CN211005244U - System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation - Google Patents
System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation Download PDFInfo
- Publication number
- CN211005244U CN211005244U CN201921836184.XU CN201921836184U CN211005244U CN 211005244 U CN211005244 U CN 211005244U CN 201921836184 U CN201921836184 U CN 201921836184U CN 211005244 U CN211005244 U CN 211005244U
- Authority
- CN
- China
- Prior art keywords
- gas
- sulfur
- methanation
- dry distillation
- temperature
- 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.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model discloses a system for well low temperature dry distillation raw coke oven gas is through resistant sulphur samming temperature methanation system CNG belongs to the clean high-efficient technical field that utilizes of coal, carry out tar recovery after with dry distillation raw coke oven gas dust removal deamination purification, obtain high value by-product, repressurization liquefaction separation is with direct preparation into L PG of higher hydrocarbons such as propane, butane, the H that desulfurization decarbonization device analyzed out2The S gas has high purity, sulfur can be recovered by adopting a Claus sulfur recovery process, and combustible gas generated by nitrogen separated by a pressure swing adsorption system is used as combustion gas, so that the cost is saved. Gas component CH after separation of nitrogen by PSA4The system is simple and convenient to operate, realizes clean and efficient utilization of low-rank coal by adopting a coal low-temperature dry distillation poly-generation technology, produces high-calorific-value compressed natural gas and byproducts such as tar, L PG, sulfur, carbon dioxide and the like, saves energy and has high economic benefit.
Description
Technical Field
The utility model belongs to the technical field of the clean high-efficient utilization of coal, concretely relates to system of well low temperature dry distillation raw coke oven gas through resistant sulphur samming methanation system CNG (compressed natural gas).
Background
Natural gas, as a high-efficiency, clean and safe fossil energy, has increased year by year in global energy consumption; along with the enhancement of environmental awareness and the improvement of life quality of people, the demand of natural gas is increased year by year, coal resources with relatively rich reserves are utilized to deeply develop a low-temperature dry distillation natural gas co-production technology of low-quality coal, and raw gas with lower heat value is utilized to be converted into environment-friendly natural gas, so that the comprehensive utilization of the coal resources is realized, the phenomenon of relative shortage of oil and gas resources in China is relieved, and the clean and efficient utilization technical route of coal is met.
Three products, namely semi coke, coal tar and raw coke gas (also comprising the raw coke) are obtained in the process of producing the semi coke by low-temperature dry distillation of the low-quality coalThe semi-coke tail gas or the low-temperature dry distillation gas) produced by a semi-coke production device generally adopting flue gas for heating is shown in table 1, so that the crude gas components have low methane content, low gas heat value and large amount of nitrogen, the energy consumption in the compression and liquefaction processes is high, the process cost for directly purifying methane from gas is high, the crude gas is generally combusted by a boiler to produce steam and generate electricity at present, and the economic benefit is low. The coal can generate a large amount of H in the low-temperature dry distillation process2CO and CO2But the hydrogen-carbon ratio (H/C) is about 1.8-2.2, which is not beneficial to methanation reaction, and also contains C2-C4 paraffin and olefin as main petroleum gas components, H2S、NH3And tar, dust, etc.
Table 1: crude gas component of traditional vertical furnace
With the development of the low-temperature dry distillation technology of pulverized coal in recent years, technologies such as an external heating type vertical furnace, a solid heat carrier low-temperature rapid pyrolysis technology, a pulverized coal rotary kiln pyrolysis technology and the like appear, the technology is different from the prior mode that flue gas is directly heated by adopting indirect heating, the produced raw coke oven gas has more effective combustible components, the general components of the raw coke oven gas are shown in a table 2, the content of nitrogen is obviously reduced, but the problems of low hydrogen-carbon ratio and high carbon dioxide content still exist.
Table 2: indirectly heated raw gas component for pyrolysis technology
Because of the characteristics of the raw coke oven gas, unlike the coke oven gas which is easy to prepare natural gas, the development of a technology for preparing natural gas by methanation, which is suitable for the raw coke oven gas, is urgently needed, and the technology can be used for preparing natural gas at a low H/C ratio and high CO2Under the condition of partial pressure, high CO conversion rate and high CH are realized4And (4) selectivity.
