CN101724471A - Method for purifying and recycling benzoid hydrocarbon, ammonia and coal tar from coke-oven gas - Google Patents
Method for purifying and recycling benzoid hydrocarbon, ammonia and coal tar from coke-oven gas Download PDFInfo
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- CN101724471A CN101724471A CN200910272911A CN200910272911A CN101724471A CN 101724471 A CN101724471 A CN 101724471A CN 200910272911 A CN200910272911 A CN 200910272911A CN 200910272911 A CN200910272911 A CN 200910272911A CN 101724471 A CN101724471 A CN 101724471A
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Abstract
The invention relates to a method for purifying and recycling benzoid hydrocarbon, ammonia and coal tar from coke-oven gas. The technical scheme of the method comprises the following steps of: cooling the 80-90 DEG C coke-oven gas through a condensation step to 20-27 DEG C, then directly carrying out a benzene washing step, absorbing benzoid hydrocarbon in the coke-oven gas to the wash oil to form rich oil, desulfurizing the coke-oven gas at 30-35 DEG C after the benzene washing step, air-blast pressurizing the desulfurized coke-oven gas at 30-35 DEG C, naturally raising the temperature of the coke-oven gas to 50-55 DEG C, carrying out an ammonium sulfate step on the coke-oven gas to recycle ammonia therein, and using the purified coke-oven gas after the ammonium sulfate step as high-grade fuel to be supplied to the outside. The remaining ammonia water generated in the condensation step goes into an ammonia desorption step so as to desorb ammonia and goes into the ammonium sulfate step to produce ammonium sulfate; and benzoid hydrocarbon is recycled from the rich oil produced in the benzene washing step through a crude benzene distilling step. The invention has the characteristics of orderly temperature change, smooth change of gradient, simple technical process, low energy consumption, low production cost, high purification efficiency and environmental friendliness.
Description
Technical field
The invention belongs to coke oven gas purification and chemical products recovery technology field.Be specifically related to the method for a kind of coke oven gas purification and recovery benzene hydrocarbon, ammonia and coal tar.
Background technology
At present, coke oven gas purification and chemical products reclaim, usually adopt both at home and abroad benzene hydrocarbon, ammonia and the coal tar wet goods chemical products (selection of fine purification technique for coke oven gas in coke-oven gas condensation cooling and the methods recovery coal gas such as the absorption of various absorption agent, wet distillation processing, Yang Jianhua Wang Yong woods, " Anhui metallurgy " the 2nd phase in 2008), technical process is: condensation operation, air blast pressurization operation, pre-cooling working procedure, desulfurization process, ammonia still process, sulphur ammonium operation, final cooling process, wash benzene operation, crude benzol distillation process.
In above-mentioned technology: 80～90 ℃ coke-oven gas is forced into 11000～15000Pa through the centrifugal blower of air blast pressurization operation after the condensation operation is cooled to 20～27 ℃, coke-oven gas is warming up to 40～47 ℃ naturally; Again coke-oven gas is pre-chilled to 30～35 ℃ through pre-cooling working procedure, enter desulfurization process then and remove hydrogen sulfide in the coke-oven gas, remove 30～35 ℃ coke-oven gas behind the hydrogen sulfide and be preheated to 50～60 ℃ and enter sulphur ammonium operation, reclaim ammonia in the coke-oven gas to produce ammonium sulfate; 50～60 ℃ of coke-oven gas after the sulphur ammonium operation enter after final cooling process is cooled to 25～27 ℃ once more washes the benzene operation, with the benzene hydrocarbon in the washing oil absorption coke-oven gas; The washing oil that has absorbed benzene hydrocarbon forms rich oil, and rich oil reclaims benzene hydrocarbon by the crude benzol distillation process, and the clean coke-oven gas of washing after the benzene operation promptly supplies outward as clean fuel.Simultaneously, the remained ammonia that produces in coke oven gas purification and the chemical products removal process with water vapour desorb ammonia wherein, enters sulphur ammonium operation and produces ammonium sulfate in ammonia still process.
Above-mentioned change in process temperature is unordered, graded is frequent, technical process is complicated, energy consumption is big, source of pollution are many, production cost is high.
