CN201990480U - Coke oven gas purifying device - Google Patents
Coke oven gas purifying device Download PDFInfo
- Publication number
- CN201990480U CN201990480U CN201120054163XU CN201120054163U CN201990480U CN 201990480 U CN201990480 U CN 201990480U CN 201120054163X U CN201120054163X U CN 201120054163XU CN 201120054163 U CN201120054163 U CN 201120054163U CN 201990480 U CN201990480 U CN 201990480U
- Authority
- CN
- China
- Prior art keywords
- gas
- hydrolysis
- outlet
- cog
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Abstract
The utility model relates to an industrial waste gas purifying device, in particular to a coke oven gas purifying device which purifies coke oven gas generated in the coking process into raw gas that is used for synthesis ammonia and synthesis methanol. The coke oven gas purifying device is characterized in that the device consists of a coke oven gas (COG) booster unit, a COG pretreating unit, a naphthalene recovery unit, a compressing unit, a pressure swing adsorption (PSA) unit and a hydrolyzing unit; when the coal gas is purified, the device can purify a large amount of coke oven gas that is discharged as waste gas into the high-quality raw gas for the synthesis ammonia and the synthesis methanol through boosting, pretreating, naphthalene recovering, compressing, pressure swing adsorption and hydrolyzing, thereby greatly saving coal resources, reducing discharge amount of the burnt gas, and obviously improving comprehensive utilization benefit of the resources.
Description
Technical field
The utility model relates to a kind of industrial waste-gas purifier, and specifically a kind of is the coke oven gas purification device that synthetic ammonia, synthesizing methanol are used unstripped gas with the coke oven gas purification that produces in the process of coking.
Background technology
In the Mineral resources structure of China, coal reserves is abundant and the hydrocarbon resources deficiency causes the consumption of coal resources in China's energy consumption structure to account for more than 40% of total energy consumption.And in the coal utilization course of processing, a large amount of coke(oven)gas (COG) that the large quantities of coal chemical enterprises of China can produce in process of coking, these coke(oven)gas that produced, except that a minimum part is used as fuel, the overwhelming majority is by direct " emptying ", not only cause serious environmental to pollute, and caused the waste of the energy.Coke(oven)gas is used as fuel, because its calorific value is low, dissemination is little.For coke-oven gas is utilized effectively, someone once proposed to use used as the unstripped gas of synthetic ammonia, synthesizing methanol, but because the coke-oven gas complicated component is difficult to directly apply to synthetic ammonia and methanol production, and lack supporting refining plant, fail to succeed always.Therefore, research and development are that synthetic ammonia, synthesizing methanol seem very necessary with the device of unstripped gas with coke oven gas purification.
Summary of the invention
The purpose of this utility model is that providing a kind of is the coke oven gas purification device that synthetic ammonia, synthesizing methanol are used unstripped gas with the coke oven gas purification that produces in the process of coking.
The technical scheme that the utility model coke oven gas purification device is adopted is as follows: design a kind of coke oven gas purification device, it is characterized in that: this device is made of COG boosting unit, COG pretreatment unit, bitter edible plant recovery unit, compressed element, PSA psa unit, hydrolysis unit;
Each unitary structure is as follows:
1) COG boosting unit: this unit comprises roots blower, the COG cooling tower, the circulation fluid water cooler, cooling column, coolant recirculation pump, cooling water circulating pump, the discharging of waste liquid pump, the intake header and the gas main of roots blower join, the outlet header is communicated with COG cooling tower bottom, be provided with the Pall ring packing layer in the COG cooling tower, the circulation fluid water cooler is arranged on outside the COG cooling tower, the fluid inlet of circulation fluid water cooler, liquid outlet is separately positioned on the top and the bottom of pipe in the circulation fluid water cooler, the fluid inlet of circulation fluid water cooler, liquid outlet is communicated with coolant recirculation pump liquid outlet and COG cooling tower top respectively by pipeline, the fluid inlet of coolant recirculation pump is communicated with COG cooling tower bottom by pipeline, the end of cooling column, top is respectively arranged with into, water outlet, the water outlet of cooling column communicates with recirculation cooler outer tube bottom by cooling water circulating pump, water-in communicates with recirculation cooler outer tube top by pipeline, discharging of waste liquid pump one end communicates with COG cooling tower bottom by pipeline, the other end communicates with bilge main, is provided with by-pass valve control on each connecting tube;
The roots blower of this COG boosting unit is 4, and 4 roots blowers are 3 to open 1 and be equipped with, and each roots blower outlet is equipped with sound damper, is connected with the coal gas return line between the outlet header of roots blower and intake header;
