CN112725047A - Coal tar distillate hydrogenation modification and LNG preparation co-production process for comprehensive utilization of coke oven gas - Google Patents
Coal tar distillate hydrogenation modification and LNG preparation co-production process for comprehensive utilization of coke oven gas Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/20—Refining by chemical means inorganic or organic compounds
- C10C1/205—Refining by chemical means inorganic or organic compounds refining in the presence of hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
Abstract
The invention discloses a coal tar distillate hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas, which comprises a hydro-upgrading system and an LNG preparation system which can run jointly or respectively and independently, wherein the hydro-upgrading system and the LNG preparation system share a set of pretreatment and continuous pressure boosting system, and the joint operation process of the hydro-upgrading system and the LNG preparation system comprises the following steps: a1, processing the coke oven gas by one-time raw materials and continuously boosting pressure; a2, pre-hydrogenation of coke oven gas, and sulfur-tolerant shift; a3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system; a4, methanation treatment; a5, PSA pressure swing adsorption dehydrogenation to prepare product hydrogen; a6, compressing and purifying the residual product; and A7, liquefying to prepare the LNG product. The coal tar distillate hydro-upgrading and LNG preparation co-production process for comprehensively utilizing the coke oven gas has the advantages of reasonable investment, low operation cost, maximized resource utilization and safe system operation.
Description
Technical Field
The invention relates to the technical field of coal tar distillate hydro-upgrading by taking coke oven gas as a raw material, in particular to a coal tar distillate hydro-upgrading and LNG (liquefied natural gas) preparation co-production process for comprehensively utilizing coke oven gas.
Background
With the implementation of the national energy strategy, the technologies for preparing LNG by comprehensively utilizing coke oven gas and preparing light fuel oil by hydro-upgrading coal tar fractions taking the coke oven gas as raw materials are mature and industrialized, the wide application of the technologies also enables the deep processing of downstream byproducts in the coking industry to be more perfect, and the comprehensive utilization rate of coal is improved.
The existing high-temperature coal tar distillate hydro-upgrading and low-temperature coal tar distillate hydro-upgrading processes which take coke oven gas as a raw material mainly extract hydrogen in the coke oven gas as the raw material, and meanwhile, the abundant gas is sent out of a boundary area to be processed or utilized.
The main components of the coke oven gas are H, CO2, CH4 and CnHm, and the impurity components comprise hydrogen sulfide, organic sulfide, benzene, naphthalene, cyanide and the like.
The method for extracting hydrogen in the coke oven gas as the raw material comprises two main methods of pressure swing adsorption and membrane separation, and the general process flow is as follows: the coke oven gas enters a temperature and pressure swing adsorption unit after primary compression to remove benzene and naphthalene in the coke oven gas, then continuously increases the pressure and enters a separation unit to obtain product hydrogen, and the separation unit can select pressure swing adsorption or membrane separation technology.
It can be seen from the above flow that hydrogen is inevitably rich in the high-temperature coal tar fraction hydro-upgrading and low-temperature coal tar fraction hydro-upgrading processes using coke oven gas as a raw material, and the part of the gas is usually sent out of a junior region to be used as fuel or reprocessed for utilization.
If the rich gas is used as the raw material for preparing LNG, substances such as CO2, CnHm, organic sulfur and the like must be separated again, and the process needs a longer flow path to realize the process.
In summary, the high-temperature coal tar distillate hydro-upgrading and low-temperature coal tar distillate hydro-upgrading processes using coke oven gas as the raw material have defects in comprehensive utilization of coke oven gas, mainly reflect that there is no integrated solution for utilization of abundant gas, and simultaneously, reasonable and maximum resource utilization cannot be achieved under the conditions of increasing and decreasing hydrogen demand due to changes in raw material gas quantity and production load.
Disclosure of Invention
Aiming at the problems, the invention provides a coproduction process for the hydro-upgrading of coal tar distillate and the preparation of LNG by comprehensively utilizing coke oven gas, and the process has the advantages of reasonable investment, low operation cost, maximized resource utilization and safe system operation.
The technical scheme of the invention is as follows:
a coal tar fraction hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas comprises a hydro-upgrading system and an LNG preparation system which can run in a combined mode or independently, wherein the hydro-upgrading system and the LNG preparation system share a set of pretreatment and continuous pressure boosting system.
In a further technical scheme, when the hydro-upgrading system and the LNG preparation system are operated in a combined mode, the method comprises the following steps:
a1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
a2, pre-hydrogenation of coke oven gas, and sulfur-tolerant shift;
a3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
a4, methanation treatment;
a5, PSA pressure swing adsorption dehydrogenation to prepare product hydrogen;
a6, compressing and purifying the residual product;
and A7, liquefying to prepare the LNG product.