Summary of the invention
The purpose of this invention is to provide that a kind of temperature variation is orderly, graded is level and smooth, the technical process simplification, energy consumption is low, production cost is low, purification efficiency is high and eco-friendly coke oven gas purification and reclaim the method for benzene hydrocarbon, ammonia and coal tar.
For achieving the above object, the technical process that the present invention adopts is: 80～90 ℃ coke-oven gas are directly advanced to wash the benzene operation after the condensation operation is cooled to 20～27 ℃, benzene hydrocarbon in the coke-oven gas absorbed form rich oil in the washing oil, 30～35 ℃ of coke-oven gas after washing the benzene operation enter the desulfurization process desulfurization, 30～35 ℃ of coke-oven gas after the desulfurization enter the pressurization of air blast pressurization operation, coke-oven gas is warming up to 50～55 ℃ naturally, naturally the sulphur ammonium operation that enters the coke-oven gas after heating up reclaims ammonia wherein, and the clean coke-oven gas after the sulphur ammonium operation supplies outward as high-grade fuel.
The remained ammonia that the condensation operation produces enters the ammonia desorption step ammonia is desorbed, and enters sulphur ammonium operation and produces ammonium sulfate; Wash the rich oil process crude benzol distillation process recovery benzene hydrocarbon that the benzene operation produces.
In the technical process that the present invention adopts:
The condensation operation is: 80～90 ℃ the coke-oven gas that comes from coke oven enters the transverse tube type water cooler, the transverse tube type water cooler divides epimere and hypomere, and coke-oven gas is gone into water cooler epimere and recirculated water heat exchange earlier, is cooled to 40～45 ℃, reenter water cooler hypomere and chilled water heat exchange, be cooled to 20～27 ℃; Cooled coke-oven gas enters electrical tar precipitator, enters behind the capture coal tar droplet and washes the benzene operation; After separating water outlet, the phlegma that the coke-oven gas cooling is produced is coal-tar products.
Washing the benzene operation is: will be entered by the bottom through cooled 20～27 ℃ coke-oven gas of condensation operation and wash the benzene tower, with temperature that cat head sprays is 27～32 ℃ reverse contact of circulating washing oil, the benzene hydrocarbon that washing oil absorbs in the coal gas forms rich oil, rich oil is gone out by tower bottom flow, deliver to the crude benzol distillation process, 30～35 ℃ of coke-oven gas washing behind the benzene tower enter desulfurization process.
The crude benzol distillation process is: will be from the rich oil elder generation of washing the benzene operation and the benzene hydrocarbon steam on debenzolizing tower top and the mixture heat exchange of steam, again with the hot oil-poor heat exchange of discharging at the bottom of the debenzolizing tower, enter the dehydration tower dehydration then, the rich oil after the dehydration is heated to 180～190 ℃ and enters the debenzolizing tower distillation; Discharge at the bottom of the benzene hydrocarbon steam of overflowing in debenzolizing tower top and the mixture of steam and the debenzolizing tower hot oil-poor successively with from the rich oil heat exchange of washing the benzene operation, hot oil-poor getting back to as washing oil after the heat exchange washed the benzene operation, the benzene hydrocarbon steam after the heat exchange and the mixture of steam carry out oily water separation after condensation, be the benzene hydrocarbon product after the separation water outlet.
Desulfurization process is: the coke-oven gas of washing after the benzene operation 30～35 ℃ enters thionizer by the bottom, and with reverse contact of doctor solution that cat head sprays, 30～35 ℃ of coke-oven gas that removed hydrogen sulfide enter air blast pressurization operation; The doctor solution that has absorbed the hydrogen sulfide in the coke-oven gas is discharged at the bottom of by tower, recycles after regeneration.
Air blast pressurization operation is: the coke-oven gas behind the desulfurization process is forced into 5000～8000Pa through centrifugal blower, and coke-oven gas is warming up to 50～55 ℃ naturally, enters sulphur ammonium operation.
Sulphur ammonium operation is: 50～55 ℃ of coke-oven gas after the centrifugal blower pressurization enter Spray Saturator with the ammonia in the sulfuric acid absorption coal gas, generate product ammonium sulfate; Clean coke-oven gas sub-fraction after the sulphur ammonium operation recycles as poor ammonia coal gas desorb remained ammonia, and all the other supply outward as high-grade fuel.