2) COG pretreatment unit: this unit comprises pretreater, resurgent gases water cooler and skimmer, the pretreater bottom is communicated with by pipeline with the COG cooling tower top of COG boosting unit, be provided with the active carbon filler layer in the pretreater, the top is provided with gas exit and steam, the import of regeneration blast-cold gas, steam inlet is connecting the pre-treatment steam inlet tube, the pretreater bottom is provided with steam and the outlet of regeneration blast-cold gas, the resurgent gases water cooler communicates with the outlet of pretreater bottom regeneration blast-cold gas by pipeline, the resurgent gases water cooler is being communicated with skimmer, the top of skimmer, the bottom is respectively equipped with vapor pipe and water shoot, water shoot communicates with bilge main, is provided with by-pass valve control on each connecting tube;
The pretreater of this COG pretreatment unit is 4, and 4 pretreaters are alternate run chronologically, and its operation system is: three are in on-line adsorption work, and one is in reproduction operation;
3) bitter edible plant is reclaimed the unit: this unit comprises condenser, circulation cooling tank, recycle pump, filter, sump pump, condenser overhead communicates with the pretreater bottom vapor outlet port of COG pretreatment unit by pipeline, circulation cooling tank top communicates with the condenser bottom, the liquid-inlet pipe of recycle pump and drain pipe communicate with the end, the middle part of circulation cooling tank respectively, the drain pipe of recycle pump is provided with the otch that can switch to filter, and be communicated with filter by this otch, sump pump one end communicates with filter, and the other end connects bilge main;
4) compressed element: this unit comprises compressor, the compressor two ends are communicated with by pipeline with the pretreater top gas exit of COG pretreatment unit and the oil removing tower bottom inlet mouth of PSA psa unit respectively, and the pipeline that connects compressor and pretreater is provided with being in charge of towards the methyl alcohol synthesizing section;
This compressed element has 3 on compressor, and its operating duty is 2 to open 1 and be equipped with, and is connected with the coal gas return line between the outlet header of compressor and intake header;
5) PSA psa unit: this unit comprises the oil removing tower, along the venting surge tank, the hydrogen rich gas surge tank, vacuum pump, contrary venting surge tank and at least 5 adsorption towers, the inlet mouth of oil removing tower communicates with the compressor outlet house steward of compressed element by pipeline, communicate by pipeline between each adsorption tower, each adsorption tower top is equipped with the hydrogen rich gas outlet, the bottom is equipped with gas inlet, inside is equipped with adsorption bed, acticarbon is arranged on the adsorption bed, each adsorption tower bottom gas inlet is communicated with by pipeline with oil removing tower air outlet, the hydrogen rich gas surge tank is arranged on the adsorption tower hydrogen rich gas delivery trunk, be communicated with each adsorption tower hydrogen rich gas output tube along venting surge tank pneumatic tube, contrary venting surge tank communicates with each adsorption tower gas inlet pipe by pneumatic tube, the two ends of vacuum pump all communicate with contrary venting surge tank pneumatic tube, contrary venting surge tank, all communicate with the pretreater top regeneration blast-cold gas import of COG pretreatment unit by regeneration blast-cold tracheae along venting surge tank top, each connecting tube is provided with by-pass valve control;
The adsorption tower of this PSA psa unit is 8, and wherein two adsorption towers are in online adsorbed state, and described is 2 along the venting surge tank;
6) hydrolysis unit: this unit comprises the hydrolysis preheater, the hydrolysis well heater, hydrolysis tower, the hydrolysis water cooler, the hydrolysis gas-liquid separator, the water of condensation tundish, smart thionizer, pipe and outer tube in the hydrolysis preheater is provided with, interior pipe bottom and top are respectively equipped with gas feed and pneumatic outlet, the bottom of outer tube and top are respectively equipped with pneumatic outlet and gas feed, the bottom of hydrolysis well heater is provided with gas feed and condensation-water drain, the top is provided with pneumatic outlet and steam inlet, steam inlet is connecting the hydrolysis steam inlet tube, the inlet mouth of pipe bottom communicates with the adsorption tower top hydrogen rich gas outlet of PSA psa unit by pipeline in the hydrolysis preheater, the air outlet at pipe top communicates with the gas feed of hydrolysis heater base in the hydrolysis preheater, the outlet of hydrolysis well heater top gas communicates with the hydrolysis tower bottom by pipeline, be provided with the hydrolytic reagent bed in the hydrolysis tower, the outlet of hydrolysis tower top gas communicates with hydrolysis preheater outer tube top inlet mouth by pipeline, the top of hydrolysis water cooler communicates with hydrolysis preheater outer tube bottom pneumatic outlet by pipeline, the bottom is connected by the inlet mouth of pipeline with the hydrolysis gas-liquid separator, hydrolysis gas-liquid separator bottom is provided with water vent, the top is provided with the air outlet, the air outlet of hydrolysis gas-liquid separator communicates with smart thionizer bottom by pipeline, be provided with the desulfurizing agent bed in the smart thionizer, the top is provided with clean gas outlet, the water of condensation tundish communicate with hydrolysis heater base condensation-water drain by pipeline, and each connecting tube is provided with by-pass valve control.
