CN102079999A - Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material - Google Patents
Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material Download PDFInfo
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Abstract
The invention discloses a method for producing liquefied natural gas and synthetic gas by taking coke oven gas as a raw material, which mainly comprises the steps of: removing naphthalene, benzene and tar of coke oven gas, decarburizing by MDEA (Activated Methyl Diethanol Amine), enriching methane by pressure swing adsorption to separate out synthetic gas and preparing a liquefied natural gas product by the enriched methane. The liquefied natural gas is obtained by the steps of pretreatment of coke oven gas, decarburization by MDEA, efficient separation of H2, N2, CO and methane by a pressure swing adsorption technology, separation of synthetic gas at top of the tower and liquefaction of the enriched methane. The invention has the advantages of short technical flow, small investment and good economic benefits.
Description
Technical field
The invention discloses a kind of is the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, belongs to the comprehensive utilization applied technical field of coke-oven gas.
Background technology
The China's natural gas demand continues to increase in recent years.Natural gas liquids has the characteristic of exchanging fully with pipeline gas, and has the advantages that calorific value is big, performance is high, make things convenient for accumulating, has demonstrated good market outlook.The source of the gas that can either increase natural gas liquids by the coke-oven gas preparing liquefied natural gas can improve the economic benefit of coking plant again, reduces the carbon emission amount, the protection environment.
There are following different operational path in coke-oven gas preparing liquefied natural gas or compressed natural gas.
Patent CN 100506956C low-temperature rectisol and NHD desulfurization, decarburization, transformation adsorption and enrichment CO, weak adsorbed gas transformation fractionation by adsorption lower carbon number hydrocarbons, lower carbon number hydrocarbons liquefaction, weak adsorbed gas separating hydrogen gas and nitrogen.
Compressed low-temperature rectisol of patent CN 100543118C coke-oven gas and NHD desulfurization, decarburization, transformation adsorption and enrichment CO, the liquefaction of gases that is not adsorbed obtains natural gas liquids.
Use transformation adsorption and enrichment hydrogen among the patent CN 100453626C after the compressed desulfurization of coke-oven gas, separate the gassing second-compressed, separating propane and CO
2, condensation separation nitrogen, CO and methane once more.
Patent CN 101434879A coke-oven gas adds through purifying treatment, conversion process, desulfurization and decarburization, pressure swing adsorption/separation of methane and hydrogen, high methane gas and is pressed into compressed natural gas.
Patent CN 101575540A coke-oven gas is to the coke-oven gas pre-treatment, transformation fractionation by adsorption hydrogen and be rich in the gas of methane, compression then, dry method depickling, wet method depickling, dehydration, purifying, liquefaction acquisition natural gas liquids and be rich in the gas of CO.
There is long flow path in current coke-oven gas preparing liquefied natural gas or the Compressed Natural Gas Technology, the shortcoming that energy consumption is high, the gas that particularly enters liquefaction has a large amount of non-condensable gases, has increased the energy consumption of liquefaction by a larger margin:
(1) the available technology adopting methanation is to the CO in the coke-oven gas
2, CO transforms, and carries out methane-rich liquefaction then, this is not quite reasonable technically and economically;
(2) in the prior art with coke-oven gas compression cooling, enter the heat exchanger package heat-shift, enter separation column and obtain natural gas liquids, this technology component is not carried out isolating energy consumption height;
(3) in the existing technology, adopt the pressure swing adsorption enrich methane, changing device is adopted in the front, is target in the methane-rich unit with the enriched hydrogen, and inert component enters liquefaction unit.
Summary of the invention
The object of the present invention is to provide above-mentioned deficiency of the prior art, providing a kind of is the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, and this method can be extracted liquid methane efficiently and obtain synthetic gas from coke-oven gas.