The ammonia desorption step is: the agent that removes that adds earlier 15～35g/L in the remained ammonia that the condensation operation is produced, modulation pH value to 10～14, again it is sent into reaction unit, reacted remained ammonia enters immersed type stripping desorption apparatus, the clean coke-oven gas of sub-fraction after the origin bin cure ammonium operation enters the desorb of subsurface one, the two section gas distributor stripping of immersed type stripping desorption apparatus, and the rich ammonia coal gas after the stripping desorb is got back to sulphur ammonium operation and produced ammonium sulfate.
Described 80～90 ℃ of coke-oven gas mainly are made up of inflammable gas component, chemical products component and water vapour; The inflammable gas component mainly is: hydrogen 45～54g/Nm
3, methane 170～210g/Nm
3, carbon monoxide 63～88g/Nm
3, ethane and homologue 13～26g/Nm thereof
3The chemical products component mainly is: coal tar 100～125g/Nm
3, benzene hydrocarbon 30～40g/Nm
3, ammonia 6～10g/Nm
3, hydrogen sulfide 7～12g/Nm
3, prussiate 0.5～1.5g/Nm
3, naphthalene 8～12g/Nm
3, sulfide 2～2.5g/Nm
3Water vapour content is 260～470g/Nm
3
Because adopt technique scheme, the present invention has following characteristics:
1, because 20～27 ℃ coke-oven gas temperature of the present invention after the condensation operation is lower, so this coke-oven gas directly enters and washes the benzene operation and the benzene hydrocarbon in the coke-oven gas is absorbed form rich oil in the washing oil.In washing the benzene operation, enter washing oil for preventing the steam condensation in this coke-oven gas, used washing oil temperature is a little more than this coke-oven gas temperature, washes that coke-oven gas is warming up to 30～35 ℃ naturally in the benzene operation, satisfies the requirement of desulfurization process to the coke-oven gas temperature.30～35 ℃ of coke-oven gas after the desulfurization are warming up to 50～55 ℃ naturally through the centrifugal blower pressurization of air blast pressurization operation, satisfy the requirement of sulphur ammonium operation to the coke-oven gas temperature, and coke-oven gas enters sulphur ammonium operation recovery ammonia wherein to produce ammonium sulfate.Thus, the temperature variation in the technical process of the present invention is orderly, graded is level and smooth, and energy consumption is low.
2, because the present invention is orderly by the coke-oven gas temperature variation, the graded principle of smoothing is provided with technical process, cancelled the primary heater unit in pre-cooling working procedure, final cooling process and the sulphur ammonium operation in existing coke oven gas purification and the chemical products recovery method, not only simplify technical process, and saved the energy.
3, because the temperature variation of technical process of the present invention is orderly, graded is level and smooth, only need coke-oven gas once is cooled to 20～27 ℃ of production requirements that can satisfy follow-up each operation in the condensation operation, with existing with coke-oven gas heat repeatedly, the refrigerative method compares, can save energy more than 51%, correspondingly reduce production costs more than 33%.Because pre-cooling working procedure and the used recirculated water of final cooling process cooling coke-oven gas need to recycle after the cooling tower cooling in the existing method, phenol cyanogen pollutent contained in the recirculated water evaporates into contaminate environment in the atmosphere in a large number, the present invention has cancelled this two-step, and the pollutional equivalent that can reduce discharging atmospheric polluting material in coke oven gas purification and the chemical products removal process is more than 83%; Simultaneously, ammonia desorption step of the present invention can be increased to the removal efficiency of ammonia nitrogen in the remained ammonia more than 25%, reduces discharging deposed ammonia 20%.So energy consumption of the present invention is low, production cost is low, environmental friendliness.
4, air blast pressurization operation of the present invention is arranged on the condensation operation, washes after benzene operation, crude benzol distillation process and the desulfurization process; make condensation operation in the whole process flow, wash the benzene operation, crude benzol distillation process, desulfurization process all be in negative pressure state production; eliminate each operation coke-oven gas and reached wherein leaking of toxic chemical substance, protected atmospheric environment.