The utility model can carry out recycling with a large amount of coke-oven gas that process of coking produces, make as the coke-oven gas of off gas treatment by after the purifying treatment of this device, become the high quality raw material gas that is used for synthetic ammonia and synthesizing methanol, thereby, save coal resources greatly, reduce the combustion emission amount, significantly improve overall economic efficiency, realized energy-conserving and environment-protective, turn waste into wealth, the purpose of recycling economy and Sustainable development.
Description of drawings
Below in conjunction with the accompanying drawing narration, the utility model is described further:
Fig. 1 is the structural representation of this refining plant embodiment.
Among the figure: the 1-roots blower, the 2-COG cooling tower, 3-circulation fluid water cooler, the 4-cooling column, the 5-coolant recirculation pump, the 6-cooling water circulating pump, 7-discharging of waste liquid pump, 8-roots blower intake header, 9-roots blower outlet header, 10-coal gas return line, the 11-pretreater, 12-resurgent gases water cooler, the 13-skimmer, 14-skimmer vapor pipe, 15-skimmer water shoot, the 16-condenser, 17-circulation cooling tank, the 18-recycle pump, the 19-filter, the 20-sump pump, the 21-compressor, 22-coal gas return line, 23-oil removing tower, the 24-adsorption tower, 25-is along the venting surge tank, 26-hydrogen rich gas surge tank, the 27-vacuum pump, the contrary venting of 28-surge tank, 29-hydrolysis preheater, 30-hydrolysis well heater, the 31-hydrolysis tower, 32-hydrolysis water cooler, 33-hydrolysis gas-liquid separator, 34-water of condensation tundish, the smart thionizer of 35-, 36-pre-treatment steam inlet tube, 37-regeneration blast-cold tracheae, 38-leads to the methyl alcohol synthesizing section and is in charge of, 39-hydrolysis steam inlet tube.
Embodiment
As shown in Figure 1, this coke oven gas purification device is made of COG boosting unit, COG pretreatment unit, bitter edible plant recovery unit, compressed element, PSA psa unit, six productive units of hydrolysis unit;
The structure of each productive unit is as follows:
1) COG boosting unit: this unit comprises four roots blowers 1, a COG cooling tower 2, a circulation fluid water cooler 3, a cooling column 4, a coolant recirculation pump 5, a cooling water circulating pump 6, a discharging of waste liquid pump 7, the intake header 8 and the gas main of roots blower join, outlet header 9 is communicated with COG cooling tower 2 bottoms, each roots blower outlet is equipped with sound damper, be connected with coal gas return line 10 between the outlet header of roots blower and intake header, be provided with the Pall ring packing layer in the COG cooling tower 2, circulation fluid water cooler 3 is arranged on outside the COG cooling tower 2, the fluid inlet of circulation fluid water cooler 3, liquid outlet is separately positioned on the top and the bottom of pipe in the circulation fluid water cooler, the fluid inlet of circulation fluid water cooler, liquid outlet is communicated with coolant recirculation pump 5 liquid outlets and COG cooling tower 2 tops respectively by pipeline, the fluid inlet of coolant recirculation pump 5 is communicated with COG cooling tower 2 bottoms by pipeline, the end of cooling column 4, top is respectively arranged with into, water outlet, the water outlet of cooling column 4 communicates with recirculation cooler outer tube bottom by cooling water circulating pump 6, water-in communicates with recirculation cooler outer tube top by pipeline, discharging of waste liquid pump 7 one ends communicate with COG cooling tower 2 bottoms by pipeline, the other end communicates with bilge main, is provided with by-pass valve control on each connecting tube;
2) COG pretreatment unit: this unit comprises four pretreaters 11, a resurgent gases water cooler 12, a skimmer 13, four pretreaters are alternate run chronologically, its operation system is: three are in on-line adsorption work, one is in reproduction operation, each pretreater bottom is communicated with by pipeline with COG cooling tower 2 tops of COG boosting unit, be equipped with the active carbon filler layer in each pretreater, the top is equipped with gas exit and steam, the import of regeneration blast-cold gas, steam inlet is connecting pre-treatment steam inlet tube 36, each pretreater bottom is equipped with steam and the outlet of regeneration blast-cold gas, resurgent gases water cooler 12 communicates with each pretreater bottom regeneration blast-cold gas outlet by pipeline, resurgent gases water cooler 12 is being communicated with skimmer 13, the top of skimmer 13, the bottom is respectively equipped with vapor pipe 14 and water shoot 15, water shoot 15 communicates with bilge main, is provided with by-pass valve control on each connecting tube;