Disclosure of Invention
In order to solve the existing problem, the utility model aims to provide a well low temperature dry distillation raw coke oven gas has realized the clean high-efficient utilization of low order coal through the system of resistant sulphur samming methanation system CNG, produces the compressed natural gas of high calorific value and by-products such as by-product tar, L PG, sulphur, carbon dioxide, the energy saving, economic benefits is high.
The utility model discloses a following technical scheme realizes:
the utility model discloses a system for preparing CNG from middle and low temperature dry distillation raw gas through sulfur-resistant uniform temperature methanation, which comprises a deamination dust removal device, wherein the inlet of the deamination dust removal device is connected with a middle and low temperature dry distillation raw gas inlet pipe, the outlet of the deamination dust removal device is connected with a primary compression device, the primary compression device is connected with a tar recovery device, the tar recovery device is connected with a secondary compression device, the secondary compression device is connected with a sulfur-resistant methanation device and a liquefied petroleum gas collection device, the sulfur-resistant methanation device is connected with a desulfurization and decarbonization device, the desulfurization and decarbonization device is connected with a dehydration adsorption, carbon dioxide collection device and hydrogen sulfide collection device, hydrogen sulfide collection device are connected with claus sulphur recovery unit, and the dehydration adsorption tower is connected with pressure swing adsorption equipment, and pressure swing adsorption equipment is connected with nitrogen gas collection device and tertiary compression device, and tertiary compression device is connected with the CNG outlet duct.
Preferably, the first-stage compression device is a screw compressor, the second-stage compression device is a piston compressor, and the third-stage compression device is a centrifugal compressor.
Preferably, the tar recovery device is a rectifying tower or a temperature swing adsorption device.
Preferably, an oxygen removing device is arranged between the tar recovery device and the secondary compression device.
Preferably, the sulfur-resistant methanation device is a tubular uniform temperature reactor, a cobalt-molybdenum catalyst is arranged in a tube pass of the tubular uniform temperature reactor, and boiling water is 60-100 bar in a shell pass; the two ends of the tube pass are respectively connected with the secondary compression device and the desulfurization and decarburization device.
Further preferably, the shell side is connected with a steam drum, and the shell side, the steam drum, the tar recovery device and the desulfurization and decarburization device form a closed circulation loop of boiling water/saturated steam.
Preferably, the desulfurization and decarbonization device comprises a desulfurization tower and a decarbonization tower which are filled with MDEA solution, the inlet of the decarbonization tower is connected with the sulfur-tolerant methanation device, the outlet of the decarbonization tower is connected with the inlet of the desulfurization tower and the dehydration adsorption tower, and the outlet of the desulfurization tower is connected with the hydrogen sulfide collection device.
Preferably, the pressure swing adsorption unit is a pressure swing adsorption column.
Compared with the prior art, the utility model discloses following profitable technological effect has:
the utility model discloses a system of well low temperature dry distillation raw coke oven gas through resistant sulphur samming temperature methanation system CNG, with dry distillation raw coke oven gas remove dust the deamination and purify the back and carry out tar earlier and retrieve, obtain high-value by-product, the separation of repressurization liquefaction is with the direct L PG that prepares into of higher hydrocarbons such as propane, butane in the dry distillation coal gas, the effective utilization of a large amount of higher hydrocarbons simultaneously, greatly reduced the carbon load of methanation workshop section, methanation catalyst thermal stability has been improved, the life-span of methanation catalyst has been prolonged, H that desulfurization decarbonization device was analyzed out2The S gas has high purity, sulfur can be recovered by adopting a Claus sulfur recovery process, and combustible gas generated by nitrogen separated by a pressure swing adsorption system is used as combustion gas, so that the cost is saved. Gas component CH after separation of nitrogen by PSA4The content is high and is more than 95 percent, and the requirement of a first-grade natural gas product is met, the low-temperature dry distillation poly-generation technology of coal is adopted, the clean and efficient utilization of low-rank coal is realized, and the high-calorific-value compressed natural gas is produced and byproducts such as tar, L PG, sulfur, carbon dioxide and the like are produced.
Furthermore, the first-stage compression device is a screw compressor, the second-stage compression device is a piston compressor, the third-stage compression device is a centrifugal compressor, the type of the compression device is selected according to actual needs, the setting is reasonable, and the cost is saved.
Furthermore, an oxygen removal device is arranged between the tar recovery device and the secondary compression device, so that the activity of the catalyst in the subsequent reactor can be protected.