In order to realize the foregoing invention purpose, the present invention has adopted following technical scheme:
A kind of is the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, may further comprise the steps:
(1) pre-treatment:
Coke-oven gas is carried out pre-treatment, remove wherein benzene, naphthalene, tar, C
5Above heavy constituent obtain raw gas;
(2) MDEA decarburization:
Step (1) gained raw gas is fed the bottom, absorption tower, the CO in MDEA decarburization absorption raw gas
2, purified gas enters psa unit by the top, absorption tower after gas-liquid separator is discharged, and rich solution (is rich in CO
2Absorption liquid) after poor-rich solution interchanger heat exchange, separate separation of C O to regenerator column regeneration by amine liquid pump pump
2After lean solution tell the back at the bottom of the Tata by regeneration and return the absorption tower by water cooler regeneration, by the CO of pure degree ≧ 99% of regenerator column removed overhead
2After the cooling gas-liquid separation, enter other unit or directly discharging;
(3) transformation adsorption and enrichment methane:
With step (2) gained purified gas with send into one or more levels pressure-swing absorption apparatus after the unitary non-condensable gas of natural gas liquefaction mixes, by transformation absorption with the H in the purified gas
2, N
2, CO separates with methane, collects the cat head component and obtains synthetic gas, the methane of enrichment enters liquefaction unit,
The step of described transformation absorption is: absorption, and all pressure drops along putting, are replaced, and contrary putting vacuumizes, and boosts all voltage rises, final rise along venting; Perhaps absorption, all pressure drops, along putting, contrary putting boosted along venting, all voltage rises, final rise;
The absorption of described transformation is sorbent used be in aluminum oxide, silica gel, gac or the molecular sieve any two or more, the quantity of every grade of adsorption tower is 4～20;
(4) liquefaction:
The methane gas of step (3) enrichment is compressed to 0.8～6.0MPa, cools to bottom or the top of sending into TSA molecular sieve bed behind the normal temperature, concentrate methane gas at the bottom of the tower or cat head enter bed and dehydrate, the methane dew point stops absorption after reaching set(ting)value, use dry gas that bed is carried out equipressure or step-down regeneration, the regeneration back uses dry gas that bed layer pressure slowly is raised to adsorptive pressure, adsorptive pressure is 0.8～6.0MPa, and the resurgent gases temperature is 150～300 ℃;
Above-mentioned exsiccant methane rich is sent into ice chest liquefaction, obtain natural gas liquids, non-condensable gas is sent into the unitary inlet of transformation adsorption and enrichment methane.
Above-mentioned is in the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, and step (1) pre-treatment removes benzene, naphthalene, tar, the C in the coke-oven gas
5The concrete grammar of above heavy constituent can for: coke-oven gas is compressed to 0.1 MPa～4.0MPa, is cooled to 10 ℃～60 ℃, remove components such as part naphthalene, tar, benzene, the coke-oven gas process purifying treatment after lowering the temperature be will compress then, wherein benzene, naphthalene, tar, C removed
5Above heavy constituent obtain raw gas;
Perhaps coke-oven gas removes wherein benzene, naphthalene, tar, C through purifying treatment
5Above heavy constituent obtain raw gas, are compressed to 0.1～4.0MPa then and cool to 10～60 ℃ and enter the MDEA decarburization.
Above-mentioned is in the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, the method that coke oven gas purification is handled in the step (1) can adopt alternating temperature adsorption method (TSA) to carry out purifying treatment, when adopting TSA to carry out purifying treatment, TSA is one-level or secondary, the adsorption tower of each grade is 2～8, each level all has a tower to be in the heating and cooling state simultaneously, the bed sorbent material is wherein any two kinds or two or more of coke, gac, aluminum oxide, silica gel, and the bed regeneration temperature is 150～300 ℃.