3) bitter edible plant is reclaimed the unit: this unit comprises condenser 16, circulation cooling tank 17, recycle pump 18, filter 19, respectively one of sump pump 20, condenser 16 tops communicate with each pretreater bottom vapor outlet port of COG pretreatment unit by pipeline, circulation cooling tank 17 tops communicate with condenser 16 bottoms, the liquid-inlet pipe of recycle pump 18 and drain pipe respectively with the end of circulation cooling tank 17, the middle part communicates, also be provided with the otch that can switch to filter 19 on the drain pipe of recycle pump 18, and be communicated with filter 19 by this otch, sump pump 20 1 ends communicate with filter 19, the other end connects bilge main, is provided with by-pass valve control on each connecting tube;
4) compressed element: this unit comprises three compressors 21, its operating duty is 2 to open 1 and be equipped with, compressor inlet house steward communicates by pipeline with each pretreater top gas exit of COG pretreatment unit, the outlet header is communicated with by pipeline with the oil removing tower bottom inlet mouth of PSA psa unit, the pipe connecting of compressor and each pretreater be provided with towards the methyl alcohol synthesizing section be in charge of 38, be connected with coal gas return line 22 between the outlet header of compressor and intake header;
5) PSA psa unit: this unit comprises an oil removing tower 23, eight adsorption towers 24, two along venting surge tank 25, a hydrogen rich gas surge tank 26, a vacuum pump 27, a contrary venting surge tank 28, the inlet mouth of oil removing tower 23 communicates with the compressor outlet house steward of compressed element by pipeline, two are in online adsorbed state all the time in 8 adsorption towers, communicate by pipeline between each adsorption tower, each adsorption tower top is equipped with the hydrogen rich gas outlet, the bottom is equipped with gas inlet, inside is equipped with adsorption bed, acticarbon is arranged on the adsorption bed, each adsorption tower bottom gas inlet is communicated with by pipeline with oil removing tower 23 air outlets, hydrogen rich gas surge tank 26 is arranged on each adsorption tower hydrogen rich gas delivery trunk, each pneumatic tube along the venting surge tank is communicated with each adsorption tower hydrogen rich gas output tube, the pneumatic tube of contrary venting surge tank 28 communicates with each adsorption tower gas inlet pipe, the two ends of vacuum pump 27 all communicate with contrary venting surge tank 28 pneumatic tubes by pipeline, each is along the venting surge tank, contrary venting surge tank top all communicates with each pretreater top regeneration blast-cold gas import of COG pretreatment unit by regeneration blast-cold tracheae 37, is provided with by-pass valve control on each connecting tube;
6) hydrolysis unit: this unit comprises hydrolysis preheater 29, hydrolysis well heater 30, hydrolysis tower 31, hydrolysis water cooler 32, hydrolysis gas-liquid separator 33, water of condensation tundish 34, respectively one of smart thionizer 35, pipe and outer tube in hydrolysis preheater 29 is provided with, interior pipe bottom and top are respectively equipped with gas feed and pneumatic outlet, the bottom of outer tube and top are respectively equipped with pneumatic outlet and gas feed, the bottom of hydrolysis well heater 30 is provided with gas feed and condensation-water drain, the top is provided with pneumatic outlet and steam inlet, steam inlet is connecting hydrolysis steam inlet tube 39, the inlet mouth of pipe bottom communicates with each adsorption tower top hydrogen rich gas outlet of PSA psa unit by pipeline in the hydrolysis preheater 29, the air outlet at pipe top communicates with the 30 bottom gas feeds of hydrolysis well heater in the hydrolysis preheater 29, the outlet of hydrolysis well heater 30 top gas communicates with hydrolysis tower 31 bottoms by pipeline, be provided with the hydrolytic reagent bed in the hydrolysis tower 31, the outlet of hydrolysis tower 31 top gas communicates with hydrolysis preheater 29 outer tube top inlet mouths by pipeline, the top of hydrolysis water cooler 32 communicates with hydrolysis preheater 29 outer tubes bottom pneumatic outlet by pipeline, the bottom is connected by the inlet mouth of pipeline with hydrolysis gas-liquid separator 33, hydrolysis gas-liquid separator 33 bottoms are provided with water vent, the top is provided with the air outlet, the air outlet of hydrolysis gas-liquid separator 33 communicates with smart thionizer 35 bottoms by pipeline, be provided with the desulfurizing agent bed in the smart thionizer 35, the top is provided with clean gas outlet, water of condensation tundish 34 communicate with the outlet of hydrolysis well heater 30 bottom condensate waters by pipeline, are provided with by-pass valve control on each connecting tube.
This refining plant scavenging process step is as follows:
1) the COG step raw coke oven gas that boosts enters each roots blower import by gas main, gas pressure is promoted to 55.0～58.0 KPa (G) from 4.0KPa (G), and after the sound damper by roots blower outlet carries out noise reduction, coal gas is sent in the COG cooling tower from COG cooling tower bottom by pipeline, make by coolant recirculation pump simultaneously that the cooling fluid in the pipe enters in the tower from cooling tower top in the external placed type circulation fluid water cooler, pass the packing layer in the tower from top to bottom, carry out heat exchange with the coal gas that passes packing layer from bottom to top and remove heat, make gas temperature reduce to 40-15 ℃ from 45-55 ℃; For guaranteeing the roots blower intake pressure, part coal gas refluxes by the outlet header of connection roots blower and the return line of intake header, carries out ftercompction and latent the pressure with the intake header pressure to roots blower; In the liquid circulation process, by cooling water circulating pump the cold water in the cooling column is constantly circulated in circulation fluid water cooler outer tube, so that cooling fluid keeps cooling temperature, the waste liquid that accumulates in the COG cooling tower after heat exchange is finished is extracted out by the discharging of waste liquid pump and is entered bilge main, draws from COG cooling tower top through the coal gas that boosts of cooling, washing and enters next purifying step;
2) pipeline of the pretreater bottom of the COG pre-treatment step coal gas of drawing from the COG cooling tower top of COG boosting unit by connecting COG cooling tower and COG pretreatment unit enters in each pretreater that is in online adsorbed state, coal gas passes the active carbon filler layer in the tower from bottom to top, makes benzene, naphthalene, tar, ammonia and other heavy hydrocarbons organic substance and section H in the coal gas
2S, COS, CS
2, thiophene, thioether sulfides absorbed by packing layer, coal gas after the purification shifts out from the top of pretreater, and through the assignment of traffic adjusting, a part is transported to the COG compressed element and further purifies, and another part is transported to Methanol Plant as the unstripped gas of producing methyl alcohol;
After a pretreater absorption is saturated, promptly change regenerative process over to.The regenerative process step is as follows: at first, to add pressure be that the steam of 0.1-0.14 MPa (G) heats pretreater from adsorbing saturated pretreater top, make the adsorbent temperature in the tower rise to 95-105 ℃, the benzene of adsorbent surface will be adsorbed on, naphthalene and other heavy hydrocarbons organic impurity parse, and discharge from pretreater bottom with low-pressure steam, be transported to the bitter edible plant and reclaim the unit, add steam after 40-80 hours, stop the steam input, to add from top of tower from the regeneration blast-cold gas of PSA psa unit then, sorbent material is lowered the temperature and dried up, the regeneration blast-cold gas that contains steam is discharged from tower bottom, and cool through the resurgent gases water cooler, carrying out gas-liquid by the COG skimmer separates, regeneration blast-cold gas after dewatering is by emission by exhaust pipe, and isolated water of condensation enters bilge main and discharges, thereby finishes the pretreater regenerative process;
3) how recycling step in pre-treatment step pretreater regenerative process, produce contain a large amount of benzene, how, the aqueous vapor of tar and other heavy hydrocarbons organic impurity enters condenser by pipeline from the top of how reclaiming unitary condenser, and in condenser, coagulate entirely, condensed cooling fluid flows into the circulation cooling tank from top to bottom and continues cooling, make naphthalene wherein be condensed into solid, by recycle pump the slurries in the circulation cooling tank are carried out pump circulation simultaneously, slurries are extracted out from pot bottom, after the recycle pump pressurization, return in the jar from the middle part of jar, when the solution level in the jar arrives the circulation liquid-inlet pipe mouth of pipe, outlet of circulating pump is switched to filter, Gu solution carries out liquid through filter in jar---separate, the solution part is extracted out by sump pump and is entered bilge main, the separated collection of the solid bitter edible plant;
4) compression step enters each compressor of compressed element through the coal gas of rough purification by pipeline from the COG pretreatment unit, and the pressure that purifies coal gas is pressurized to 0.750-0.850MPa (G) by 0.045MPa (G), then, is sent to the PSA psa unit; For guaranteeing the intake pressure of compressor, part coal gas refluxes by the outlet header of connection compressor and the return line of intake header, carries out ftercompction and latent the pressure with the intake header pressure to compressor;
5) the adsorption tower bottom from the PSA psa unit after the oil removing of oil removing tower of the coke-oven gas after PSA transformation adsorption step boosts enters in the adsorption tower that is in on-line adsorption, pass the charcoal absorption bed that is provided with in the adsorption tower from bottom to top, under the sorbent material selective adsorption, the disposable CH that removes in the coal gas
4Gas obtains CH
4Content is less than 0.80% hydrogen rich gas, hydrogen rich gas is discharged the laggard further desulfurizing and purifying in hydrolysis unit of going into from top of tower, when the mass transfer zone forward position that is adsorbed gas arrives the hydrogen rich gas outlet at adsorption tower top, stop adsorption operations, change this adsorption tower over to the adsorbent reactivation process;
The regenerative process step of sorbent material is as follows:
(1) drop pressure is after the adsorption tower adsorption process finishes, along the absorption direction hydrogen rich gas of the elevated pressures in the tower is put into other and finished regenerated lower pressure adsorption tower, this process is not only the step-down process, reclaim the process of bed dead space hydrogen rich gas especially, this step comprises four successive continuous release gas process to different adsorption towers altogether, and the pressure in the adsorption tower is reduced to 0.300-0.200 MPa (G) by 0.750-0.850 MPa (G);
(2) along be placed on all push back receive the hydrogen rich gas end of processing after, continuation is reduced pressure along the absorption direction, pressure in the adsorption tower is reduced to 0.180-0.100 MPa (G) by 0.200-0.300 MPa (G), put into along the venting surge tank along the hydrogen rich gas of releasing and to mix and store, as the regenerate source of the gas of blast-cold gas of adsorption tower flushing and pretreatment system;
(3) contrary being placed on along after putting end, against the absorption direction adsorption column pressure is reduced to 0.010-0.001 MPa (G), the impurity that be adsorbed this moment begins to parse in a large number from sorbent material, and contrary putting resolved pneumatic transmission to contrary venting surge tank, as the regeneration blast-cold source of the gas of pretreatment system;
(4) flushing is for being regenerated sorbent material completely, and against absorption direction flushing adsorption bed, the flushing resurgent gases after the flushing is delivered to pretreatment system as regeneration blast-cold source of the gas by the contrary surge tank of exitting with the hydrogen rich gas that stores in the suitable venting surge tank;
(5) vacuumize after flushing finishes, utilize vacuum pump to bleed against adsorption tower, adsorption column pressure is evacuated to-0.040Mpa, the gas that vacuum pump is extracted out is sent in the contrary venting surge tank, as the regeneration blast-cold source of the gas of pretreatment system;
(6) boost pressure is vacuumizing after step finishes, elevated pressures hydrogen rich gas with other adsorption tower boosts to this adsorption tower successively, this process is corresponding with the drop pressure process, be not only the process of boosting, and be the process that reclaims the bed dead space hydrogen rich gas of other tower, this step comprises continuous four boost pressure intake processes altogether, and the pressure in the adsorption tower is risen to 0.500-0.550MPa (G);
(7) the purified gas final rise is after the boost pressure step is finished, for adsorption tower can be switched to reposefully adsorb and guarantee that product purity does not fluctuate in adsorption process next time, slowly and reposefully adsorption column pressure is risen to absorption operating pressure 0.750-0.850 MPa (G) with the hydrogen rich gas that stores in the hydrogen rich gas surge tank by the pressure regulator valve on the adsorption tower, thereby finish the adsorbent reactivation process, for absorption is next time got ready;
6) hydrolysing step at first enters by connecting tube from the hydrogen rich gas of PSA psa unit and carries out preheating in the hydrolysis preheater in the pipe, enter the hydrolysis well heater again and continue heat temperature raising to 150-270 ℃ by steam, the liquid that produces in the heat-processed enters the water of condensation tundish, hydrogen rich gas after the heating is drawn the bottom that enters hydrolysis tower from the top of hydrolysis well heater, pass the hydrolytic reagent bed from bottom to top, make in the hydrolytic reagent bed, the be hydrolyzed reaction and generate hydrogen sulfide of organosulfur in the gas, gas after the hydrolysis shifts out from the top of hydrolysis tower by the hydrolysis preheater and carries out heat recuperation and the hydrolysis water cooler is lowered the temperature, make gas temperature reduce to 40-10 ℃, gas after the cooling enters the hydrolysis gas-liquid separator and carries out the solution-air separation, the liquid that decomposites is discharged from the water vent of hydrolysis gas-liquid separator bottom, the gas that decomposites is introduced from the bottom of smart thionizer, pass the sweetening agent bed that is provided with in the smart thionizer from bottom to top, with the hydrogen sulfide adsorbing and removing in the gas, make the total sulfur content in the gas reach 0.1mg/Nm
3Below, promptly can be used as syngas for synthetic ammonia through the purified gas of smart desulfurization and be used for Ammonia Production.
Claims (5)
1. a coke oven gas purification device is characterized in that, it is made of COG boosting unit, COG pretreatment unit, bitter edible plant recovery unit, compressed element, PSA psa unit, six productive units of hydrolysis unit:
1) COG boosting unit: this unit comprises roots blower, the COG cooling tower, the circulation fluid water cooler, cooling column, coolant recirculation pump, cooling water circulating pump, the discharging of waste liquid pump, the intake header and the gas main of roots blower join, the outlet header is communicated with COG cooling tower bottom, be provided with the Pall ring packing layer in the COG cooling tower, the circulation fluid water cooler is arranged on outside the COG cooling tower, the fluid inlet of circulation fluid water cooler, liquid outlet is separately positioned on the top and the bottom of pipe in the circulation fluid water cooler, the fluid inlet of circulation fluid water cooler, liquid outlet is communicated with coolant recirculation pump liquid outlet and COG cooling tower top respectively by pipeline, the fluid inlet of coolant recirculation pump is communicated with COG cooling tower bottom by pipeline, the end of cooling column, top is respectively arranged with into, water outlet, the water outlet of cooling column communicates with recirculation cooler outer tube bottom by cooling water circulating pump, water-in communicates with recirculation cooler outer tube top by pipeline, discharging of waste liquid pump one end communicates with COG cooling tower bottom by pipeline, the other end communicates with bilge main, is provided with by-pass valve control on each connecting tube;
