Outlet side, tank top connects the bottom of described rectifying column, the lower liquid phase port of export of medium pressure flash separation tank
The top of described rectifying column is connected through pump；The lower liquid phase port of export of medium pressure flash column is connected to described low
The entrance point of pressure flash tank；The upper gaseous phase port of export of described low pressure flash chamber connects under described rectifying column
Portion；The lower liquid phase port of export of described low pressure flash chamber is connected to the entrance point of described vacuum flasher；Described
Rectifier outlet side is connected to sulfur recovery unit through sour gas cooler, the middle part side line of described rectifying column
Outlet connects the entrance point of described rich ammonia condenser, is connected to described rich ammonia through described rich ammonia condenser
Condensation separation tank, the upper gas of described rich ammonia condensing knockout drum does desulfurizing agent, described rich ammonia condensing separation
The bottom liquid outlet end of tank is connected to described rectifying column as backflow；The bottom liquid phases outlet of described rectifying column
End connects the entrance point of described oxygen-eliminating device；The upper gaseous phase port of export of described vacuum flasher is through described vacuum
Flash distillation evaporator overhead condenser is connected to the entrance point of described vacuum knockout drum, described vacuum knockout drum
The upper gaseous phase port of export connects vacuum pump, and the lower liquid phase port of export of described vacuum knockout drum connects described
The entrance point of oxygen-eliminating device, the lower liquid phase port of export of described vacuum flasher is connected to the import of described defecator
End, the top clear liquor port of export of described defecator is connected to the entrance point of described ash water tank, described clarification
The groove bottom mortar port of export connects described mortar-trough；The bottom mortar port of export of described mortar-trough connects mortar and takes off
Water treatment facilities；The port of export of described ash water tank connects sewage disposal system and described oxygen-eliminating device, described deoxygenation
The liquid-phase outlet end of device connects scrubbing tower through high-pressure pump.
The technique of the system that the Coal Chemical Industry buck flash distillation using above-mentioned minimizing ammonia to accumulate processes comprises the following steps:
(1) gasification furnace of coal gasification and carbon wash Heisui River of tower through overregulate valve sequentially enter middle pressure flash column,
Low pressure flash chamber and vacuum flasher carry out flash distillation process；
(2) the coal gasification gasification Heisui River after step (1) flash distillation processes, enters defecator and removes solid
Grain, it is achieved solid-liquid separation, top water outlet is returned gasification system after entering deoxygenation groove deoxygenation and is recycled；
(3) flashed vapour that medium pressure flash column flashes off contains NH3And H2S、CO、CO2、
COS gas, utilizes the saturated low-pressure steam of waste heat boiler by-product, after reclaiming heat, during partial condensation enters
Pressure flash separation tank carries out gas-liquid separation, gives vent to anger entrance rectifier bottoms in top, and bottom liquid enters rectifying column
Top；
(4) flashed vapour that flashes off of described low pressure flash chamber contains NH3And H2S、CO、CO2、
COS gas, is directly entered rectifier bottoms as rectification thermal source；
(5) ammonia that in the middle part of rectifying column, side take-off is qualified, wherein H2S content ＜ 10PPM, as item
Supplementing of mesh supporting boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2Sour gas with COS
Body, removes sulfur recovery system；The qualified water outlet in bottom returns deoxygenation groove as supplementary water.
The present invention also provides for the system that the another kind of Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes, described another
Kind reduce ammonia accumulation Coal Chemical Industry buck flash distillation process system include: high pressure flash tower, middle pressure flash column,
Low pressure flash chamber, vacuum flasher, defecator, ash water tank, oxygen-eliminating device, mortar-trough, vacuum flashing top
Condenser, vacuum knockout drum, rectifying column, waste heat boiler, high pressure flash gas condenser, high pressure flash
Knockout drum, sour gas cooler, rich ammonia condenser, rich ammonia condensing knockout drum；Described high pressure flash tower
The upper gaseous phase port of export connects the entrance point of described waste heat boiler, and the port of export of described waste heat boiler is through described height
Pressure flashed vapour condenser connects described high pressure flash knockout drum and carries out gas-liquid separation, described high pressure flash knockout drum
Outlet side, top connect described rectifying column bottom, the lower liquid phase port of export of described high pressure flash knockout drum
The top of described rectifying column is entered through pump；The lower liquid phase port of export of described high pressure flash tower is connected to described
The entrance point of middle pressure flash column；The upper gaseous phase port of export of medium pressure flash column enters under described rectifying column
Portion；The lower liquid phase port of export of medium pressure flash column is connected to the entrance point of described low pressure flash chamber；Described
The upper gaseous phase port of export of low pressure flash chamber connects the bottom of described rectifying column；The bottom of described low pressure flash chamber
Liquid-phase outlet end is connected to the entrance point of described vacuum flasher；Described rectifier exhaust outlets end is through acid
Property Gas Cooler be connected to sulfur recovery unit, in the middle part of described rectifying column, side line outlet connects described rich ammonia condensation
The entrance point of device, is connected to described rich ammonia condensing knockout drum, described rich ammonia condensing through described rich ammonia condenser
Knockout drum upper gas does desulfurizing agent, and bottom liquid backflow end is connected to described rectifying column as backflow；Institute
The bottom liquid phases port of export stating rectifying column connects the entrance point of described oxygen-eliminating device；The top of described vacuum flasher
Gaseous phase outlet end, through described vacuum flashing evaporator overhead condenser, is connected to the import of described vacuum knockout drum
End, the upper gaseous phase port of export of described vacuum knockout drum connects vacuum pump, described vacuum knockout drum
The lower liquid phase port of export connect described oxygen-eliminating device entrance point, described vacuum flasher lower liquid phase outlet
End is connected to the entrance point of described defecator, and the top clear liquor port of export of described defecator is connected to described
The entrance point of ash water tank, the bottom mortar port of export of described defecator connects described mortar-trough；Described mortar-trough
The outlet of bottom mortar connect mortar dehydration treatment equipment；The port of export of described ash water tank connects sewage disposal system
System and described oxygen-eliminating device, the liquid-phase outlet end of described oxygen-eliminating device is connected to scrubbing tower through high-pressure pump.