The invention discloses a kind of is the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, and coke-oven gas is carried out pre-treatment and obtains raw gas taking off naphthalene, benzene and tar unit, removes the CO in the thick coke-oven gas then through MDEA decarburization unit
2, by transformation adsorption and enrichment methane unit methane component and other component are cut, the H in the purified gas
2, N
2, CO effectively separates with methane, the cat head component enters other unit as synthetic gas, the methane of enrichment enters liquefaction unit liquefaction and makes liquefied natural gas product.Provided by the invention is in the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, owing to adsorb the H in the purified gas by transformation
2, N
2, CO carried out effectively separating with methane, significantly reduced the inert component in the methane gas of enrichment, alleviated the load of liquefaction unit, and saved changing device, greatly saved the energy.
Compare with existing technology, advantage of the present invention is:Because significantly having reduced inert component alleviates the load of liquefaction unit, and has saved changing device, has greatly saved the energy.
Processing method of the present invention is that each component in the coke-oven gas is carried out the classification utilization, and in transformation adsorbed methane enrichment unit, the reasonable combination arrangement by to sorbent material separates methane with synthesis gas components.The methanation of employing is arranged to the CO in the coke-oven gas in the prior art
2, CO transforms, and carries out methane-rich liquefaction then, this is not quite reasonable technically and economically.
With with coke-oven gas compression cooling, enter the heat exchanger package heat-shift, enter the prior art that separation column obtains natural gas liquids and compare, the energy consumption of this technology is 1.0KWh/m
3(methane), and present technique energy consumption be 0.50KWh/m
3(methane) (comprising compression, dehydration), energy consumption reduces significantly.
In aforementioned existing technology, adopt the pressure swing adsorption enrich methane, then changing device is adopted in the front, is target in the methane-rich unit with the enriched hydrogen, and inert component enters liquefaction unit.Compare with this technology, this patent has been saved changing device, and with the part of the CO in the coke-oven gas as synthetic gas, has improved economic benefit.
After method of the present invention goes out methane separation, adopt transformation absorption to carry hydrogen and handle synthetic gas, investment will reduce about 50%.
Method of the present invention is in liquefaction unit, and the non-condensable gas of liquefaction unit returns the unitary inlet of transformation adsorbed methane enrichment, has improved the organic efficiency of methane.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Embodiment
The present invention is described in further detail below in conjunction with testing example and embodiment.But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment, allly all belong to scope of the present invention based on the technology that content of the present invention realized.
Embodiment 1
Present embodiment carries out pre-treatment with coke-oven gas through taking off naphthalene, benzene and tar unit, removes the CO in the thick coke-oven gas then through MDEA decarburization unit
2, with methane component and the cutting of other component, the cat head component is as synthetic gas by transformation adsorption and enrichment methane unit, and the last liquefaction of enrich methane gas makes liquefied natural gas product.The concrete treatment process of its each step is as follows:
(1) benzene, naphthalene, tar are taken off in pre-treatment
Coke-oven gas is compressed to 650KPa by spiral-lobe compressor, and cools to 40 ℃ of naphthalene, tar, benzene, C that remove wherein
5Above heavy constituent.
Wherein extraneous next coke-oven gas tolerance is 45657.3Nm
3/ h, pressure are 100KPa, and temperature is 40 ℃, form (vol%): H
257.0, O
20.6, N
25.0, CO 9.0, CO
22.0, H
2O 2.4, CH
423, C
23.0, hydrogen sulfide, naphthalene, benzene, tar, C
5More than reorganization grades a small amount of.
Coke-oven gas after the compression cooling removes wherein benzene, naphthalene, tar, C through purifying treatment
5Above heavy constituent obtain raw gas.The raw gas that obtains adopts TSA to carry out purifying treatment, and TSA comprises 3 attached towers of suction.