Furthermore, the sulfur-tolerant cobalt-molybdenum catalyst is adopted, has the dual-function catalytic action of transformation and methanation, omits the traditional wet desulphurization and dry desulphurization process sections, and adopts the tubular reactor to replace the traditional multi-section adiabatic fixed bed reactionThe reactor shortens the process flow and saves the equipment investment; the combination of the sulfur-tolerant methanation catalyst and the temperature-equalizing tubular reactor controls the reaction temperature to be 300-400 ℃, thereby realizing high CO conversion rate and high CH of the raw coke oven gas with low hydrogen-carbon ratio4Selectivity, solves the problems of low CO conversion rate and CO conversion at the high temperature of 650 ℃ in the traditional heat-insulating bed of 550-2High selectivity (high reaction rate at high temperature in water gas reaction).
Furthermore, the medium-pressure steam generated by the shell and tube reactor can provide heat for the tar recovery device and the desulfurization and decarburization device, so that the optimal utilization of heat is realized, and the energy is saved.
Further, desulfurization and decarburization are carried out in one unit, and H can be removed simultaneously through an MDEA absorption tower2S and CO2Acid gas, for CO2At concentrations less than 30%, MDEA (diethanolamine) absorption desorption is more economical than PSA.
Drawings
FIG. 1 is a schematic view of the whole system for producing CNG from medium and low temperature dry distillation raw gas through sulfur-tolerant temperature equalization methanation.
In the figure: 1-medium and low temperature carbonization raw gas inlet pipe, 2-deamination dust removal device, 3-primary compression device, 4-tar recovery device, 5-secondary compression device, 6-sulfur-tolerant methanation device, 7-desulfurization and decarburization device, 8-Claus sulfur recovery device, 9-dehydration adsorption tower, 10-pressure swing adsorption device, 11-tertiary compression device, 12-liquefied petroleum gas collection device, 13-hydrogen sulfide collection device, 14-carbon dioxide collection device, 15-nitrogen collection device and 16-CNG outlet pipe.
Detailed Description
The invention will be described in further detail with reference to the following drawings and specific examples, which are intended to illustrate and not to limit the invention:
FIG. 1 is a system for producing CNG by sulfur-tolerant uniform-temperature methanation of middle and low temperature dry distillation raw gas, which comprises a deamination dust collector 2, wherein the inlet of the deamination dust collector 2 is connected with a middle and low temperature dry distillation raw gas inlet pipe 1, the outlet of the deamination dust collector is connected with a primary compressor 3, the primary compressor 3 is connected with a tar recovery device 4, and the tar recovery device 4 can adopt a rectifying tower or a temperature swing adsorption device; the tar recovery device 4 is connected with a secondary compression device 5, and a deaerating device can be arranged between the tar recovery device 4 and the secondary compression device 5; the secondary compression device 5 is connected with a sulfur-resistant methanation device 6 and a liquefied petroleum gas collection device 12, the sulfur-resistant methanation device 6 is a tubular isothermal reactor, a cobalt-molybdenum catalyst is arranged in the tube pass of the tubular isothermal reactor, and boiling water is 60-100 bar in the shell pass; the two ends of the tube pass are respectively connected with a secondary compression device 5 and a desulfurization and decarburization device 7. The shell pass is connected with a steam drum, and the shell pass, the steam drum, the tar recovery device 4 and the desulfurization and decarburization device 7 form a closed circulation loop of boiling water/saturated steam.
Sulphur-resistant methanation device 6 is connected with desulfurization decarbonization device 7, and desulfurization decarbonization device 7 is including filling desulfurizing tower and the decarbonization tower of MDEA solution, and the import and the sulphur-resistant methanation device 6 of decarbonization tower are connected, and the export is connected with the import and the dehydration adsorption tower 9 of desulfurizing tower, and the export and the hydrogen sulfide collection device 13 of desulfurizing tower are connected.
The hydrogen sulfide collecting device 13 is connected with a Claus sulfur recovery device 8, the desulfurization and decarburization device 7 is connected with a dehydration adsorption tower 9, the dehydration adsorption tower 9 is connected with a pressure swing adsorption device 10, and the pressure swing adsorption device 10 can select a pressure swing adsorption tower; the pressure swing adsorption device 10 is connected with a nitrogen collecting device 15 and a three-stage compression device 11, and the three-stage compression device 11 is connected with a CNG outlet pipe 16.
Screw compressor can be chooseed for use to one-level compressor arrangement 3, and piston compressor can be chooseed for use to second grade compressor arrangement 5, and centrifugal compressor can be chooseed for use to tertiary compressor arrangement 11.