In a further technical scheme, in the step A3, the deacidification of the coke oven gas comprises desulfurization and MDEA (N-methyldiethanolamine) decarburization.
In a further technical scheme, the hydro-upgrading system independently operates and comprises the following steps:
b1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
b2, pre-hydrogenation of coke oven gas;
b3, PSA pressure swing adsorption dehydrogenation to prepare the product hydrogen.
In a further technical scheme, the LNG preparation system comprises the following steps when operating alone:
c1, one-time raw material treatment and continuous pressure increase of coke oven gas;
c2, pre-hydrogenation of coke oven gas;
c3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
c4, methanation treatment;
c5, PSA pressure swing adsorption dehydrogenation, and sending out rich hydrogen;
c6, compressing and purifying the residual product;
and C7, liquefying to prepare the LNG product.
In a further technical scheme, in the step C2, the deacidification of the coke oven gas is hydrodesulfurization.
In a further technical scheme, in the step A7 and the step C7, hydrogen separated in the process of preparing the LNG product by liquefaction is respectively returned to the step A2 and the step C2 for pre-hydrogenation, so that the hydrogen is fully utilized.
In a further technical scheme, in the step A1, the step B1 and the step C1, the method for processing the coke oven gas disposable raw materials and continuously boosting the pressure is as follows:
after primary pressure increase, the raw material coke oven gas enters a TSA temperature and pressure swing adsorption unit to remove benzene and naphthalene impurities, and then pressure increase is continued to prepare for pre-hydrogenation.
The working principle of the technical scheme is as follows:
the method comprises the steps that coke oven gas is subjected to one-step raw material treatment and continuous pressure boosting to realize coal tar distillate hydro-upgrading and LNG (liquefied natural gas) preparation co-production, only one set of pretreatment and continuous pressure boosting is needed to meet the requirements of coal tar distillate hydro-upgrading and LNG preparation co-production, a hydro-upgrading system and an LNG preparation system can run in a combined mode or independently respectively, coke oven gas is subjected to pre-hydrogenation, extra hydrogen is obtained from coke oven gas through a conversion process (complete conversion or partial conversion), wherein the limit of partial conversion is 0, more hydrogen is obtained through the conversion process (complete conversion or partial conversion) according to the change of raw material components and flow, and the conversion range is 0-99.9%; the carbon-hydrogen balance of the whole process system is realized by the coke oven gas through the deacidification process.
The invention has the beneficial effects that:
1. only one set of pretreatment and continuous pressure boosting are needed to meet the requirements of coal tar distillate hydrogenation modification and LNG preparation co-production, the operation cost is lower, and the resource utilization maximization is realized;
2. the hydro-upgrading system and the LNG preparation system can be operated in a combined mode or independently, so that the operation process is safer;
3. the pre-hydrogenation unit is arranged in front, so that the system can meet the process requirements no matter the system operates in a combined mode or independently and respectively, and the safe operation of the system is ensured;
4. the coke oven gas comprehensively utilizes the coal tar distillate hydrogenation modification and the conversion or partial conversion of the LNG preparation co-production process, can meet the joint operation in a normal design state, can also meet the requirements of higher coal tar distillate hydrogenation modification independent operation or joint operation under the working condition of coke oven gas quantity reduction, and can also meet the joint operation under the working condition of coal tar distillate hydrogenation modification load reduction under the normal state of coke oven gas;
5. the coke oven gas comprehensively utilizes the coal tar distillate hydrogenation modification and deacidification or partial deacidification of the LNG preparation co-production process, can meet the joint operation of a normal design state by combining transformation (partial transformation) through full deacidification or partial deacidification, meets the requirements of the coal tar distillate hydrogenation modification independent operation or the joint operation under the working condition of reducing the coke oven gas quantity, and meets the joint operation under the working condition of reducing the load of the coal tar distillate hydrogenation modification of the coke oven gas normal state.
Drawings
FIG. 1 is a prior art hydrogen extraction flow diagram for coke oven gas;
FIG. 2 is a flow diagram of a combined operation of a hydro-upgrading system and an LNG production system according to an embodiment of the present invention;
FIG. 3 is a flow diagram of a hydro-upgrading system in accordance with an embodiment of the invention when operating alone;
fig. 4 is a flow diagram illustrating the operation of an LNG production system in accordance with an embodiment of the present invention when operating alone.
Detailed Description
The embodiments of the present invention will be further described with reference to the accompanying drawings.
Example (b):
a coal tar fraction hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas comprises a hydro-upgrading system and an LNG preparation system which can run in a combined mode or independently, wherein the hydro-upgrading system and the LNG preparation system share a set of pretreatment and continuous pressure boosting system.