Coke-oven gas by compression cooling enters TSA bed, naphthalene in coke-oven gas, tar, benzene, C from the bed bottom at 650KPa under 40 ℃ of conditions
5Above heavy constituent are adsorbed successively, reach the requirement of MDEA decarburization.Its concrete treatment process is: coke-oven gas is entering the TSA adsorption bed from the bed bottom, it is adsorbed that strong absorbed component such as the naphthalene in the coke-oven gas, tar, benzene is adsorbed agent successively, weak absorbed component is sent through the adsorption bed top, after the impurity in the coke-oven gas reaches normality, stop absorption, bed layer pressure is dropped to normal pressure.Use the resurgent gases that is heated to 240 ℃ that bed is heated up then, at the bottom of tower, discharge bed with resurgent gases behind the strong absorbed component heated volatile in the bed and make bed obtain regeneration.Heater heats is gone as resurgent gases in the regeneration back after taking away the bed waste heat through the coke-oven gas cooling bed that purifies.Boost after bed drops to 40 ℃ and wait for use when next time adsorbing.Resurgent gases is after cooling, gas-liquid separation, and gas can be sent into torch burning and handle or enter the fuel pipe network, and liquid and solid can be as fuel or further refining naphthalene, the benzene etc. of obtaining.The bed sorbent material is gac, aluminum oxide, silica gel, and volume ratio is 5:30:65.
⑵ MDEA decarburization
Above-mentioned raw gas is fed the bottom, absorption tower, use the CO in the MDEA absorption liquid absorption raw gas
2, purified gas is discharged through gas-liquid separator by the top, absorption tower and is entered psa unit, and rich solution is through poor-rich solution interchanger, the amine liquid pump, regenerator column, absorption tower, the CO that removes are returned in water cooler regeneration
2Give other unit or directly discharging.CO
2Chun Du ≧ 99%.
The service temperature of coke-oven gas is 630KPa, 40 ℃, absorb through MDEA, and gaseous fraction becomes: H
257.715, O
20.608, N
25.063, CO 9.113, CO
20, H
2O 1.175, CH
423.289, C
23.038.
⑶ transformation adsorption and enrichment methane
Adopt the absorption of one-level transformation, with the entering methane from transformation absorption from the adsorption bed bottom and concentrate bed of the non-condensable gas of the mixed liquefied natural gas liquefaction of above-mentioned purified gas, strong absorbed component such as methane is adsorbed, and synthetic gas goes to other unit by cat head.
After methane concentration in the cat head synthetic gas reaches 1.7% (vol), by four equal pressure drops adsorption column pressure is dropped to 133KPa, reclaim effective constituent, improve the bed methane concentration, all press the back to adjust the bed methane concentration, and pressure is dropped to 100KPa, enter surge tank along venting along putting.Along after putting end, use the enrich methane gas after compressing under 100KPa, bed to be replaced.Bed methane purity reaches that step-down is contrary at the bottom of by tower puts and remove compressor through vacuum pump greater than the strong absorbed component in 80% (vol) back, and pressure is raised to 5.5MPa.After emitting product gas, use bed being boosted of transformation adsorption and enrichment methane along venting.Bed regeneration back boost pressure, and use the cat head synthetic gas that pressure is raised to adsorptive pressure, wait for and using again when adsorbing next time.Displacement gas returns the coke-oven gas suction port of compressor.
The working pressure of coke-oven gas is 600KPa, 40 ℃ of service temperatures, and through transformation adsorption and enrichment methane, the gaseous fraction of the synthetic gas that cat head comes out becomes: H
278.868, O
20.824, N
26.742, CO 11.864, CO
20, CH
41.7, C
20.002.
Adopt 10 adsorption towers in the transformation adsorbed methane enrichment system, wherein two towers absorption is all pressed, is used to vacuumize the back adsorption tower along venting and boosts for four time.The volume ratio aluminum oxide of sorbent material filling: gac: molecular sieve 5:80:15.
⑷ liquefaction
With the top of above-mentioned 5500KPa high methane gas feeding TSA molecular sieve bed, high methane gas enters the bed dehydration from cat head, and water etc. contain strong absorbed component and are adsorbed, and weak absorbed component such as methane enters ice chest liquefaction.Stop absorption after the dew point of methane rich reaches-75 ℃, bed layer pressure drops to 1600KPa then, uses dry gas to be warmed up to 240 ℃ bed is regenerated.The regeneration back uses dry gas that bed temperature is dropped to 40 ℃, and the bed that heats up is removed in the resurgent gases heating.Use dry gas that bed layer pressure slowly is raised to adsorptive pressure then.