2) COG pretreatment unit: this unit comprises pretreater, resurgent gases water cooler and skimmer, the pretreater bottom is communicated with by pipeline with the COG cooling tower top of COG boosting unit, be provided with the active carbon filler layer in the pretreater, the top is provided with gas exit and steam, the import of regeneration blast-cold gas, steam inlet is connecting the pre-treatment steam inlet tube, the pretreater bottom is provided with steam and the outlet of regeneration blast-cold gas, the resurgent gases water cooler communicates with the outlet of pretreater bottom regeneration blast-cold gas by pipeline, the resurgent gases water cooler is being communicated with skimmer, the top of skimmer, the bottom is respectively equipped with vapor pipe and water shoot, water shoot communicates with bilge main, is provided with by-pass valve control on each connecting tube;
3) bitter edible plant is reclaimed the unit: this unit comprises condenser, circulation cooling tank, recycle pump, filter, sump pump, condenser overhead communicates with the pretreater bottom vapor outlet port of COG pretreatment unit by pipeline, circulation cooling tank top communicates with the condenser bottom, the liquid-inlet pipe of recycle pump and drain pipe communicate with the end, the middle part of circulation cooling tank respectively, the drain pipe of recycle pump is provided with the otch that can switch to filter, and be communicated with filter by this otch, sump pump one end communicates with filter, and the other end connects bilge main;
4) compressed element: this unit comprises compressor, the compressor two ends are communicated with by pipeline with the pretreater top gas exit of COG pretreatment unit and the oil removing tower bottom inlet mouth of PSA psa unit respectively, and the pipeline that connects compressor and pretreater is provided with being in charge of towards the methyl alcohol synthesizing section;
5) PSA psa unit: this unit comprises the oil removing tower, along the venting surge tank, the hydrogen rich gas surge tank, vacuum pump, contrary venting surge tank and at least 5 adsorption towers, the inlet mouth of oil removing tower communicates with the compressor outlet house steward of compressed element by pipeline, communicate by pipeline between each adsorption tower, each adsorption tower top is equipped with the hydrogen rich gas outlet, the bottom is equipped with gas inlet, inside is equipped with adsorption bed, acticarbon is arranged on the adsorption bed, each adsorption tower bottom gas inlet is communicated with by pipeline with oil removing tower air outlet, the hydrogen rich gas surge tank is arranged on the adsorption tower hydrogen rich gas delivery trunk, be communicated with each adsorption tower hydrogen rich gas output tube along venting surge tank pneumatic tube, contrary venting surge tank communicates with each adsorption tower gas inlet pipe by pneumatic tube, the two ends of vacuum pump all communicate with contrary venting surge tank pneumatic tube, contrary venting surge tank, all communicate with the pretreater top regeneration blast-cold gas import of COG pretreatment unit by regeneration blast-cold tracheae along venting surge tank top, each connecting tube is provided with by-pass valve control;
6) hydrolysis unit: this unit comprises the hydrolysis preheater, the hydrolysis well heater, hydrolysis tower, the hydrolysis water cooler, the hydrolysis gas-liquid separator, the water of condensation tundish, smart thionizer, pipe and outer tube in the hydrolysis preheater is provided with, interior pipe bottom and top are respectively equipped with gas feed and pneumatic outlet, the bottom of outer tube and top are respectively equipped with pneumatic outlet and gas feed, the bottom of hydrolysis well heater is provided with gas feed and condensation-water drain, the top is provided with pneumatic outlet and steam inlet, steam inlet is connecting the hydrolysis steam inlet tube, the inlet mouth of pipe bottom communicates with the adsorption tower top hydrogen rich gas outlet of PSA psa unit by pipeline in the hydrolysis preheater, the air outlet at pipe top communicates with the gas feed of hydrolysis heater base in the hydrolysis preheater, the outlet of hydrolysis well heater top gas communicates with the hydrolysis tower bottom by pipeline, be provided with the hydrolytic reagent bed in the hydrolysis tower, the outlet of hydrolysis tower top gas communicates with hydrolysis preheater outer tube top inlet mouth by pipeline, the top of hydrolysis water cooler communicates with hydrolysis preheater outer tube bottom pneumatic outlet by pipeline, the bottom is connected by the inlet mouth of pipeline with the hydrolysis gas-liquid separator, hydrolysis gas-liquid separator bottom is provided with water vent, the top is provided with the air outlet, the air outlet of hydrolysis gas-liquid separator communicates with smart thionizer bottom by pipeline, be provided with the desulfurizing agent bed in the smart thionizer, the top is provided with clean gas outlet, the water of condensation tundish communicate with hydrolysis heater base condensation-water drain by pipeline, and each connecting tube is provided with by-pass valve control.
2. a kind of coke oven gas purification device according to claim 1, it is characterized in that the roots blower of described COG boosting unit is 4,4 roots blowers are 3 to open 1 and be equipped with, each roots blower outlet is equipped with sound damper, is connected with the coal gas return line between the outlet header of roots blower and intake header.
3. a kind of coke oven gas purification device according to claim 1, it is characterized in that the pretreater of described COG pretreatment unit is 4,4 pretreaters are alternate run chronologically, its operation system is: three are in on-line adsorption work, and one is in reproduction operation.