The technique using the system that the above-mentioned another kind of Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes include with
Lower step:
(1) gasification furnace of coal gasification and carbon wash Heisui River of tower through overregulate valve sequentially enter high pressure flash tower,
Middle pressure flash column, low pressure flash chamber and vacuum flasher carry out flash distillation process；
(2) defecator removing solid particle is entered in the coal gasification gasification Heisui River after step (1) flash distillation processes,
Realizing solid-liquid separation, top water outlet is returned gasification system after entering deoxygenation groove deoxygenation and is recycled；
(3) flashed vapour that high pressure flash tower flashes off contains NH3And H2S、CO、CO2、COS
Gas, after utilizing waste heat boiler to reclaim heat, partial condensation enters high pressure flash knockout drum and carries out gas-liquid separation,
Giving vent to anger entrance rectifier bottoms in top, bottom liquid enters rectifier；
(4) in, the flashed vapour that flashes off of low pressure flash chamber contain NH3And H2S、CO、CO2、
The gases such as COS, are directly entered rectifier bottoms as rectification thermal source.
(5) ammonia that in the middle part of rectifying column, side take-off is qualified, wherein H2S content ＜ 10PPM, as project
Supplementing of supporting boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2, COS sour gas,
Remove sulfur recovery system；The qualified water outlet in bottom returns deoxygenation groove as supplementary water.
Preferably, described deoxygenation groove is atmospheric pressure device, and water temperature is 109 DEG C, is directly entered washing by high-pressure pump
Tower.
Preferably, described deoxygenation groove is equipment with pressure, and temperature is 145 DEG C, is directly entered washing by high-pressure pump
Tower.
Preferably, for ensureing the separation purity of weak ammonia, the low of one 0.5MPaG at the bottom of rectifying tower, is being added
Pressure saturated vapor is as thermal source.
Preferably, medium pressure flash column flashed vapour out heats described rectification tower bottoms by reboiler,
Entering from described rectifier after condensation, the still liquid of heated gasification enters described rectification as steam source of the gas
The bottom of tower.
Preferably, described high pressure flash tower flashed vapour out heats described rectification tower bottoms by reboiler,
Entering from described rectifier after condensation, the still liquid of heated gasification enters described rectification as steam source of the gas
The bottom of tower.
The invention provides a kind of Coal Chemical Industry buck flash distillation processing system reducing ammonia accumulation and technique, the present invention
In high pressure flash tower flash distillation by after a series of energy recovery unit enter rectifying column, middle pressure flash column and
The top flashed vapour of low pressure flash chamber is directly entered rectifying column, by the NH in flashed vapour3、H2S、CO、
CO2, the gas such as COS carry out collection respectively, concentrate and effectively have collected the ammonia in ash water system, receive
The ammonia of collection supplements as the weak ammonia of desulfurization；The H of the collection on top2S、CO、CO2、COS
Going sulfur recovery, solve equipment and the problem of pipeline scale, bottom obtains the liquid that ammonia content is relatively low, is back to
Deoxygenation groove, the concentration of ash water system ammonia reduces 40%～50%, will save the consumption of fresh water, and alleviates
Subsequent biochemical intractability.Present invention achieves coalification Wastewater Concentrated height ammonia nitrogen, energy efficient, and
It is effectively reduced subsequent biochemical and processes load, it is achieved discharged wastewater met the national standard, and the present invention reduces ammonia accumulation
Coal Chemical Industry buck flash distillation processing system and technique fully reclaim valuable ammonia resource, it is to avoid secondary pollution.
Accompanying drawing explanation
Fig. 1 is that traditional coal gasification buck processes process schematic representation.