Three tower dryings, tower absorption, a tower heats up, tower cooling, intensification and cooling are continuously.Sorbent material is a molecular sieve.
Above-mentioned exsiccant methane rich is entered ice chest liquefaction, and the liquid that condensation is got off is exactly the product natural gas liquids.Flow is 9268.5kg/h, wherein methane 85.964% (mol).Non-condensable gas returns unit, transformation adsorption and enrichment methane unit inlet.
Embodiment 2
Present embodiment carries out pre-treatment with coke-oven gas through taking off naphthalene, benzene and tar unit, removes the CO in the thick coke-oven gas then through MDEA decarburization unit
2, with methane component and the cutting of other component, the cat head component is as synthetic gas by transformation adsorption and enrichment methane unit, and the last liquefaction of enrich methane gas makes liquefied natural gas product.The concrete treatment process of its each step is as follows:
⑴ take off benzene, naphthalene, tar
Coke-oven gas after the compression cooling removes wherein benzene, naphthalene, tar through purifying treatment, obtains raw gas, adopts TSA to handle.
The coke-oven gas that the external world is come enters TSA bed, the naphthalene in the coke-oven gas, tar, benzene, C from the bed bottom
5Above heavy constituent are adsorbed successively, reach the requirement of MDEA decarburization.Its concrete treatment process is: coke-oven gas is entering the TSA adsorption bed from the bed bottom, it is adsorbed that strong absorbed component such as the naphthalene in the coke-oven gas, tar, benzene is adsorbed agent successively, weak absorbed component is sent through the adsorption bed top, after the impurity in the coke-oven gas reaches normality, stop absorption, bed layer pressure is dropped to normal pressure.Use the resurgent gases that is heated to 240 ℃ that bed is heated up then, at the bottom of tower, discharge bed with resurgent gases behind the strong absorbed component heated volatile in the bed and make bed obtain regeneration.Heater heats is gone as resurgent gases in the regeneration back after taking away the bed waste heat through the coke-oven gas cooling bed that purifies.Boost after bed drops to 40 ℃ and wait for use when next time adsorbing.Resurgent gases is after cooling, gas-liquid separation, and gas can be sent into torch burning and handle or enter the fuel pipe network, and liquid and solid can be as fuel or further refining naphthalene, the benzene etc. of obtaining.3 of adsorption towers.The bed sorbent material is coke, aluminum oxide, silica gel, and volume ratio is 5:30:65.
Wherein extraneous next coke-oven gas tolerance 45657.3Nm
3/ h, pressure 100KPa, 40 ℃ of temperature are formed (vol%): H
257.0, O
20.6, N
25.0, CO 9.0, CO
22.0, H
2O 2.4, CH
423, C
23.0, hydrogen sulfide, naphthalene, benzene, tar, C
5More than reorganization grades a small amount of.
Remove the compressed machine pressurization of the coke-oven gas 1700KPa of benzene, naphthalene, tar, cool to 40 ℃, enter MDEA decarburization unit then.
⑵ MDEA decarburization
Above-mentioned raw gas is fed the bottom, absorption tower, use the CO in the MDEA absorption liquid absorption raw gas
2, purified gas is discharged through gas-liquid separator by the top, absorption tower and is entered psa unit, and rich solution is through poor-rich solution interchanger, the amine liquid pump, regenerator column, absorption tower, the CO that removes are returned in water cooler regeneration
2Give other unit or directly discharging.CO
2Chun Du ≧ 99%.
Service temperature is 1670KPa, 40 ℃, absorb through MDEA, and gaseous fraction becomes: H
257.715, O
20.608, N
25.063, CO 9.113, CO
20, H
2O 1.175, CH
423.289, C
23.038.