In another embodiment, as shown in fig. 2, the hydro-upgrading system and the LNG production system are operated in combination, comprising the steps of:
a1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
a2, pre-hydrogenation of coke oven gas, and sulfur-tolerant shift;
a3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
a4, methanation treatment;
a5, PSA pressure swing adsorption dehydrogenation to prepare product hydrogen;
a6, compressing and purifying the residual product;
and A7, liquefying to prepare the LNG product.
In another embodiment, step a3, the coke oven gas deacidification includes desulfurization and MDEA (N-methyldiethanolamine) decarbonization.
In another embodiment, as shown in FIG. 3, the hydro-upgrading system, when operated alone, comprises the steps of:
b1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
b2, pre-hydrogenation of coke oven gas;
b3, PSA pressure swing adsorption dehydrogenation to prepare the product hydrogen.
In another embodiment, as shown in fig. 4, the LNG production system, when operating alone, comprises the steps of:
c1, one-time raw material treatment and continuous pressure increase of coke oven gas;
c2, pre-hydrogenation of coke oven gas;
c3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
c4, methanation treatment;
c5, PSA pressure swing adsorption dehydrogenation, and sending out rich hydrogen;
c6, compressing and purifying the residual product;
and C7, liquefying to prepare the LNG product.
In another embodiment, in step C2, the coke oven gas is deacidified as hydrodesulfurized.
In another embodiment, in step a7 and step C7, the hydrogen separated from the liquefaction process for producing LNG as a product is returned to step a2 and step C2, respectively, for pre-hydrogenation to achieve full utilization of hydrogen.
In another embodiment, the method for processing the coke oven gas disposable raw material and continuously boosting the pressure in the steps A1, B1 and C1 is as follows:
after primary pressure increase, the raw material coke oven gas enters a TSA temperature and pressure swing adsorption unit to remove benzene and naphthalene impurities, and then pressure increase is continued to prepare for pre-hydrogenation.
The working principle of the technical scheme is as follows:
the method comprises the steps that coke oven gas is subjected to one-step raw material treatment and continuous pressure boosting to realize coal tar distillate hydro-upgrading and LNG (liquefied natural gas) preparation co-production, only one set of pretreatment and continuous pressure boosting is needed to meet the requirements of coal tar distillate hydro-upgrading and LNG preparation co-production, a hydro-upgrading system and an LNG preparation system can run in a combined mode or independently respectively, coke oven gas is subjected to pre-hydrogenation, extra hydrogen is obtained from coke oven gas through a conversion process (complete conversion or partial conversion), wherein the limit of partial conversion is 0, more hydrogen is obtained through the conversion process (complete conversion or partial conversion) according to the change of raw material components and flow, and the conversion range is 0-99.9%; the carbon-hydrogen balance of the whole process system is realized by the coke oven gas through the deacidification process.
Comparative example 1:
by applying the process provided by the embodiment, the project of carrying out hydro-upgrading refining on the high-temperature coal tar distillate of 15 ten thousand tons per year to co-produce LNG is developed, wherein the gas amount of the coke oven gas is 34500Nm 3/h.
The coke oven gas comprises the following components:
the other impurities were as follows:
| composition (I) | Tar oil | Naphthalene | Benzene and its derivatives | NH3 | HCN | Thiophene(s) |
| mg/Nm3 | ≤30 | ≤300 | ≤5000 | ≤50 | -- | Micro-scale |
The full load hydrogen amount of a coke oven gas hydrogen stripping unit of the high-temperature coal tar distillate hydro-upgrading refining device is 17000Nm3And h, the independent operation load range of the high-temperature coal tar distillate hydro-upgrading refining device is 30-100%.
Hydrogenation modification refining device for high-temperature coal tar distillate and preparation LNG combined process for supplying 17000Nm maximum hydrogen amount to hydrogenation modification refining device for high-temperature coal tar distillate3Matched LNG capacity of 25 x 104Nm3And d. The minimum hydrogen supply amount of the combined process to the high-temperature coal tar distillate hydro-upgrading refining device is 10000Nm3Matching LNG capacity of 31 x 104Nm3/d。
The maximum load of the independent operation of preparing LNG by coke oven gas is 34 multiplied by 104Nm3/d。
Joint transform unit transform rate range: 25 to 85 percent.
Relative CO of deacidification unit of combined plant2Range of removal rate: 0 to 100 percent.