Fig. 2 is Coal Chemical Industry buck flash distillation processing system and the technique of three stages of flashing of technique reducing ammonia accumulation
Schematic flow sheet.
Fig. 3 is Coal Chemical Industry buck flash distillation processing system and the technique of level Four flash distillation of technique reducing ammonia accumulation
Schematic flow sheet.
Detailed description of the invention
Clearer, below in conjunction with the present invention for the purpose making the present invention implement, technical scheme and advantage
Accompanying drawing in embodiment, is further described in more detail the technical scheme in the embodiment of the present invention.At accompanying drawing
In, the most same or similar label represents same or similar element or has same or like function
Element.Described embodiment is a part of embodiment of the present invention rather than whole embodiments.Below
It is exemplary by the embodiment being described with reference to the drawings, it is intended to be used for explaining the present invention, and it is not intended that
Limitation of the present invention.Based on the embodiment in the present invention, those of ordinary skill in the art are not making wound
The every other embodiment obtained under the property made work premise, broadly falls into the scope of protection of the invention.Tie below
Close accompanying drawing embodiments of the invention are described in detail.
In describing the invention, it is to be understood that term " " center ", " longitudinally ", " laterally ", " front ",
The side of the instruction such as " afterwards ", "left", "right", " vertically ", " level ", " top ", " end " " interior ", " outward "
Position or position relationship be based on orientation shown in the drawings or position relationship, be for only for ease of description the present invention with
Simplify and describe rather than indicate or imply that the device of indication or element must have specific orientation, with specific
Azimuth configuration and operation, therefore it is not intended that limiting the scope of the invention.
In the present invention one broad embodiment, the system that the Coal Chemical Industry buck flash distillation of minimizing ammonia accumulation processes:
Middle pressure flash column, low pressure flash chamber, vacuum flasher, defecator, ash water tank, oxygen-eliminating device, mortar-trough,
Vacuum flashing evaporator overhead condenser, vacuum knockout drum, rectifying column, waste heat boiler, middle pressure flashed vapour condense
Device, middle pressure flash separation tank, rich ammonia condenser, rich ammonia condensing knockout drum；Medium pressure flash column upper
Portion's gaseous phase outlet end connects the entrance point of described waste heat boiler, and the port of export of described waste heat boiler dodges through medium pressure
Vapour condenser connects medium pressure flash separation tank and carries out gas-liquid separation, medium pressure flash separation tank top
Outlet side connects the bottom of described rectifying column, and the lower liquid phase port of export of medium pressure flash separation tank is through pump even
Connect the top of described rectifying column；The lower liquid phase port of export of medium pressure flash column is connected to described low pressure flash
The entrance point of tank；The upper gaseous phase port of export of described low pressure flash chamber connects the bottom of described rectifying column；Described
The lower liquid phase port of export of low pressure flash chamber is connected to the entrance point of described vacuum flasher；On described rectifying column
Outlet side, portion connects sulfur recovery unit, and the middle part side line outlet of described rectifying column connects described rich ammonia condenser
Entrance point, through the described rich ammonia condensing knockout drum that is connected to of described rich ammonia condenser, described rich ammonia condensing
The upper gas of knockout drum does desulfurizing agent, and the bottom liquid outlet end of described rich ammonia condensing knockout drum is connected to
Described rectifying column is as backflow；The bottom liquid phases port of export of described rectifying column connects the import of described oxygen-eliminating device
End；The upper gaseous phase port of export of described vacuum flasher is connected to institute through described vacuum flashing evaporator overhead condenser
Stating the entrance point of vacuum knockout drum, the upper gaseous phase port of export of described vacuum knockout drum connects vacuum
Pump, the lower liquid phase port of export of described vacuum knockout drum connects the entrance point of described oxygen-eliminating device, described very
The lower liquid phase port of export of empty flash tank is connected to the entrance point of described defecator, the top of described defecator
The clear liquor port of export is connected to the entrance point of described ash water tank, and the described defecator bottom mortar port of export connects institute
State mortar-trough；The bottom mortar port of export of described mortar-trough connects mortar dehydration treatment equipment；Described ash water tank
The port of export connect sewage disposal system and described oxygen-eliminating device, the liquid-phase outlet end of described oxygen-eliminating device is through high-pressure pump
Connect scrubbing tower.
As in figure 2 it is shown, the system that the Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes includes: middle pressure flash column
1, low pressure flash chamber 2, vacuum flasher 3, defecator 4, ash water tank 5, oxygen-eliminating device 6, mortar-trough 7,
Vacuum flashing evaporator overhead condenser 8, vacuum knockout drum 9, rectifying column 10, waste heat boiler 11, middle pressure are dodged
Vapour condenser 12, middle pressure flash separation tank 13, sour gas cooler 14, rich ammonia condenser 15, richness
Ammonia condensing knockout drum 16.