The utility model discloses a system of well low temperature dry distillation raw coke oven gas through resistant sulphur samming methanation system CNG at the during operation:
the medium-low temperature dry distillation raw gas enters a deamination dust removal device 2 from a medium-low temperature dry distillation raw gas inlet pipe 1, ammonia gas is removed by washing, dust is removed by filtering, the gas enters a primary compression device 3, the gas is pressurized to 4-6bar and then enters a tar recovery device 4, components such as benzene, anthracene oil, tar and the like in the gas are recovered, and the content of benzene and tar in the recovered gas components is less than 5 ppm.
The residual gas enters a secondary compression device 5, the secondary compression device 5 pressurizes the gas to 26-30bar, liquefied petroleum gas components such as ethane, ethylene, propane, propylene, butane, butylene and the like are changed into liquid in the compression process, and the byproduct liquefied petroleum gas enters a liquefied petroleum gas collecting device 12.
And the residual gas enters a sulfur-tolerant methanation device 6, the sulfur-tolerant methanation device 6 adopts a tubular temperature-equalizing reactor, a catalyst is filled in a tube pass, boiling water of 60-100 bar flows away from a shell pass, and natural circulation of a steam drum and the reactor is formed through the density difference of the boiling water. The catalyst adopts cobalt-molybdenum catalyst, and is treated by H in raw material gas2S is reduced to generate active MoS at low airspeed2The water gas shift reaction and the methanation reaction can be simultaneously realized. As the hot spot temperature of the tubular temperature equalizing reactor is about 400 ℃, and the outlet temperature is 260-280 ℃, CO in the raw coke oven gas is basically and completely converted, and the selectivity of methane is over 85 percent. If the raw material gas is the raw gas of the traditional vertical furnace, the main components of the gas after the reaction of the sulfur-tolerant methanation device 6 are as follows: CH (CH)412-18% of CO, 0-0.3% of H23-6% of CO212-18% of N240-50% of H2O content of 6-12%, CnHm(ethane, ethylene, propane, propylene, butane, butylene) content is 0.5-5%, H2S content of 500-3000 ppm and NH3The content is 300-1200 ppm. If the raw gas is low-temperature dry distillation raw gas generated by external heating type vertical furnace, solid heat carrier low-temperature fast pyrolysis and pulverized coal rotary kiln pyrolysis, the main components of the gas after the reaction of the sulfur-resistant methanation device 6 are as follows: CH (CH)445-55% of CO, 0-0.3% of H23-6% of CO28-12% of N20 to 20% of H2O content of 6-24%, CnHm(ethane, ethylene, propane, propylene, butane, butylene) content is 0.5-6%, H2The S content is 500-3000 ppm. In addition, organic sulfur and SO in raw gas2Also converted to H by catalytic hydrogenation2And S. The by-product of 1.2 to 2.5 tons of pressure 6 can be obtained by methanation of each 1000 prescriptions of raw gas in a sulfur-tolerant methanation device 6The saturated steam of 0-100 bar can be used for solution heating and desorption of the desulfurization and decarburization device 7 and rectification or temperature swing adsorption of the tar recovery device 4, so that the optimal utilization of heat is realized.
The main reactions that occur during methanation are as follows:
CO+3H2→CH4+H2O ΔH298K＝-206KJ/mol R1
CO2+4H2→CH4+2H2O ΔH298K＝-165KJ/mol R2
CO+H2O→H2+CO2ΔH298K＝-41.2KJ/mol R3
according to the reaction formula, the reactions of R1 and R2 are strong exothermic reactions, the temperature rise of 72 ℃ is brought by every 1% of CO converted, and every 1% of CO converted2The temperature rise of 60 ℃ can be brought, the reaction activity is highest at about 300 ℃, the reaction rate equilibrium constant is smaller when the temperature is higher, and the reaction driving force is smaller. At present, the methanation process generally adopts a method of using a multi-section adiabatic reactor and gas circulation to dilute the content of CO in raw material gas, the first section of the adiabatic fixed bed methanation reactor usually reaches 620-650 ℃, the reactions of R1, R2 and R3 reach thermodynamic equilibrium at the temperature, and CO react2And CH4The content is controlled by thermodynamic equilibrium, the conversion rate of CO is lower, a plurality of adiabatic reactors are subsequently added to ensure the reaction depth, and finally the CO content is lower than 0.1%. And a tubular isothermal reactor is adopted, a tube pass is filled with a catalyst, a shell pass adopts boiling water for heat exchange to timely remove heat released by the reaction from the reactor, and medium-pressure steam is a byproduct. The tubular temperature equalizing reactor can control the reaction temperature to be 300-400 ℃, the R1 reaction equilibrium constant is large in the temperature range, and the high conversion rate of CO can be realized in a section of reactor after the reaction is continuously carried out.