5, its chemical products component of clean coke-oven gas behind purification and recovery chemical products mainly comprises coal tar 0～0.01g/Nm
3, benzene hydrocarbon 2～4g/Nm
3, ammonia 0.03～0.1g/Nm
3, hydrogen sulfide 0～0.02g/Nm
3, prussiate 0～0.1g/Nm
3, naphthalene 0.05～0.1g/Nm
3, sulfide 0.05～0.2g/Nm
3Its inflammable gas component mainly comprises hydrogen 45～54g/Nm
3, methane 170～210g/Nm
3, carbon monoxide 63～88g/Nm
3, ethane and homologue 13～26g/Nm thereof
3Its water vapour content is 55～65g/Nm
3
Therefore, the present invention has that temperature variation is orderly, graded is level and smooth, the technical process simplification, energy consumption is low, production cost is low, purification efficiency is high and eco-friendly characteristics.
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
Fig. 2 is the temperature changing curve diagram of coke-oven gas among Fig. 1;
Existing a kind of coke oven gas purification of Fig. 3 and the process flow diagram that reclaims the chemical products method;
Fig. 4 is the temperature changing curve diagram of coke-oven gas among Fig. 3.
Embodiment
Below in conjunction with the drawings and specific embodiments the present invention being described further, is not the restriction to its protection domain:
Embodiment
The method of a kind of coke oven gas purification and recovery benzene hydrocarbon, ammonia and coal tar.Its technical process is as shown in Figure 1: 80～90 ℃ coke-oven gas are directly advanced to wash the benzene operation after the condensation operation is cooled to 20～27 ℃, benzene hydrocarbon in the coke-oven gas absorbed form rich oil in the washing oil, 30～35 ℃ of coke-oven gas after washing the benzene operation enter the desulfurization process desulfurization, 30～35 ℃ of coke-oven gas after the desulfurization enter the pressurization of air blast pressurization operation, coke-oven gas is warming up to 50～55 ℃ naturally, naturally the sulphur ammonium operation that enters the coke-oven gas after heating up reclaims ammonia wherein, and the clean coke-oven gas after the sulphur ammonium operation supplies outward as high-grade fuel.
The remained ammonia that the condensation operation produces enters the ammonia desorption step ammonia is desorbed, and enters sulphur ammonium operation and produces ammonium sulfate; Wash the rich oil process crude benzol distillation process recovery benzene hydrocarbon that the benzene operation produces.
In the technical process that present embodiment adopts:
The condensation operation is: 80～90 ℃ the coke-oven gas that comes from coke oven enters the transverse tube type water cooler, the transverse tube type water cooler divides epimere and hypomere, and coke-oven gas is gone into water cooler epimere and recirculated water heat exchange earlier, is cooled to 40～45 ℃, reenter water cooler hypomere and chilled water heat exchange, be cooled to 20～27 ℃; Cooled coke-oven gas enters electrical tar precipitator, enters behind the capture coal tar droplet and washes the benzene operation; After separating water outlet, the phlegma that the coke-oven gas cooling is produced is coal-tar products.
Washing the benzene operation is: will be entered by the bottom through cooled 20～27 ℃ coke-oven gas of condensation operation and wash the benzene tower, with temperature that cat head sprays is 27～32 ℃ reverse contact of circulating washing oil, the benzene hydrocarbon that washing oil absorbs in the coal gas forms rich oil, rich oil is gone out by tower bottom flow, deliver to the crude benzol distillation process, 30～35 ℃ of coke-oven gas washing behind the benzene tower enter desulfurization process.
The crude benzol distillation process is: will be from the rich oil elder generation of washing the benzene operation and the benzene hydrocarbon steam on debenzolizing tower top and the mixture heat exchange of steam, again with the hot oil-poor heat exchange of discharging at the bottom of the debenzolizing tower, enter the dehydration tower dehydration then, the rich oil after the dehydration is heated to 180～190 ℃ and enters the debenzolizing tower distillation; Discharge at the bottom of the benzene hydrocarbon steam of overflowing in debenzolizing tower top and the mixture of steam and the debenzolizing tower hot oil-poor successively with from the rich oil heat exchange of washing the benzene operation, hot oil-poor getting back to as washing oil after the heat exchange washed the benzene operation, the benzene hydrocarbon steam after the heat exchange and the mixture of steam carry out oily water separation after condensation, be the benzene hydrocarbon product after the separation water outlet.