The upper gaseous phase port of export of described middle pressure flash column 1 connects the import of waste heat boiler 11 by pipeline
End, presses flashed vapour condenser 12 to be desalted water section condensation in the flashed vapour warp of the port of export of waste heat boiler 11
After, entrance is pressed flash separation tank 13 gas-liquid separation, outlet side, middle pressure flash separation tank 13 top enters essence
Evaporating the bottom of tower 10, middle pressure flash separation tank 13 lower liquid phase enters rectifying column 10 top through pump；Described
The lower liquid phase port of export of middle pressure flash column 1 be connected to the entrance point of low pressure flash chamber 2；Described low pressure
The upper gaseous phase of flash tank 2 is given vent to anger and is entered the bottom of rectifying column 10；The bottom of described low pressure flash chamber 2
The Heisui River of liquid-phase outlet end is together connected to vacuum flashing with the Heisui River from pulp water pump and gasification furnace start-stop car
The entrance point of tank 3；Give vent to anger and be connected to sulfur recovery dress through sour gas cooler 14 in described rectifying column 10 top
Putting, in the middle part of described rectifying column 10, side line outlet connects the entrance point of rich ammonia condenser 16, through rich ammonia
Condenser 15 be connected to rich ammonia condensing knockout drum 16, rich ammonia condensing knockout drum 16 upper gas is done de-
Sulfur agent, bottom liquid is back to rectifying column 10, as backflow；Described rectifying column 10 bottom liquid phases outlet
End connects the entrance point of oxygen-eliminating device 6；The upper gaseous phase port of export of vacuum flasher 3 is through vacuum flashing top
Condenser 8 is connected to the entrance point of vacuum knockout drum 9, and the upper gaseous phase of vacuum knockout drum 9 goes out
Mouth end connects vacuum pump, and the vacuum knockout drum 9 lower liquid phase port of export connects oxygen-eliminating device 6 entrance point, very
The lower liquid phase port of export of empty flash tank 3 is connected to the entrance point of defecator 4, described defecator 4 upper
Portion's clear liquor port of export is connected to the entrance point of ash water tank 5, and the defecator 4 bottom mortar port of export connects mortar
Groove 7；Bottom described mortar-trough 7, mortar outlet connects mortar dehydration treatment equipment；Described ash water tank 5
The port of export connects sewage disposal system and oxygen-eliminating device 6, and the liquid-phase outlet end of described oxygen-eliminating device 6 enters through high-pressure pump
Enter scrubbing tower.
Reduce Coal Chemical Industry buck flash distillation processing system and the technique of ammonia accumulation, comprise the following steps:
1) coal gasified black water sequentially enters middle pressure flash column, low pressure flash chamber and vacuum flasher and carries out
Flash distillation processes.
2) the coal gasification gasification Heisui River after step (1) flash distillation processes, enters defecator and removes solid particle,
Realizing solid-liquid separation, top water outlet is returned gasification system after entering deoxygenation groove deoxygenation and is recycled.
3) flashed vapour that in, pressure flash column flashes off contains NH3、H2S、CO、CO2And COS
Deng gas, after utilizing waste heat boiler to reclaim heat, partial condensation presses flash separation tank gas-liquid separation in entering,
Giving vent to anger entrance rectifier bottoms in top, bottom liquid enters rectifier.
4) flashed vapour that flashes off of low pressure flash chamber contains NH3、H2S、CO、CO2、COS
Deng gas, it is directly entered rectifier bottoms as rectification thermal source.
The ammonia that in the middle part of rectifying column, side take-off is qualified, wherein H2S content ＜ 10PPM, as project assorted
Supplementing of boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2, the sour gas such as COS,
Remove sulfur recovery system；The qualified water outlet in bottom returns deoxygenation groove as supplementary water.
The high temperature (200～224 DEG C) high pressure (4.0MPaG) of tower and gasification furnace is washed containing solid from coal gasification carbon
(2%) Heisui River presses flash column 1 to carry out first order pressure release flash distillation in entering, and flashing pressure is 0.5～0.8
MPaG, temperature are 159～175 DEG C, entrainment of substantial amounts of NH in flashed vapour3And H2S、CO、CO2、
The gases such as COS, flashed vapour is introduced into waste heat boiler 11 and reclaims heat, and it is saturated that waste heat boiler 11 produces
Steam is incorporated to the saturated vapor pipeline of factory, presses flash distillation air cooling in the flashed vapour of waste heat boiler 11 enters
Condenser 12 partial condensation, presses flash separation tank 13 to carry out gas-liquid separation in entrance, isolated liquid passes through
The top of pump input rectifying column 10, gas enters rectifying column 10 bottom as thermal source；
The lower liquid phase of middle pressure flash column 1 enters low pressure flash chamber 2, carries out second level pressure release flash distillation, flash distillation
Pressure is 0.3MPaG, temperature is 143 DEG C, entrainment of substantial amounts of NH in flashed vapour3、H2S、CO、
CO2, the gas such as COS, flashed vapour enters rectifying column 10 bottom as thermal source；Operation pressure in rectifying column
Power is 0.2MPaG, and in the middle part of rectifying column, extraction is qualified 10～15% strong aqua ammonia, wherein H2S content ＜ 10PPM,
Supplementing as project assorted boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2, COS etc.
Sour gas, removes sulfur recovery system, and the qualified water outlet in bottom returns deoxygenation groove as supplementary water.
The lower liquid phase of low pressure flash chamber 2 together enters vacuum with the Heisui River of slag pool pump and gasification furnace start-stop car
Flash tank 3；Carry out third level pressure release flash distillation, flashing pressure for-0.08～-0.05MPaG, temperature be 60～
80 DEG C, the upper gaseous phase of vacuum flasher 3, through vacuum flashing evaporator overhead condenser 8 partial condensation, enters vacuum
Knockout drum 9 gas-liquid separation, the upper gaseous phase port of export of vacuum knockout drum 9 connects vacuum pump, very
Air fluid knockout drum 9 lower liquid phase enters oxygen-eliminating device 6, and the bottom of vacuum flasher 3 is containing (2% Heisui River is entered admittedly
Enter defecator 4, Heisui River at defecator 4 in additional flocculating agents effect, it is achieved solid-liquor separation, defecator 4
Top clear liquor enters ash water tank 5, and defecator 4 bottom mortar enters mortar-trough 7；Mortar-trough 7 bottom ash
Slurry outlet connects mortar dehydration treatment equipment；Ash water tank 5 be partly into sewage disposal system and a part
Enter oxygen-eliminating device 6, deoxygenation groove 6 water from ash water tank 5, vacuum knockout drum 9 and rectifying column 10,
Remove oxygen under the heat effect of low-pressure steam, directly enter scrubbing tower as washings through high-pressure pump.
As it is shown on figure 3, high pressure flash tower 1, middle pressure flash column 2, low pressure flash chamber 3, vacuum flasher 4,
Defecator 5, ash water tank 6, oxygen-eliminating device 17, mortar-trough 7, vacuum flashing evaporator overhead condenser 8, vacuum gas
Liquid knockout drum 9, rectifying column 10, waste heat boiler 11, high pressure flash gas condenser 12, high pressure flash separate
Tank 13, sour gas cooler 14, rich ammonia condenser 15, rich ammonia condensing knockout drum 16；It is characterized in that:
The upper gaseous phase port of export of described high pressure flash tower 1 connects the entrance point of waste heat boiler 11, waste heat boiler 11
The port of export flashed vapour through high pressure flash gas condenser 12 be desalted water section condensation after, enter high pressure dodge
Steaming knockout drum 13 gas-liquid separation, outlet side, high pressure flash knockout drum 13 top enters the bottom of rectifying column 10,
High pressure flash knockout drum 13 lower liquid phase enters rectifying column 10 top through pump；Described high pressure flash tower 1
The lower liquid phase port of export be connected to the entrance point of middle pressure flash column 2；The top of described middle pressure flash column 2
Gas phase is given vent to anger and is entered the bottom of rectifying column 10；The lower liquid phase port of export of described middle pressure flash column 2 connects
Entrance point to low flash tank 3；The upper gaseous phase of described low pressure flash chamber 3 is given vent to anger and is entered rectifying column 10
Bottom；The Heisui River of the lower liquid phase port of export of described low pressure flash chamber 3 with from pulp water pump and gasification furnace
The Heisui River of start-stop car is together connected to the entrance point of vacuum flasher 4；Give vent to anger in described rectifying column 10 top
Being connected to sulfur recovery unit through sour gas cooler 14, in the middle part of described rectifying column 10, side line outlet connects richness
The entrance point of ammonia condenser 15, is connected to rich ammonia condensing knockout drum 16 through rich ammonia condenser 15,
Rich ammonia condensing knockout drum 16 upper gas does desulfurizing agent, and bottom liquid is back to rectifying column 10, as returning
Stream；The described rectifying column 10 bottom liquid phases port of export connects the entrance point of oxygen-eliminating device 17；Vacuum flasher 4
The upper gaseous phase port of export be connected to the import of vacuum knockout drum 9 through vacuum flashing evaporator overhead condenser 8
End, the upper gaseous phase port of export of vacuum knockout drum 9 connects vacuum pump, vacuum knockout drum 9 bottom
Liquid-phase outlet end connects oxygen-eliminating device 17 entrance point, and the lower liquid phase port of export of vacuum flasher 4 is connected to clear
The entrance point of clear groove 5, the top clear liquor port of export of described defecator 5 is connected to the import of ash water tank 6
End, the defecator 5 bottom mortar port of export connects mortar-trough 7；Bottom described mortar-trough 7, mortar outlet is even
Ash slurry dehydration treatment equipment；The port of export of described ash water tank 6 connects sewage disposal system and oxygen-eliminating device 17,
The liquid-phase outlet end of described oxygen-eliminating device 17 enters scrubbing tower through high-pressure pump.
The high temperature (250～260 DEG C) high pressure (8.4MPaG) of tower and gasification furnace is washed containing solid from coal gasification carbon
(2%) Heisui River enters high pressure flash tower 1 and carries out first order pressure release flash distillation, and flashing pressure is 3.0～3.4
MPaG, temperature are 240～250 DEG C, entrainment of substantial amounts of NH in flashed vapour3And H2S、CO、CO2、
The gases such as COS, flashed vapour is introduced into waste heat boiler 11 and reclaims heat, and it is saturated that waste heat boiler 11 produces
Steam is incorporated to the saturated vapor pipeline of factory, and the flashed vapour through waste heat boiler 11 enters high pressure flash air cooling
Condenser 12 partial condensation, enters high pressure flash knockout drum 13 and carries out gas-liquid separation, and isolated liquid passes through
The top of pump input rectifying column 10, gas enters rectifying column 10 bottom as thermal source；
The lower liquid phase of high pressure flash tower 1 presses flash column 2 in entering, and carries out second level pressure release flash distillation, flash distillation
Pressure is 0.5～0.8MPaG, temperature is 159～175 DEG C, entrainment of substantial amounts of NH in flashed vapour3With
H2S、CO、CO2, the gas such as COS, flashed vapour enters rectifying column 10 bottom as thermal source；
The lower liquid phase of middle pressure flash column 2 enters low pressure flash chamber 3, carries out third level pressure release flash distillation, flash distillation
Pressure is 0.3MPaG, temperature is 143 DEG C, entrainment of substantial amounts of NH in flashed vapour3、H2S、CO、
CO2, the gas such as COS, flashed vapour enters rectifying column 10 bottom as thermal source；Operation pressure in rectifying column
For 0.2MPaG, in the middle part of rectifying column, extraction is qualified 10～15% strong aqua ammonia, wherein H2S content ＜ 10PPM,
Supplementing as project assorted boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2, COS etc.
Sour gas, removes sulfur recovery system, and the qualified water outlet in bottom returns deoxygenation groove as supplementary water.
The lower liquid phase of low pressure flash chamber 3 together enters vacuum with the Heisui River of slag pool pump and gasification furnace start-stop car
Flash tank 4；Carry out fourth stage pressure release flash distillation, flashing pressure for-0.08～-0.05MPaG, temperature be 60～
80 DEG C, the upper gaseous phase of vacuum flasher 4, through vacuum flashing evaporator overhead condenser 8 partial condensation, enters vacuum
Knockout drum 9 gas-liquid separation, the upper gaseous phase port of export of vacuum knockout drum 9 connects vacuum pump, very
Air fluid knockout drum 9 lower liquid phase enters oxygen-eliminating device 17, and the bottom of vacuum flasher 4 is containing solid (2% Heisui River
Enter defecator 5, Heisui River at defecator 5 in additional flocculating agents effect, it is achieved solid-liquor separation, defecator 5
Top clear liquor enters ash water tank 6, and defecator 5 bottom mortar enters mortar-trough 7；Mortar-trough 7 bottom ash
Slurry outlet connects mortar dehydration treatment equipment；Ash water tank 5 be partly into sewage disposal system and a part
Enter oxygen-eliminating device 17, deoxygenation groove 17 water from ash water tank 5, vacuum knockout drum 9 and rectifying column 10,
Under the heat effect of low-pressure steam, remove oxygen, directly enter scrubbing tower as washings through high-pressure pump.
Transformation system uses low-carbon (LC) water than flow process, and deoxygenation groove is atmospheric pressure device, and water temperature is about 109 DEG C, logical
Cross high-pressure pump and directly enter scrubbing tower.
Deoxygenation groove is equipment with pressure, and temperature is about 145 DEG C, is directly entered scrubbing tower by high-pressure pump.
A kind of Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes technique and system, the flashed vapour of high pressure flash tower
Heat rectifying column 10 still liquid by reboiler, enter from rectifying column 10 top after condensation, heated gasification
Still liquid enters the bottom of rectifying column 10 as steam source of the gas.
A kind of Coal Chemical Industry buck flash distillation processing system reducing ammonia accumulation and technique, the flashed vapour of middle pressure flash column
Heat rectifying column 10 still liquid by reboiler, enter from rectifying column 10 top after condensation, heated gasification
Still liquid enters the bottom of rectifying column 10 as steam source of the gas.