⑶ transformation adsorption and enrichment methane
Adopt the absorption of one-level transformation, with the entering methane from transformation absorption from the adsorption bed bottom and concentrate bed of the non-condensable gas of the mixed liquefied natural gas liquefaction of above-mentioned purified gas, strong absorbed component such as methane is adsorbed, and the cat head synthetic gas goes to other unit.
After methane concentration in the cat head synthetic gas reaches 1.7% (vol), by eight equal pressure drops adsorption column pressure is dropped to 450KPa, reclaim effective constituent, improve the bed methane concentration, all press the back to adjust the bed methane concentration along putting, along being put into 400 KPa, bed methane purity reaches greater than 83% (vol), enters surge tank along venting.Along after putting end, step-down is contrary at the bottom of by tower puts liquefaction unit or directly send for methane.After emitting product gas, that uses psa unit purges regeneration along venting to bed.Bed regeneration back boost pressure, and use the cat head synthetic gas that pressure is raised to adsorptive pressure, wait for and using again when adsorbing next time.Sweep gas is returned the coke-oven gas suction port of compressor
The service temperature of coke-oven gas is 1640KPa, and 40 ℃, through transformation adsorption and enrichment methane, the gaseous fraction of the synthetic gas that cat head comes out becomes: H
278.868, O
20.824, N
26.742, CO 11.864, CO
20, CH
41.7, C
20.002.
Adopt 13 adsorption towers in the transformation adsorbed methane enrichment system, wherein two towers absorption is all pressed, is used for adsorption tower along venting and purges regeneration for eight time.Sorbent material admission space ratio aluminum oxide: gac: molecular sieve 5:75:20.
⑷ liquefaction
Above-mentioned high methane gas is compressed to 5.5MPa, and feeding TSA molecular sieve bed after cooling to 40 ℃ dewaters, and high methane gas enters the bed dehydration from cat head, and water etc. contain strong absorbed component and are adsorbed, and weak absorbed component such as methane enters ice chest liquefaction.Stop absorption after the dew point of methane rich reaches-75 ℃, bed layer pressure drops to 1.6MPa then, uses dry gas to be warmed up to 240 ℃ bed is regenerated.The regeneration back uses dry gas that bed temperature is dropped to 40 ℃, and the bed that heats up is removed in the resurgent gases heating.Use dry gas that bed layer pressure slowly is raised to adsorptive pressure then.
Three tower dryings, tower absorption, a tower heats up, tower cooling, intensification and cooling are continuously.Sorbent material is a molecular sieve.
Above-mentioned exsiccant methane rich is entered ice chest liquefaction, and the liquid that condensation is got off is exactly the product natural gas liquids.Flow is 9268.5kg/h, wherein methane 85.964% (mol).Non-condensable gas returns transformation adsorbed methane enrichment unit inlet.