Desulfurization process is: the coke-oven gas of washing after the benzene operation 30～35 ℃ enters thionizer by the bottom, and with reverse contact of doctor solution that cat head sprays, 30～35 ℃ of coke-oven gas that removed hydrogen sulfide enter air blast pressurization operation; The doctor solution that has absorbed the hydrogen sulfide in the coke-oven gas is discharged at the bottom of by tower, recycles after regeneration.
Air blast pressurization operation is: the coke-oven gas behind the desulfurization process is forced into 5000～8000Pa through centrifugal blower, and coke-oven gas is warming up to 50～55 ℃ naturally, enters sulphur ammonium operation.
Sulphur ammonium operation is: 50～55 ℃ of coke-oven gas after the centrifugal blower pressurization enter Spray Saturator with the ammonia in the sulfuric acid absorption coal gas, generate product ammonium sulfate; Clean coke-oven gas sub-fraction after the sulphur ammonium operation recycles as poor ammonia coal gas desorb remained ammonia, and all the other supply outward as high-grade fuel.
The ammonia desorption step is: the agent that removes that adds earlier 15～35g/L in the remained ammonia that the condensation operation is produced, modulation pH value to 10～14, again it is sent into reaction unit, reacted remained ammonia enters immersed type stripping desorption apparatus, the clean coke-oven gas of sub-fraction after the origin bin cure ammonium operation enters the desorb of subsurface one, the two section gas distributor stripping of immersed type stripping desorption apparatus, and the rich ammonia coal gas after the stripping desorb is got back to sulphur ammonium operation and produced ammonium sulfate.
Described 80～90 ℃ of coke-oven gas mainly are made up of inflammable gas component, chemical products component and water vapour; The inflammable gas component mainly is: hydrogen 45～54g/Nm
3, methane 170～210g/Nm
3, carbon monoxide 63～88g/Nm
3, ethane and homologue 13～26g/Nm thereof
3The chemical products component mainly is: coal tar 100～125g/Nm
3, benzene hydrocarbon 30～40g/Nm
3, ammonia 6～10g/Nm
3, hydrogen sulfide 7～12g/Nm
3, prussiate 0.5～1.5g/Nm
3, naphthalene 8～12g/Nm
3, sulfide 2～2.5g/Nm
3Water vapour content is 260～470g/Nm
3
Its chemical products component of clean coke-oven gas after present embodiment purifies and reclaims chemical products mainly comprises coal tar 0～0.01g/Nm
3, benzene hydrocarbon 2～4g/Nm
3, ammonia 0.03～0.1g/Nm
3, hydrogen sulfide 0～0.02g/Nm
3, prussiate 0～0.1g/Nm
3, naphthalene 0.05～0.1g/Nm
3, sulfide 0.05～0.2g/Nm
3Its inflammable gas component mainly comprises hydrogen 45～54g/Nm
3, methane 170～210g/Nm
3, carbon monoxide 63～88g/Nm
3, ethane and homologue 13～26g/Nm thereof
3Its water vapour content is 55～65g/Nm
3
Comparative Examples
Existing a kind of coke oven gas purification and recovery chemical products method.Its technical process is as shown in Figure 3: 80～90 ℃ coke-oven gas is forced into 11000～15000Pa through the centrifugal blower of air blast pressurization operation after the condensation operation is cooled to 20～27 ℃, coke-oven gas is warming up to 40～47 ℃ naturally; Again coke-oven gas is pre-chilled to 30～35 ℃ through pre-cooling working procedure, enter desulfurization process then and remove hydrogen sulfide in the coke-oven gas, remove 30～35 ℃ coke-oven gas behind the hydrogen sulfide and be preheated to 50～60 ℃ and enter sulphur ammonium operation, reclaim ammonia in the coke-oven gas to produce ammonium sulfate; 50～60 ℃ of coke-oven gas after the sulphur ammonium operation enter after final cooling process is cooled to 25～27 ℃ once more washes the benzene operation, with the benzene hydrocarbon in the washing oil absorption coke-oven gas; The washing oil that has absorbed benzene hydrocarbon forms rich oil, and rich oil reclaims benzene hydrocarbon by the crude benzol distillation process, and the clean coke-oven gas of washing after the benzene operation promptly supplies outward as clean fuel.Simultaneously, the remained ammonia that produces in coke oven gas purification and the chemical products removal process with steam desorb ammonia wherein, enters sulphur ammonium operation and produces ammonium sulfate in ammonia still process.