4. a kind of coke oven gas purification device according to claim 1 is characterized in that described compressed element has 3 on compressor, and its operating duty is 2 to open 1 and be equipped with, and is connected with the coal gas return line between the outlet header of compressor and intake header.
5. a kind of coke oven gas purification device according to claim 1 is characterized in that the adsorption tower of described PSA psa unit is 8, and wherein two adsorption towers are in online adsorbed state all the time, and described is 2 along the venting surge tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120054163XU CN201990480U (en) | 2011-03-03 | 2011-03-03 | Coke oven gas purifying device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120054163XU CN201990480U (en) | 2011-03-03 | 2011-03-03 | Coke oven gas purifying device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201990480U true CN201990480U (en) | 2011-09-28 |
Family
ID=44666974
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120054163XU Expired - Lifetime CN201990480U (en) | 2011-03-03 | 2011-03-03 | Coke oven gas purifying device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201990480U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139860A (en) * | 2011-03-03 | 2011-08-03 | 韩城市黑猫能源利用有限公司 | Device and method for purifying coke oven gas |
| CN103205278A (en) * | 2013-04-10 | 2013-07-17 | 山西鑫立能源科技有限公司 | Thermal-cycle continuous pyrolysis-gasification comprehensive device for coal gangues |
| CN103242910A (en) * | 2013-04-10 | 2013-08-14 | 山西鑫立能源科技有限公司 | Hot waste gas active coke regeneration device combining pyrolysis and gasification of coal gangue and purification and combustion of raw gas |
-
2011
- 2011-03-03 CN CN201120054163XU patent/CN201990480U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139860A (en) * | 2011-03-03 | 2011-08-03 | 韩城市黑猫能源利用有限公司 | Device and method for purifying coke oven gas |
| CN102139860B (en) * | 2011-03-03 | 2013-03-20 | 韩城市黑猫能源利用有限公司 | Device and method for purifying coke oven gas |
| CN103205278A (en) * | 2013-04-10 | 2013-07-17 | 山西鑫立能源科技有限公司 | Thermal-cycle continuous pyrolysis-gasification comprehensive device for coal gangues |
| CN103242910A (en) * | 2013-04-10 | 2013-08-14 | 山西鑫立能源科技有限公司 | Hot waste gas active coke regeneration device combining pyrolysis and gasification of coal gangue and purification and combustion of raw gas |
| CN103242910B (en) * | 2013-04-10 | 2014-06-11 | 山西鑫立能源科技有限公司 | Hot waste gas active coke regeneration device combining pyrolysis and gasification of coal gangue and purification and combustion of raw gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102139860B (en) | Device and method for purifying coke oven gas | |
| CN102250658A (en) | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas | |
| CN101874967A (en) | Process for removing acid gas with low-temperature methanol solution | |
| CN107758617A (en) | A kind of biogas biolobic material hydrogen production process | |
| CN110127613B (en) | Efficient and advanced hydrogen production process by using coke oven gas | |
| CN107512702A (en) | Hydrogen production from coke oven gas technique | |
| CN202297109U (en) | Total recycle low-pressure hydrogen recovery device | |
| CN105820846B (en) | A kind of full temperature journey pressure swing adsorption purge method of coke-stove gas benzene-removal naphthalene-removal | |
| CN106281476A (en) | A kind of low temperature washing device for methanol and a kind of remove the method for sour gas in synthesis gas | |
| CN102190541A (en) | Method for recovering methane for industrial production of clean fuel through deep purification of landfill gas | |
| CN102199433A (en) | Coal carbonization technology with treating CO2 as temperature control component in combustion process | |
| CN105294394A (en) | Methanol co-production recycling system | |
| CN201990480U (en) | Coke oven gas purifying device | |
| CN113387772A (en) | Method for synthesizing ethylene glycol by using coke oven gas | |
| CN104745260A (en) | Method and equipment for preparing and storing high-quality natural gas from marsh gas | |
| CN102765733B (en) | Device and technique of producing liquid ammonia by coke oven gas and methanol relief gas | |
| CN102489120B (en) | Low temperature methanol wash method and equipment | |
| CN109054893B (en) | System for hydrogen purification and wax oil hydrogenation coupling in coal hydrogen production | |
| CN102173379A (en) | Method for producing sulfur, hydrogen and low-sulfur desorption gas from coal gas | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN101724479A (en) | Method for pressure swing adsorption and concentration of methane | |
| CN101434872A (en) | Method for adding distilled ammonia vapor into desulfurized solution in ammonia desulphurization process and special equipment thereof | |
| CN203429147U (en) | Methane purifying system | |
| CN104845657A (en) | Purification system and process for recycling residual light oil in shale oil dry distillation tail gas | |
| CN108102727A (en) | For the method for coke oven gas purification recycling aromatic hydrocarbons |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20110928 Effective date of abandoning: 20130320 |
|
| RGAV | Abandon patent right to avoid regrant |