Comparative example 2:
by applying the process provided by the embodiment, the process is developed in 12 ten thousand tons per year,The high-temperature coal tar distillate is subjected to hydro-upgrading and refining to produce a project for coproducing LNG, wherein the gas amount of coke oven gas is 40000Nm3/h。
The coke oven gas comprises the following components:
the other impurities were as follows:
| composition (I) | Tar oil | Naphthalene | Benzene and its derivatives | NH3 | HCN | Thiophene(s) |
| mg/Nm3 | ≤80 | ≤400 | ≤5000 | ≤150 | ≤300 | Micro-scale |
Full-load hydrogen flow of coke oven gas hydrogen stripping unit of high-temperature coal tar distillate hydro-upgrading refining device65000Nm3And h, the independent operation load range of the high-temperature coal tar distillate hydro-upgrading refining device is 30-100%.
High-temperature coal tar distillate hydro-upgrading refining device and LNG preparation combined process for supplying maximum hydrogen amount to high-temperature coal tar distillate hydro-upgrading refining device to 11000Nm3Matching LNG capacity of 33.5 x 104Nm3The lowest hydrogen supply amount of the combined process to the high-temperature coal tar distillate hydrogenation modification refining device is 6500Nm3Matching LNG capacity of 40 x 104Nm3/d。
The maximum load of the independent operation of preparing LNG by coke oven gas is 40 multiplied by 104Nm3/d。
Joint transform unit transform rate range: 20 to 45 percent.
Relative CO of deacidification unit of combined plant2Range of removal rate: 0 to 100 percent.
The above-mentioned embodiments only express the specific embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention.
Claims (8)
1. A coal tar fraction hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas is characterized by comprising a hydro-upgrading system and an LNG preparation system which can run jointly or independently respectively, wherein the hydro-upgrading system and the LNG preparation system share a set of pretreatment and continuous pressure boosting system.
2. The coal tar distillate hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas according to claim 1, characterized in that when the hydro-upgrading system and the LNG preparation system are operated in a combined manner, the process comprises the following steps:
a1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
a2, pre-hydrogenation of coke oven gas, and sulfur-tolerant shift;
a3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
a4, methanation treatment;
a5, PSA pressure swing adsorption dehydrogenation to prepare product hydrogen;
a6, compressing and purifying the residual product;
and A7, liquefying to prepare the LNG product.
3. The coproduction process for the hydro-upgrading of the coal tar distillate and the preparation of LNG from the coke oven gas by comprehensive utilization of the coke oven gas as claimed in claim 2, wherein in the step A3, the deacidification of the coke oven gas comprises desulfurization and MDEA decarburization.
4. The coal tar distillate hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas according to claim 2, characterized in that a hydro-upgrading system is separately operated and comprises the following steps:
b1, processing the coke oven gas by one-time raw materials and continuously boosting pressure;
b2, pre-hydrogenation of coke oven gas;
b3, PSA pressure swing adsorption dehydrogenation to prepare the product hydrogen.
5. The coal tar distillate hydro-upgrading and LNG preparation co-production process for comprehensively utilizing coke oven gas according to claim 4, characterized in that an LNG preparation system is independently operated and comprises the following steps:
c1, one-time raw material treatment and continuous pressure increase of coke oven gas;
c2, pre-hydrogenation of coke oven gas;
c3, deacidifying the coke oven gas to balance the carbon and hydrogen of the whole process system;
c4, methanation treatment;
c5, PSA pressure swing adsorption dehydrogenation, and sending out rich hydrogen;
c6, compressing and purifying the residual product;
and C7, liquefying to prepare the LNG product.
6. The coproduction process for the hydro-upgrading of the coal tar distillate and the preparation of LNG by the comprehensive utilization of the coke oven gas as claimed in claim 5, wherein in the step C2, the deacidification of the coke oven gas is hydrodesulfurization.
7. The coal tar distillate hydro-upgrading and LNG preparation co-production process comprehensively utilizing coke oven gas as claimed in claim 5, wherein in the step A7 and the step C7, hydrogen separated in the process of liquefying to prepare the product LNG is returned to the step A2 and the step C2 respectively for pre-hydrogenation.
8. The coproduction process for the hydro-upgrading of coke oven gas by comprehensively utilizing coal tar distillate and the preparation of LNG as claimed in claim 5, wherein in the step A1, the step B1 and the step C1, the method for one-time raw material treatment and continuous pressure rise of coke oven gas is as follows:
after primary pressure increase, the raw material coke oven gas enters a TSA temperature and pressure swing adsorption unit to remove benzene and naphthalene impurities, and then pressure increase is continued to prepare for pre-hydrogenation.
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| CN104707453A (en) * | 2015-03-26 | 2015-06-17 | 山西省国新能源发展集团有限公司 | Two-stage catalytic hydrodesulfurization device |
| CN104946327A (en) * | 2015-06-04 | 2015-09-30 | 成都同创伟业新能源科技有限公司 | Coal gas utilization method realized by coal-tar fraction hydro-upgrading and LNG manufacturing combination |
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