By present embodiment and Comparative Examples as can be seen:
1, because 20～27 ℃ coke-oven gas temperature of present embodiment after the condensation operation is lower, so this coke-oven gas directly enters and washes the benzene operation and the benzene hydrocarbon in the coke-oven gas is absorbed form rich oil in the washing oil.In washing the benzene operation, enter washing oil for preventing the steam condensation in this coke-oven gas, used washing oil temperature is a little more than this coke-oven gas temperature, washes that coke-oven gas is warming up to 30～35 ℃ naturally in the benzene operation, satisfies the requirement of desulfurization process to the coke-oven gas temperature.30～35 ℃ of coke-oven gas after the desulfurization are warming up to 50～55 ℃ naturally through the centrifugal blower pressurization of air blast pressurization operation, satisfy the requirement of sulphur ammonium operation to the coke-oven gas temperature, and coke-oven gas enters sulphur ammonium operation recovery ammonia wherein to produce ammonium sulfate.Thus, the technical process coke-oven gas of present embodiment only once is cooled to 20～27 ℃ of production requirements that can satisfy follow-up each operation in the condensation operation by 80～90 ℃, and as shown in Figure 2, the coke-oven gas temperature variation is orderly, graded is level and smooth, and energy consumption is low; And the technical process coke-oven gas of Comparative Examples is cooled off repeatedly, is heated, and as shown in Figure 4, temperature variation is unordered, graded is frequent, energy consumption is big.
2, because present embodiment is orderly by the coke-oven gas temperature variation, the graded principle of smoothing is provided with technical process, cancelled as shown in Figure 3 existing coke oven gas purification and primary heater unit in the pre-cooling working procedure in the chemical products recovery method, final cooling process and the sulphur ammonium operation, not only simplify technical process, and saved the energy.
3, because the technical process temperature variation of present embodiment is orderly, graded is level and smooth, compares with the method for Comparative Examples, can save energy more than 51%, correspondingly reduce production costs more than 33%.Because pre-cooling working procedure and the used recirculated water of final cooling process cooling coke-oven gas need to recycle after the cooling tower cooling in the method for Comparative Examples, phenol cyanogen pollutent contained in the recirculated water evaporates into contaminate environment in the atmosphere in a large number, so its technical process complexity, source of pollution are many, production cost is high; Present embodiment has been cancelled this two-step, and the pollutional equivalent that can reduce discharging atmospheric polluting material in coke oven gas purification and the chemical products removal process is more than 83%; Simultaneously, the ammonia desorption step of present embodiment can be increased to the removal efficiency of ammonia nitrogen in the remained ammonia more than 25%, reduces discharging deposed ammonia 20%.So the present embodiment energy consumption is low, production cost is low, environmental friendliness.
4, the air blast of present embodiment pressurization operation is arranged on the condensation operation, washes after benzene operation, crude benzol distillation process and the desulfurization process; make condensation operation in the whole process flow, wash the benzene operation, crude benzol distillation process, desulfurization process all be in negative pressure state production; eliminate each operation coke-oven gas and reached wherein leaking of toxic chemical substance, protected atmospheric environment.
Therefore, present embodiment has that temperature variation is orderly, graded is level and smooth, the technical process simplification, energy consumption is low, production cost is low, purification efficiency is high and eco-friendly characteristics.
Claims (9)
1. a coke oven gas purification and reclaim benzene hydrocarbon, the method of ammonia and coal tar, the technical process that it is characterized in that this method is: 80～90 ℃ coke-oven gas are directly advanced to wash the benzene operation after the condensation operation is cooled to 20～27 ℃, benzene hydrocarbon in the coke-oven gas absorbed form rich oil in the washing oil, 30～35 ℃ of coke-oven gas after washing the benzene operation enter the desulfurization process desulfurization, 30～35 ℃ of coke-oven gas after the desulfurization enter the pressurization of air blast pressurization operation, coke-oven gas is warming up to 50～55 ℃ naturally, naturally the sulphur ammonium operation that enters the coke-oven gas after heating up reclaims ammonia wherein, and the clean coke-oven gas after the sulphur ammonium operation supplies outward as high-grade fuel;
The remained ammonia that the condensation operation produces enters the ammonia desorption step ammonia is desorbed, and enters sulphur ammonium operation and produces ammonium sulfate;
Wash the rich oil process crude benzol distillation process recovery benzene hydrocarbon that the benzene operation produces.
2. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that described condensation operation is: 80～90 ℃ the coke-oven gas that comes from coke oven enters the transverse tube type water cooler, the transverse tube type water cooler divides epimere and hypomere, coke-oven gas is gone into water cooler epimere and recirculated water heat exchange earlier, be cooled to 40～45 ℃, reenter water cooler hypomere and chilled water heat exchange, be cooled to 20～27 ℃; Cooled coke-oven gas enters electrical tar precipitator, enters behind the capture coal tar droplet and washes the benzene operation;
After separating water outlet, the phlegma that the coke-oven gas cooling is produced is coal-tar products.
3. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that the described benzene operation of washing is: will enter by the bottom through cooled 20～27 ℃ coke-oven gas of condensation operation and wash the benzene tower, with temperature that cat head sprays is 27～32 ℃ reverse contact of circulating washing oil, the benzene hydrocarbon that washing oil absorbs in the coal gas forms rich oil, rich oil is gone out by tower bottom flow, deliver to the crude benzol distillation process, 30～35 ℃ of coke-oven gas washing behind the benzene tower enter desulfurization process.
4. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that described crude benzol distillation process is: will be from the rich oil elder generation of washing the benzene operation and the benzene hydrocarbon steam on debenzolizing tower top and the mixture heat exchange of steam, again with the hot oil-poor heat exchange of discharging at the bottom of the debenzolizing tower, enter the dehydration tower dehydration then, the rich oil after the dehydration is heated to 180～190 ℃ and enters the debenzolizing tower distillation; Discharge at the bottom of the benzene hydrocarbon steam of overflowing in debenzolizing tower top and the mixture of steam and the debenzolizing tower hot oil-poor successively with from the rich oil heat exchange of washing the benzene operation, hot oil-poor getting back to as washing oil after the heat exchange washed the benzene operation, the benzene hydrocarbon steam after the heat exchange and the mixture of steam carry out oily water separation after condensation, be the benzene hydrocarbon product after the separation water outlet.
5. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that described desulfurization process is: the coke-oven gas of washing after the benzene operation 30～35 ℃ enters thionizer by the bottom, with reverse contact of doctor solution that cat head sprays, 30～35 ℃ of coke-oven gas that removed hydrogen sulfide enter air blast pressurization operation;
The doctor solution that has absorbed the hydrogen sulfide in the coke-oven gas is discharged at the bottom of by tower, recycles after regeneration.
6. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that described air blast pressurization operation is: the coke-oven gas behind the desulfurization process is forced into 5000～8000Pa through centrifugal blower, coke-oven gas is warming up to 50～55 ℃ naturally, enters sulphur ammonium operation.
7. the method for coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, ammonia and coal tar, it is characterized in that described sulphur ammonium operation is: 50～55 ℃ of coke-oven gas after the centrifugal blower pressurization enter Spray Saturator with the ammonia in the sulfuric acid absorption coal gas, generate product ammonium sulfate; Clean coke-oven gas sub-fraction after the sulphur ammonium operation recycles as poor ammonia coal gas desorb remained ammonia, and all the other supply outward as high-grade fuel.
8. coke oven gas purification according to claim 1 and recovery benzene hydrocarbon, the method of ammonia and coal tar, it is characterized in that described ammonia desorption step is: the agent that removes that in the remained ammonia that the condensation operation is produced, adds earlier 15～35g/L, modulation pH value to 10～14, again it is sent into reaction unit, reacted remained ammonia enters immersed type stripping desorption apparatus, the clean coke-oven gas of sub-fraction after the origin bin cure ammonium operation enters immersed type stripping desorption apparatus subsurface, the desorb of two sections gas distributor strippings, the rich ammonia coal gas after the stripping desorb are got back to sulphur ammonium operation and are produced ammonium sulfate.
9. coke oven gas purification according to claim 1 and reclaim the method for benzene hydrocarbon, ammonia and coal tar is characterized in that described 80～90 ℃ of coke-oven gas mainly are made up of inflammable gas component, chemical products component and water vapour; The inflammable gas component mainly is: hydrogen 45～54g/Nm
3, methane 170～210g/Nm
3, carbon monoxide 63～88g/Nm
3, ethane and homologue 13～26g/Nm thereof
3The chemical products component mainly is: coal tar 100～125g/Nm
3, benzene hydrocarbon 30～40g/Nm
3, ammonia 6～10g/Nm
3, hydrogen sulfide 7～12g/Nm
3, prussiate 0.5～1.5g/Nm
3, naphthalene 8～12g/Nm
3, sulfide 2～2.5g/Nm
3Water vapour content is 260～470g/Nm
3
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Cited By (8)
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| CN102559288A (en) * | 2010-12-31 | 2012-07-11 | 中国海洋石油总公司 | Purification method of mixed gas obtained by coal gasification |
| CN102559285A (en) * | 2012-02-27 | 2012-07-11 | 重庆钢铁(集团)有限责任公司 | Coke oven gas finely-purifying process for multiple combustion engines |
| CN102732327A (en) * | 2012-06-26 | 2012-10-17 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN102810283A (en) * | 2012-07-26 | 2012-12-05 | 天津津大莱博科技有限公司 | Coal gasification methanol simulation training platform and control method thereof |
| CN103589462A (en) * | 2013-11-21 | 2014-02-19 | 王光华 | Technological method for purifying coal oven gas and recovering chemical products |
| CN105694988A (en) * | 2016-03-03 | 2016-06-22 | 金能科技股份有限公司 | Process for solving coal gas desulfuration liquid expansion in coking industry and system for process |
| CN105820846A (en) * | 2016-03-31 | 2016-08-03 | 四川天采科技有限责任公司 | Full-temperature-process pressure swing adsorption purification method for benzene removal and naphthalene removal of coke oven gas |
| CN108285154A (en) * | 2017-12-29 | 2018-07-17 | 攀钢集团西昌钢钒有限公司 | Precipitation ammonium sulfate device for making |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102559288A (en) * | 2010-12-31 | 2012-07-11 | 中国海洋石油总公司 | Purification method of mixed gas obtained by coal gasification |
| CN102559288B (en) * | 2010-12-31 | 2013-10-09 | 中国海洋石油总公司 | Purification method of mixed gas obtained by coal gasification |
| CN102559285A (en) * | 2012-02-27 | 2012-07-11 | 重庆钢铁(集团)有限责任公司 | Coke oven gas finely-purifying process for multiple combustion engines |
| CN102732327A (en) * | 2012-06-26 | 2012-10-17 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN102732327B (en) * | 2012-06-26 | 2014-04-09 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN102810283A (en) * | 2012-07-26 | 2012-12-05 | 天津津大莱博科技有限公司 | Coal gasification methanol simulation training platform and control method thereof |
| CN103589462A (en) * | 2013-11-21 | 2014-02-19 | 王光华 | Technological method for purifying coal oven gas and recovering chemical products |
| CN105694988A (en) * | 2016-03-03 | 2016-06-22 | 金能科技股份有限公司 | Process for solving coal gas desulfuration liquid expansion in coking industry and system for process |
| CN105820846A (en) * | 2016-03-31 | 2016-08-03 | 四川天采科技有限责任公司 | Full-temperature-process pressure swing adsorption purification method for benzene removal and naphthalene removal of coke oven gas |
| CN105820846B (en) * | 2016-03-31 | 2018-06-05 | 四川天采科技有限责任公司 | A kind of full temperature journey pressure swing adsorption purge method of coke-stove gas benzene-removal naphthalene-removal |
| CN108285154A (en) * | 2017-12-29 | 2018-07-17 | 攀钢集团西昌钢钒有限公司 | Precipitation ammonium sulfate device for making |
| CN108285154B (en) * | 2017-12-29 | 2021-08-17 | 攀钢集团西昌钢钒有限公司 | Device is prepared to heavy vanadium ammonium sulfate |
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