Last it is noted that above example is only in order to illustrate technical scheme, rather than right
It limits.Although the present invention being described in detail with reference to previous embodiment, the ordinary skill of this area
Personnel it is understood that the technical scheme described in foregoing embodiments still can be modified by it, or
Wherein portion of techniques feature is carried out equivalent；And these amendments or replacement, do not make relevant art side
The essence of case departs from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (9)
1. the system that the Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes, it is characterised in that including:
Middle pressure flash column, low pressure flash chamber, vacuum flasher, defecator, ash water tank, oxygen-eliminating device, mortar-trough,
Vacuum flashing evaporator overhead condenser, vacuum knockout drum, rectifying column, waste heat boiler, middle pressure flashed vapour condense
Device, middle pressure flash separation tank, sour gas cooler, rich ammonia condenser, rich ammonia condensing knockout drum；Described
The upper gaseous phase port of export of middle pressure flash column is connected with the entrance point of described waste heat boiler by pipeline, described useless
The port of export of heat boiler connects medium pressure flash separation tank through medium pressure flashed vapour condenser and carries out gas-liquid
Separating, outlet side, medium pressure flash separation tank top connects the bottom of described rectifying column, medium pressure flash distillation
The lower liquid phase port of export of knockout drum connects the top of described rectifying column through pump；The bottom of medium pressure flash column
Liquid-phase outlet end is connected to the entrance point of described low pressure flash chamber；The upper gaseous phase outlet of described low pressure flash chamber
End connects the bottom of described rectifying column；The lower liquid phase port of export of described low pressure flash chamber is connected to described vacuum
The entrance point of flash tank；Described rectifier outlet side is connected to sulfur recovery unit through sour gas cooler,
The middle part side line outlet of described rectifying column connects the entrance point of described rich ammonia condenser, cold through described rich ammonia
Condenser be connected to described rich ammonia condensing knockout drum, the upper gas of described rich ammonia condensing knockout drum does desulfurization
Agent, the bottom liquid outlet end of described rich ammonia condensing knockout drum is connected to described rectifying column as backflow；Described
The bottom liquid phases port of export of rectifying column connects the entrance point of described oxygen-eliminating device；The top gas of described vacuum flasher
The phase port of export is connected to the entrance point of described vacuum knockout drum through described vacuum flashing evaporator overhead condenser,
The upper gaseous phase port of export of described vacuum knockout drum connects vacuum pump, under described vacuum knockout drum
Portion's liquid-phase outlet end connects the entrance point of described oxygen-eliminating device, and the lower liquid phase port of export of described vacuum flasher is even
Being connected to the entrance point of described defecator, the top clear liquor port of export of described defecator is connected to described buck
The entrance point of groove, the described defecator bottom mortar port of export connects described mortar-trough；The bottom of described mortar-trough
The mortar port of export connects mortar dehydration treatment equipment；The port of export of described ash water tank connect sewage disposal system and
Described oxygen-eliminating device, the liquid-phase outlet end of described oxygen-eliminating device connects scrubbing tower through high-pressure pump.
2. the system that the Coal Chemical Industry buck flash distillation reducing ammonia accumulation used described in claim 1 processes
Technique, it is characterised in that comprise the following steps:
(1) gasification furnace of coal gasification and carbon wash Heisui River of tower through overregulate valve sequentially enter middle pressure flash column,
Low pressure flash chamber and vacuum flasher carry out flash distillation process；
(2) the coal gasification gasification Heisui River after step (1) flash distillation processes, enters defecator and removes solid
Grain, it is achieved solid-liquid separation, top water outlet is returned gasification system after entering deoxygenation groove deoxygenation and is recycled；
(3) flashed vapour that medium pressure flash column flashes off contains NH3And H2S、CO、CO2、
COS gas, utilizes the saturated low-pressure steam of waste heat boiler by-product, after reclaiming heat, during partial condensation enters
Pressure flash separation tank carries out gas-liquid separation, gives vent to anger entrance rectifier bottoms in top, and bottom liquid enters rectifying column
Top；
(4) flashed vapour that flashes off of described low pressure flash chamber contains NH3And H2S、CO、CO2、
COS gas, is directly entered rectifier bottoms as rectification thermal source；
(5) ammonia that in the middle part of rectifying column, side take-off is qualified, wherein H2S content ＜ 10PPM, as item
Supplementing of mesh supporting boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2Sour gas with COS
Body, removes sulfur recovery system；The qualified water outlet in bottom returns deoxygenation groove as supplementary water.
3. the system that the Coal Chemical Industry buck flash distillation reducing ammonia accumulation processes, it is characterised in that including:
High pressure flash tower, middle pressure flash column, low pressure flash chamber, vacuum flasher, defecator, ash water tank, deoxygenation
Device, mortar-trough, vacuum flashing evaporator overhead condenser, vacuum knockout drum, rectifying column, waste heat boiler, height
Pressure flashed vapour condenser, high pressure flash knockout drum, sour gas cooler, rich ammonia condenser, rich ammonia condensing
Knockout drum；The upper gaseous phase port of export of described high pressure flash tower connects the entrance point of described waste heat boiler, described
The port of export of waste heat boiler connects described high pressure flash knockout drum through described high pressure flash gas condenser and carries out gas
Liquid separates, and the outlet side, top of described high pressure flash knockout drum connects the bottom of described rectifying column, described high pressure
The lower liquid phase port of export of flash separation tank enters the top of described rectifying column through pump；Described high pressure flash tower
The lower liquid phase port of export be connected to the entrance point of medium pressure flash column；The top gas of medium pressure flash column
The phase port of export enters the bottom of described rectifying column；The lower liquid phase port of export of medium pressure flash column is connected to institute
State the entrance point of low pressure flash chamber；The upper gaseous phase port of export of described low pressure flash chamber connects described rectifying column
Bottom；The lower liquid phase port of export of described low pressure flash chamber is connected to the entrance point of described vacuum flasher；Institute
State rectifier exhaust outlets end and be connected to sulfur recovery unit through sour gas cooler, in the middle part of described rectifying column
Side line outlet connects the entrance point of described rich ammonia condenser, is connected to described richness through described rich ammonia condenser
Ammonia condensing knockout drum, described rich ammonia condensing knockout drum upper gas does desulfurizing agent, and bottom liquid backflow end is even
It is connected to described rectifying column as backflow；The bottom liquid phases port of export of described rectifying column connects entering of described oxygen-eliminating device
Mouth end；The upper gaseous phase port of export of described vacuum flasher, through described vacuum flashing evaporator overhead condenser, connects
To the entrance point of described vacuum knockout drum, the upper gaseous phase port of export of described vacuum knockout drum connects
Vacuum pump, the lower liquid phase port of export of described vacuum knockout drum connects the entrance point of described oxygen-eliminating device, institute
The lower liquid phase port of export stating vacuum flasher is connected to the entrance point of described defecator, described defecator
The top clear liquor port of export is connected to the entrance point of described ash water tank, the bottom mortar port of export of described defecator
Connect described mortar-trough；The bottom mortar outlet of described mortar-trough connects mortar dehydration treatment equipment；Described ash
The port of export of tank connects sewage disposal system and described oxygen-eliminating device, and the liquid-phase outlet end of described oxygen-eliminating device is through height
Press pump is connected to scrubbing tower.
4. the system that the Coal Chemical Industry buck flash distillation reducing ammonia accumulation used described in claim 3 processes
Technique, it is characterised in that comprise the following steps:
(1) gasification furnace of coal gasification and carbon wash Heisui River of tower through overregulate valve sequentially enter high pressure flash tower,
Middle pressure flash column, low pressure flash chamber and vacuum flasher carry out flash distillation process；
(2) defecator removing solid particle is entered in the coal gasification gasification Heisui River after step (1) flash distillation processes,
Realizing solid-liquid separation, top water outlet is returned gasification system after entering deoxygenation groove deoxygenation and is recycled；
(3) flashed vapour that high pressure flash tower flashes off contains NH3And H2S、CO、CO2、COS
Gas, after utilizing waste heat boiler to reclaim heat, partial condensation enters high pressure flash knockout drum and carries out gas-liquid separation,
Giving vent to anger entrance rectifier bottoms in top, bottom liquid enters rectifier；
(4) in, the flashed vapour that flashes off of low pressure flash chamber contain NH3And H2S、CO、CO2、
The gases such as COS, are directly entered rectifier bottoms as rectification thermal source.
(5) ammonia that in the middle part of rectifying column, side take-off is qualified, wherein H2S content ＜ 10PPM, as project
Supplementing of supporting boiler desulfurization weak ammonia；Collected overhead H2S、CO、CO2, COS sour gas,
Remove sulfur recovery system；The qualified water outlet in bottom returns deoxygenation groove as supplementary water.
5. the system processed according to the Coal Chemical Industry buck flash distillation reducing ammonia accumulation described in claim 2 and 4
Technique, it is characterised in that: described deoxygenation groove is atmospheric pressure device, and water temperature is 109 DEG C, straight by high-pressure pump
Tap into scrubbing tower.
6. the system processed according to the Coal Chemical Industry buck flash distillation reducing ammonia accumulation described in claim 2 and 4
Technique, it is characterised in that: described deoxygenation groove is equipment with pressure, and temperature is 145 DEG C, straight by high-pressure pump
Tap into scrubbing tower.
7. the system processed according to the Coal Chemical Industry buck flash distillation reducing ammonia accumulation described in claim 2 and 4
Technique, it is characterised in that: for ensure weak ammonia separation purity, adding one at the bottom of rectifying tower
The low-pressure saturated steam of 0.5MPaG is as thermal source.
The Coal Chemical Industry buck flash distillation processing system of minimizing ammonia the most according to claim 1 accumulation, it is special
Levy and be: medium pressure flash column flashed vapour out heats described rectification tower bottoms by reboiler, condensation
After enter from described rectifier, the still liquid of heated gasification enters described rectifying column as steam source of the gas
Bottom.
The Coal Chemical Industry buck flash distillation processing system of minimizing ammonia the most according to claim 3 accumulation, it is special
Levy and be: described high pressure flash tower flashed vapour out heats described rectification tower bottoms by reboiler, condensation
After enter from described rectifier, the still liquid of heated gasification enters described rectifying column as steam source of the gas
Bottom.
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Application publication date: 20160928 |