After reaction, the reaction product enters a desulfurization and decarbonization device 7, and H is dissolved in MDEA (diethanolamine) solution under high pressure through physical dissolution and chemical absorption2S and CO2Dissolving or generating intermediate, decompressing and flashing in a decarbonizing tower to separate out high-purity CO2Then high-purity H is resolved by heating solution in a desulfurizing tower2And S. Desulfurization and decarburization device 7CO at the outlet2Absorption rate of about 95%, H2The removal rate of S is more than 99 percent.
High-purity H separated by the desulfurization and decarbonization device 72S enters a hydrogen sulfide collecting device 13 and then enters a Claus sulfur recovery device 8 to react to generate sulfur, and CO separated by a desulfurization and decarbonization device 72The residual gas in the desulfurization and decarbonization device 7 enters a carbon dioxide collecting device 14, the residual gas enters a dehydration adsorption tower 9 to remove moisture and then enters a pressure swing adsorption device 10, nitrogen separated by the pressure swing adsorption device 10 enters a nitrogen collecting device 15, the separated nitrogen contains a small amount of methane and L PG component gas which can be used as fuel gas to be supplied to a Claus sulfur recovery device 8 for combustion, the methane and L PG component gas enters a three-stage compression device 11, the three-stage compression device 11 pressurizes the gas to 265bar to obtain a compressed natural gas product, and CH in the natural gas4The content is more than 95 percent, and the balance is hydrogen and a trace L PG component.
It should be noted that the above description is only one of the embodiments of the present invention, and all equivalent changes made by the system described in the present invention are included in the protection scope of the present invention. The technical field of the present invention can be replaced by other embodiments described in a similar manner, without departing from the structure of the present invention or exceeding the scope defined by the claims, which belong to the protection scope of the present invention.
Claims (8)
1. A system for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation is characterized by comprising a deamination dust removal device (2), wherein an inlet of the deamination dust removal device (2) is connected with a medium-low temperature dry distillation raw gas inlet pipe (1), an outlet of the deamination dust removal device is connected with a primary compression device (3), the primary compression device (3) is connected with a tar recovery device (4), the tar recovery device (4) is connected with a secondary compression device (5), the secondary compression device (5) is connected with a sulfur-resistant methanation device (6) and a liquefied petroleum gas collection device (12), the sulfur-resistant methanation device (6) is connected with a desulfurization and decarbonization device (7), the desulfurization and decarbonization device (7) is connected with a dehydration adsorption tower (9), a carbon dioxide collection device (14) and a hydrogen sulfide collection device (13), and the hydrogen sulfide collection device (13), the dehydration adsorption tower (9) is connected with a pressure swing adsorption device (10), the pressure swing adsorption device (10) is connected with a nitrogen collecting device (15) and a three-stage compression device (11), and the three-stage compression device (11) is connected with a CNG outlet pipe (16).
2. The system for preparing CNG from medium and low temperature dry distillation raw coke oven gas through sulfur-tolerant temperature equalization methanation according to claim 1, wherein the first-stage compression device (3) is a screw compressor, the second-stage compression device (5) is a piston compressor, and the third-stage compression device (11) is a centrifugal compressor.
3. The system for preparing CNG from medium and low temperature dry distillation raw gas through sulfur-tolerant temperature equalization methanation according to claim 1, wherein the tar recovery device (4) is a rectifying tower or a temperature swing adsorption device.
4. The system for preparing CNG from medium-low temperature dry distillation raw coke oven gas through sulfur-tolerant temperature equalization methanation according to claim 1, wherein an oxygen removal device is arranged between the tar recovery device (4) and the secondary compression device (5).
5. The system for preparing CNG from the medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation according to claim 1, wherein the sulfur-resistant methanation device (6) is a tubular uniform-temperature reactor, a cobalt-molybdenum catalyst is arranged in a tube pass of the tubular uniform-temperature reactor, and boiling water is 60-100 bar in a shell pass; two ends of the tube pass are respectively connected with a secondary compression device (5) and a desulfurization and decarburization device (7).