Claims (3)
1. one kind is the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, may further comprise the steps:
(1) pre-treatment:
Coke-oven gas is carried out pre-treatment, remove wherein benzene, naphthalene, tar, C
5Above heavy constituent obtain raw gas;
(2) MDEA decarburization:
Step (1) gained raw gas is fed the bottom, absorption tower, the CO in MDEA decarburization absorption raw gas
2, purified gas enters psa unit by the top, absorption tower after gas-liquid separator is discharged, and rich solution (is rich in CO
2Absorption liquid) after poor-rich solution interchanger heat exchange, separate separation of C O to regenerator column regeneration by amine liquid pump pump
2After lean solution tell the back at the bottom of the Tata by regeneration and return the absorption tower by water cooler regeneration, by the CO of pure degree ≧ 99% of regenerator column removed overhead
2After the cooling gas-liquid separation, enter other unit or directly discharging;
(3) transformation adsorption and enrichment methane:
With step (2) gained purified gas with send into one or more levels pressure-swing absorption apparatus after the unitary non-condensable gas of natural gas liquefaction mixes, by transformation absorption with the H in the purified gas
2, N
2, CO separates with methane, collects the cat head component and obtains synthetic gas, the methane of enrichment enters liquefaction unit,
The step of described transformation absorption is: absorption, and all pressure drops along putting, are replaced, and contrary putting vacuumizes, and boosts all voltage rises, final rise along venting; Perhaps absorption, all pressure drops, along putting, contrary putting boosted along venting, all voltage rises, final rise;
The absorption of described transformation is sorbent used be in aluminum oxide, silica gel, gac or the molecular sieve any two or more, the quantity of every grade of adsorption tower is 4～20;
(4) liquefaction:
The methane gas of step (3) enrichment is compressed to 0.8～6.0MPa, cools to bottom or the top of sending into TSA molecular sieve bed behind the normal temperature, concentrate methane gas at the bottom of the tower or cat head enter bed and dehydrate, the methane dew point stops absorption after reaching set(ting)value, use dry gas that bed is carried out equipressure or step-down regeneration, the regeneration back uses dry gas that bed layer pressure slowly is raised to adsorptive pressure, adsorptive pressure is 0.8～6.0MPa, and the resurgent gases temperature is 150～300 ℃;
Above-mentioned exsiccant methane rich is sent into ice chest liquefaction, obtain natural gas liquids, non-condensable gas is sent into the unitary inlet of transformation adsorption and enrichment methane.
2. according to claim 1 is in the method for raw material production natural gas liquids and synthetic gas, to it is characterized in that with the coke-oven gas: step (1) pre-treatment removes benzene, naphthalene, tar, the C in the coke-oven gas
5The concrete grammar of above heavy constituent is: coke-oven gas is compressed to 0.1 MPa～4.0MPa, is cooled to 10 ℃～60 ℃, remove part naphthalene, tar and benzene component, the coke-oven gas process purifying treatment after lowering the temperature be will compress then, remaining benzene, naphthalene, tar and C removed
5Above heavy constituent obtain raw gas;
Perhaps coke-oven gas removes wherein benzene, naphthalene, tar, C through purifying treatment
5Above heavy constituent obtain raw gas, are compressed to 0.1～4.0MPa then and cool to 10～60 ℃ and enter the MDEA decarburization.
3. according to claim 2 is in the method for raw material production natural gas liquids and synthetic gas with the coke-oven gas, it is characterized in that: the method that coke oven gas purification described in the step (1) is handled is: adopt one-level or secondary alternating temperature adsorption method to carry out purifying treatment, the adsorption tower of each grade is 2～8, each level all has a tower to be in the heating and cooling state simultaneously, the bed sorbent material is wherein any two kinds or two or more of coke, gac, aluminum oxide, silica gel, and the bed regeneration temperature is 150～300 ℃.
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| CN104673417B (en) * | 2015-02-16 | 2017-03-15 | 上海尧兴投资管理有限公司 | The system and method for precooling and dry decontamination for natural gas from coal |
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| CN105567360A (en) * | 2016-01-27 | 2016-05-11 | 中科合成油工程股份有限公司 | Method and system for preparing liquefied natural gas from coal-to-oil purified synthesis gas |
| CN108102752A (en) * | 2017-07-19 | 2018-06-01 | 湖北申昙环保新材料有限公司 | The method that coke-stove gas produces natural gas |
| CN109111968A (en) * | 2018-09-06 | 2019-01-01 | 鄂尔多斯应用技术学院 | A kind of method that coke-stove gas prepares liquefied natural gas |
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| CN109504479A (en) * | 2018-12-26 | 2019-03-22 | 黑龙江建龙化工有限公司 | Reduce the new method of LNG decarbonization process amine liquid foaming |
| CN112604453A (en) * | 2020-11-23 | 2021-04-06 | 上海电机学院 | Decompression adsorption equipment gas recycle device among carbon disulfide production process |
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