6. The system for preparing CNG from low-medium-temperature dry distillation raw gas through sulfur-tolerant uniform-temperature methanation according to claim 5, wherein a shell pass is connected with a steam drum, and the shell pass, the steam drum, the tar recovery device (4) and the desulfurization and decarbonization device (7) form a closed circulation loop of boiling water/saturated steam.
7. The system for preparing CNG (compressed natural gas) through sulfur-tolerant uniform-temperature methanation of medium-low-temperature dry distillation raw gas according to claim 1, wherein the desulfurization and decarbonization device (7) comprises a desulfurization tower and a decarbonization tower which are filled with MDEA (methyl-dimethyl-ammonium-ether-ethyl) solution, an inlet of the decarbonization tower is connected with the sulfur-tolerant methanation device (6), an outlet of the decarbonization tower is connected with an inlet of the desulfurization tower and the dehydration adsorption tower (9), and an outlet of the desulfurization tower is connected with the hydrogen sulfide collection device (13).
8. The system for preparing CNG from medium and low temperature dry distillation raw coke oven gas through sulfur-tolerant temperature equalization methanation according to claim 1, wherein the pressure swing adsorption device (10) is a pressure swing adsorption tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921836184.XU CN211005244U (en) | 2019-10-29 | 2019-10-29 | System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921836184.XU CN211005244U (en) | 2019-10-29 | 2019-10-29 | System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211005244U true CN211005244U (en) | 2020-07-14 |
Family
ID=71499896
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921836184.XU Active CN211005244U (en) | 2019-10-29 | 2019-10-29 | System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211005244U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110655940A (en) * | 2019-10-29 | 2020-01-07 | 中国华能集团有限公司 | System and method for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform temperature methanation |
-
2019
- 2019-10-29 CN CN201921836184.XU patent/CN211005244U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110655940A (en) * | 2019-10-29 | 2020-01-07 | 中国华能集团有限公司 | System and method for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform temperature methanation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101245262B (en) | Gas-steam combined cycle system and technique based on coal gasification and methanation | |
| CN104232195B (en) | Method for jointly producing methanol and synthetic natural gas by utilizing coke oven gas | |
| CN107758617B (en) | Method for producing hydrogen by using biogas biomass | |
| CN101649233B (en) | Isothermal methanation process and device for the preparation of synthetic natural gas | |
| CN102585951B (en) | Process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas | |
| CN101575540B (en) | Method for producing liquefied natural gas and carbinol simultaneously | |
| CN101705128A (en) | Adiabatic methanation process and device for preparing synthetic natural gas | |
| CN103407963A (en) | Coke oven gas hydrogen generation process | |
| CN102899112B (en) | Method and device for producing synthetic natural gas | |
| CN102942972A (en) | Method for producing liquefied natural gas by coke oven gas | |
| CN102876411B (en) | Method and device for producing synthetic natural gas | |
| CN102732347A (en) | Adjustable process for co-producing liquefied natural gas and hydrogen by coke furnace gas | |
| CN217459345U (en) | Device for producing low-carbon methanol by using coke oven gas | |
| CN114149837B (en) | Process for preparing liquefied natural gas and co-producing liquid ammonia or hydrogen by coke oven gas with conversion decarburization | |
| CN110655939A (en) | System and method for preparing LNG (liquefied Natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation | |
| CN102746870B (en) | FT synthesis technology | |
| CN211005244U (en) | System for preparing CNG (compressed natural gas) from medium-low temperature dry distillation raw gas through sulfur-resistant uniform-temperature methanation | |
| Jiang et al. | Energy optimization of ammonia synthesis processes based on oxygen purity under different purification technologies | |
| CN210885949U (en) | System for preparing LNG (liquefied Natural gas) by sulfur-resistant uniform-temperature methanation of medium-low-temperature dry distillation raw gas | |
| CN102676251A (en) | Process for preparing methane by utilizing coke oven gas | |
| CN109456139B (en) | Oil absorption separation method for reaction product of preparing ethylene from methane | |
| CN201525833U (en) | Insulated methanation assembly for producing synthetic natural gas | |
| CN201436296U (en) | Isothermal methanation device for preparing synthesized natural gas | |
| CN103013598B (en) | Method and device for producing synthesized natural gas | |
| CN203582821U (en) | Movable coal-made synthesis gas methanation catalyst test platform |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |