CN203869420U - Synthesis gas separation system applicable for using in coal-made methanol device - Google Patents

Synthesis gas separation system applicable for using in coal-made methanol device Download PDF

Info

Publication number
CN203869420U
CN203869420U CN201420256176.9U CN201420256176U CN203869420U CN 203869420 U CN203869420 U CN 203869420U CN 201420256176 U CN201420256176 U CN 201420256176U CN 203869420 U CN203869420 U CN 203869420U
Authority
CN
China
Prior art keywords
gas
heat exchanger
distillation column
liquid
low
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.)
Withdrawn - After Issue
Application number
CN201420256176.9U
Other languages
Chinese (zh)
Inventor
赖秀文
张淑文
陈兵
柯云龙
应勇江
胡明辉
孙石桥
周冬根
陈海燕
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hangzhou Hangyang Co Ltd
Original Assignee
Hangzhou Hangyang Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Hangzhou Hangyang Co Ltd filed Critical Hangzhou Hangyang Co Ltd
Priority to CN201420256176.9U priority Critical patent/CN203869420U/en
Application granted granted Critical
Publication of CN203869420U publication Critical patent/CN203869420U/en
Anticipated expiration legal-status Critical
Withdrawn - After Issue legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0271—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of H2/CO mixtures, i.e. of synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A synthesis gas separation system applicable for using in a coal-made methanol device is mainly constituted of four groups of fin-type heat exchangers, and comprises a reboiler, two condensers, two low-temperature distillation columns of two gas-liquid separation tanks, a turbine compressor and a booster expansion turbine, wherein a first feeding is sequentially communicated with first heat source channels of four groups of heat exchangers and is connected with a feeding port on the bottom of a first distillation column; a liquid outlet on the bottom of the first distillation column is connected to third cool source channels of the second and the third heat exchangers and is connected to a feeding port in the middle of the second distillation column; the top portion of the first distillation column is sequentially connected to a first condenser and a first gas-liquid separation tank; the liquid outlet of the first gas-liquid separation device is connected to a liquid returning port of the first distillation column; a gas outlet of the first gas-liquid separation device is connected to the cool source channel of the fourth heat exchanger, and is mixed with the gas on the top portion of the second distillation column and then the gas outlet is connected with the second cool source channels of the first, second and third heat exchangers; and after the gas is received, the gas can be a synthesis gas of a downstream methanol process.

Description

A kind of synthesis gas piece-rate system being applicable in coal methanol device processed
Technical field
The utility model relates to the synthesis gas piece-rate system in a kind of coal methanol project processed, particularly, the utility model is the boiling point difference of utilizing various gas components, realize the separation of admixture of gas by cryogenic rectification, can apply in the liquefaction and separator of industrial multicomponent gas.
Background technology
Methyl alcohol is as the extremely important industrial chemicals of one, and in China, more than 80% methyl alcohol derives from coal conversion, and this depends on the current resources situation of the rich coal of China, weak breath, oil starvation.State's internal olefin is produced mainly based on naphtha pyrolysis at present, how highly therefore can say that petroleum import interdependency has, and how high the external interdependency of alkene industry just have.1993 start, and China becomes crude oil net importer, and to 2009 end of the years, the external interdependency of Chinese crude oil exceedes 50% " the international line of guarding against ", and import volume reaches 2.04 hundred million tons.And methyl alcohol is as the important source material of alkene, according to statistics, methanol-to-olefins project in 2010, methyl alcohol consumption figure only has 300,000 tons, mean and only produced 100,000 tons of ethene, by the end of in October, 2011, domestic only have three cover olefin hydrocarbon making by coal devices to go into operation, the alkene project production capacity of later stage Program Construction is estimated to break through 1,800 ten thousand tons, and the new and effective olefin hydrocarbon making by coal device of utility model is extremely urgent.
The explored coal reserves of China is up to more than 2,000 hundred million tons, Coal Chemical Industry is that a development is rapid, the industry that prospect is very grand, utilize coal methyl alcohol processed, follow-up coproduction alkene, erects the bridge of coal and alkene, has utilized to greatest extent the various active ingredients in coal gasification, reduce the discharge of greenhouse gases simultaneously, belonged to environmental protection project and comprehensive utilization of resources project.In addition, popularization methanol fuel part petroleum replacing product is significant to Chinese Energy restructuring, alleviation contradiction between oil supply and demand.
Synthesis gas deep cooling process for separating is the key link of separation of products and product quality in coal methanol device processed, is CO/H in synthesis gas 2the guarantee of purity, other technique overall compact floor spaces are little relatively for deep cooling process for separating, and operating cost is low, especially on large-scale device, uses and has very large economic benefit.
Utility model content:
The purpose of this utility model is to overcome the deficiency that prior art exists, and provides a kind of flow process simple, and equipment investment expense is low, and what operating cost was low is applicable to the synthesis gas piece-rate system in coal methanol device processed, and it adopts nitrogen expansion kind of refrigeration cycle is CO/H continuously 2synthesis gas and methane separation provide cold, and the qualified LNG product of coproduction.
The purpose of this utility model completes by following technical solution, the synthesis gas piece-rate system being applicable in coal methanol device processed described in the utility model, it is mainly by four groups of plate-fin heat exchangers, comprise a reboiler, two condensers, two low-temperature fractionating towers of two knockout drums, a turbocompressor and a booster expansion turbine composition, the first charging is communicated with the bottom feed mouth that is connected in the first rectifying column after the first thermal source passage of four groups of heat exchangers successively, the bottom liquid phases outlet of the first rectifying column is connected in second, the 3rd low-temperature receiver passage of the 3rd heat exchanger is also connected in the middle part charging aperture of Second distillation column,
The top of the first rectifying column is connected in the first condenser and the first knockout drum successively, and connected the liquid phase return port of the first rectifying column by the liquid-phase outlet of the first gas-liquid separator, the gaseous phase outlet of the first knockout drum be connected in the low-temperature receiver passage of the 4th heat exchanger and mix with the top gas phase of Second distillation column after be connected the second low-temperature receiver passage of first, second and third heat exchanger, and after picking out as the synthesis gas of downstream methanol technics.
The top gaseous phase outlet of Second distillation column described in the utility model is connected in the second knockout drum after connecting the second condenser again, liquid-phase outlet connects the return port of Second distillation column, and gas phase is being mixed at the passage place that picks out of the 4th heat exchanger with the top gas phase of the first rectifying column; The bottom of Second distillation column is connected in second and third, the Secondary Heat Source passage of four heat exchangers picks out, as LNG product.
First be connected in the entrance of turbocompressor as the nitrogen of the second charging, after the pressurized end of turbocompressor outlet connection turbo-expander, be connected in again the Secondary Heat Source passage of First Heat Exchanger, after First Heat Exchanger, be connected in the reboiler of Second distillation column, connected the 3rd thermal source passage of the second heat exchanger by this reboiler, be connected to again and carry out the turbo-expander expansion throttling end that generating portion liquid phase is carried out gas-liquid separation after decrease temperature and pressure, the liquid-phase outlet of described turbo-expander has been connected in the first condenser of the first rectifying column of sweat cooling, after the evaporation of this first condenser, gas phase end is connected in the 4th heat exchanger the first low-temperature receiver passage of recovery section cold after being connected with the gaseous phase outlet mixing after turbo-expander separation, after picking out, be connected in the second condenser of released cold quantity, be connected in successively again and carry out first of cold recovery, two, three heat exchanger the first low-temperature receiver passages, finally the low-pressure gas after rewarming picked out to the entrance of turbocompressor and complete kind of refrigeration cycle one time.
Under the prerequisite that the utility model requires in the synthesis gas piece-rate system meeting in coal methanol device processed, have overall compact, floor space is little, energy consumption is lower, and cryogen consumption is few, safe, adapt to the features such as load shedding operating mode operation, especially on large-scale device, use and there is very large economic benefit.
Brief description of the drawings
Fig. 1 is process chart described in the utility model.
Shown in figure: E01-First Heat Exchanger, T01-the first rectifying column, E02-the second heat exchanger, T02-Second distillation column, E03-the 3rd heat exchanger, V01-the first knockout drum, E04-the 4th heat exchanger, V02-the second knockout drum, E05-the first condenser, E06-the second condenser, E07-Second distillation column reboiler, C1-turbocompressor, ET1-booster expansion turbine.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described in detail: shown in Fig. 1, the synthesis gas piece-rate system being applicable in coal methanol device processed described in the utility model, it is mainly by four groups of plate-fin heat exchanger E01, E02, E03, E04, comprise a reboiler E07, two condensers E05, E06, two knockout drum V01, two low-temperature fractionating tower T01 of V02, T02, a turbocompressor C1 and a booster expansion turbine ET1 composition, the first charging is communicated with four groups of heat exchanger E01 successively, E02, E03, after the first thermal source passage of E04, be connected in the bottom feed mouth of the first rectifying column T01, the bottom liquid phases outlet of the first rectifying column T01 is connected in second, the 3rd heat exchanger E02, the 3rd low-temperature receiver passage of E03 is also connected in the middle part charging aperture of Second distillation column T02,
The top of the first rectifying column T01 is connected in the first condenser E05 and the first knockout drum V01 successively, and connected the liquid phase return port of the first rectifying column T01 by the liquid-phase outlet of the first gas-liquid separator V01, the gaseous phase outlet of the first knockout drum V01 be connected in the low-temperature receiver passage of the 4th heat exchanger E04 and mix with the top gas phase of Second distillation column T02 after be connected the second low-temperature receiver passage of first, second and third heat exchanger E01, E02, E03, and after picking out as the synthesis gas of downstream methanol technics.
The top gaseous phase outlet of Second distillation column T02 described in the utility model is connected in the second knockout drum V02 after connecting the second condenser E06 again, liquid-phase outlet connects the return port of Second distillation column T02, and gas phase is being mixed at the passage place that picks out of the 4th heat exchanger E04 with the top gas phase of the first rectifying column T01; The bottom of Second distillation column T02 is connected in second and third, the Secondary Heat Source passage of four heat exchanger E02, E03, E04 picks out, as LNG product.
First be connected in the entrance of turbocompressor C1 as the nitrogen of the second charging, after the pressurized end of turbocompressor C1 outlet connection turbo-expander, be connected in again the Secondary Heat Source passage of First Heat Exchanger E01, after First Heat Exchanger E01, be connected in the reboiler E07 of Second distillation column T02, connected the 3rd thermal source passage of the second heat exchanger E02 by this reboiler E07, be connected to again and carry out the turbo-expander ET1 expansion throttling end that generating portion liquid phase is carried out gas-liquid separation after decrease temperature and pressure, the liquid-phase outlet of described turbo-expander ET1 has been connected in the first condenser E05 of the first rectifying column T01 of sweat cooling, after the evaporation of this first condenser E05, gas phase end is connected in the 4th heat exchanger E04 the first low-temperature receiver passage of recovery section cold after being connected with the gaseous phase outlet mixing after turbo-expander ET1 separation, after picking out, be connected in the second condenser E06 of released cold quantity, be connected in successively again and carry out first of cold recovery, two, three heat exchanger E01, E02, E03 the first low-temperature receiver passage, finally the low-pressure gas after rewarming picked out to the entrance of turbocompressor C1 and complete kind of refrigeration cycle one time.
Shown in Fig. 1, what the gasification system of coal described in the utility model methanol device processed produced mainly comprises hydrogen, carbon monoxide, the unstripped gas such as methane, first pass through molecular sieve adsorption unit depth carbon dioxide removal, water, hydrogen sulfide, methyl alcohol, enter again synthesis gas piece-rate system as the first charging G1, described First Heat Exchanger E01 is furnished with two thermal source passages and two low-temperature receiver passages, the second heat exchanger E02 is furnished with three thermal source passages and two low-temperature receiver passages, the 3rd heat exchanger E03 is furnished with two thermal source passages and three low-temperature receiver passages, the 4th heat exchanger E04 is furnished with two thermal source passages and two low-temperature receiver passages, the first thermal source passage that the first charging G1 enters four groups of heat exchangers is successively cooled to-162 DEG C, then enters the bottom of the first rectifying column T01 as charging G2.
The 3rd low-temperature receiver passage that the bottom distillate of the first rectifying column T01 is connected in second, third heat exchanger E02, E03 carries out cold recovery, rewarming to the middle part that enters Second distillation column T02 after-123 DEG C～-127 DEG C as charging G3; The top gas phase of the first rectifying column is connected in condenser E05 and is cooled to-173.6 DEG C for gas-liquid two-phase, and enter the first knockout drum V01 and separate, liquid phase is returned to the first rectifying column as phegma, gas phase SG1 is connected in the second low-temperature receiver passage of the 4th heat exchanger E04, the the second low-temperature receiver passage that goes out to enter after mixing with the top gas phase SG2 of Second distillation column after E04 first, second and third heat exchanger reclaims cold, and the gas SG3 after rewarming is as hydrogen and the carbon monoxide synthetic gas of downstream methanol technics.
The top gas phase of described Second distillation column T02 enters condenser E06 and is cooled to-145 DEG C for gas-liquid two-phase, and be connected in the second knockout drum V02 and separate, liquid phase is returned to Second distillation column as phegma, and gas phase SG2 mixes at the second low-temperature receiver passage exit place of E04 with the top gas phase SG1 of the first rectifying column; The distillate that Second distillation column T02 bottom is mainly methane enters second and third, the Secondary Heat Source passage of four heat exchangers carried out coldly, and LG1 is cooled to-162 DEG C, throttling and stores to entering storage tank as liquefied natural gas product after 17KPaG.
First be connected in the entrance of turbocompressor C1 as the nitrogen of the second low-temperature receiver charging, be cooled to 34bar through overcompression, the pressurized end that enters turbo-expander after 40 DEG C is pressurized to 48.2bar, after N1 is cooling, enter the Secondary Heat Source passage 2 of First Heat Exchanger E01, after going out E01, be cooled to the reboiler E07 that enters Second distillation column after-75 DEG C, after release heat, be cooled to-90.4 DEG C of the 3rd thermal source passages that enter the second heat exchanger and continue to be cooled to-113.5 DEG C, N2 picks out to turbo-expander ET1 and carries out expansion throttling to 5.6bar from passage,-177.8 DEG C, after N3 expands, generating portion liquid phase is carried out gas-liquid separation, the condenser E05 that isolated liquid phase enters the first rectifying column provides cold for overhead reflux, gas phase after evaporation with separate after gas phase return to the first low-temperature receiver passage recovery section cold of the 4th heat exchanger E04 after mixing, rewarming provides cold to the condenser E06 that enters Second distillation column after-164.5 DEG C for overhead reflux, after released cold quantity, return to first, two, the first low-temperature receiver passage of three heat exchangers carries out cold recovery, low-pressure gas N5 after rewarming picks out to the entrance of turbocompressor C1 and completes kind of refrigeration cycle one time, described nitrogen, as the main cold carrier of whole system, by decompressor swell refrigeration, and completes closed cycle by compressor boost.

Claims (3)

1. the synthesis gas piece-rate system being applicable in coal methanol device processed, it is characterized in that described synthesis gas piece-rate system is mainly by four groups of plate-fin heat exchangers, comprise a reboiler, two condensers, two low-temperature fractionating towers of two knockout drums, a turbocompressor and a booster expansion turbine composition, the first charging is communicated with the bottom feed mouth that is connected in the first rectifying column after the first thermal source passage of four groups of heat exchangers successively, the bottom liquid phases outlet of the first rectifying column is connected in second, the 3rd low-temperature receiver passage of the 3rd heat exchanger is also connected in the middle part charging aperture of Second distillation column,
The top of the first rectifying column is connected in the first condenser and the first knockout drum successively, and connected the liquid phase return port of the first rectifying column by the liquid-phase outlet of the first gas-liquid separator, the gaseous phase outlet of the first knockout drum be connected in the low-temperature receiver passage of the 4th heat exchanger and mix with the top gas phase of Second distillation column after be connected the second low-temperature receiver passage of first, second and third heat exchanger, and after picking out as the synthesis gas of downstream methanol technics.
2. the synthesis gas piece-rate system being applicable in coal methanol device processed according to claim 1, after connecting the second condenser, the top gaseous phase outlet that it is characterized in that described Second distillation column is connected in again the second knockout drum, liquid-phase outlet connects the return port of Second distillation column, and gas phase is being mixed at the passage place that picks out of the 4th heat exchanger with the top gas phase of the first rectifying column; The bottom of Second distillation column is connected in second and third, the Secondary Heat Source passage of four heat exchangers picks out, as LNG product.
3. the synthesis gas piece-rate system being applicable in coal methanol device processed according to claim 1 and 2, it is characterized in that being first connected in as the nitrogen of the second charging the entrance of turbocompressor, after the pressurized end of turbocompressor outlet connection turbo-expander, be connected in again the Secondary Heat Source passage of First Heat Exchanger, after First Heat Exchanger, be connected in the reboiler of Second distillation column, connected the 3rd thermal source passage of the second heat exchanger by this reboiler, be connected to again and carry out the turbo-expander expansion throttling end that generating portion liquid phase is carried out gas-liquid separation after decrease temperature and pressure, the liquid-phase outlet of described turbo-expander has been connected in the first condenser of the first rectifying column of sweat cooling, after the evaporation of this first condenser, gas phase end is connected in the 4th heat exchanger the first low-temperature receiver passage of recovery section cold after being connected with the gaseous phase outlet mixing after turbo-expander separation, after picking out, be connected in the second condenser of released cold quantity, be connected in successively again and carry out first of cold recovery, two, three heat exchanger the first low-temperature receiver passages, finally the low-pressure gas after rewarming picked out to the entrance of turbocompressor and complete kind of refrigeration cycle one time.
CN201420256176.9U 2014-05-19 2014-05-19 Synthesis gas separation system applicable for using in coal-made methanol device Withdrawn - After Issue CN203869420U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201420256176.9U CN203869420U (en) 2014-05-19 2014-05-19 Synthesis gas separation system applicable for using in coal-made methanol device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201420256176.9U CN203869420U (en) 2014-05-19 2014-05-19 Synthesis gas separation system applicable for using in coal-made methanol device

Publications (1)

Publication Number Publication Date
CN203869420U true CN203869420U (en) 2014-10-08

Family

ID=51650363

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201420256176.9U Withdrawn - After Issue CN203869420U (en) 2014-05-19 2014-05-19 Synthesis gas separation system applicable for using in coal-made methanol device

Country Status (1)

Country Link
CN (1) CN203869420U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103983086A (en) * 2014-05-19 2014-08-13 杭州杭氧股份有限公司 Synthesis gas separation system suitable for methyl alcohol making device by coal and cryogenic separation method for making LNG (liquefied natural gas)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103983086A (en) * 2014-05-19 2014-08-13 杭州杭氧股份有限公司 Synthesis gas separation system suitable for methyl alcohol making device by coal and cryogenic separation method for making LNG (liquefied natural gas)
CN103983086B (en) * 2014-05-19 2016-03-30 杭州杭氧股份有限公司 A kind of method being applicable to synthesis gas piece-rate system in ammonia from coal device and cryogenic separation LNG

Similar Documents

Publication Publication Date Title
Hashemi et al. Cryogenic vs. absorption biogas upgrading in liquefied biomethane production–An energy efficiency analysis
CN102115684B (en) Method for producing liquefied natural gas by using coke oven gas
RU2350553C2 (en) Method and device for natural gas products, containing helium and liquefied natural gas
CN101539362B (en) Multi-stage inflated distribution type natural gas liquefying system considering total energy system
CN201251346Y (en) Separating equipment for producing liquefied natural gas from coke-oven gases
Xu et al. Hydrogen and LNG production from coke oven gas with multi-stage helium expansion refrigeration
CN102620521B (en) Technology and device for removing hydrogen and nitrogen from methane rich gas and producing liquefied natural gas
CN108610229B (en) Light hydrocarbon separation system and method
CN105180595A (en) System and method for preparing hydrogen rich gas and liquid methane
CN104845692A (en) Oilfield associated gas complete liquefaction recovery system and method thereof
CN108795508A (en) A method of detaching coke-stove gas using nitrogen and helium swell refrigeration
CN103868324B (en) The natural gas liquefaction of small-sized skid-mounted type mix refrigerant and NGL reclaim integrated system
CN103983086B (en) A kind of method being applicable to synthesis gas piece-rate system in ammonia from coal device and cryogenic separation LNG
CN102435045A (en) Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof
CN203513622U (en) Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG)
CN103697661B (en) The device and method of liquefied natural gas and rich hydrogen production is produced from coke-stove gas
CN202494272U (en) Device for removing hydrogen and nitrogen from high methane gas and producing liquefied natural gas
CN203869420U (en) Synthesis gas separation system applicable for using in coal-made methanol device
CN103773529B (en) Pry-mounted associated gas liquefaction system
CN202382518U (en) Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas)
CN102620522B (en) Process and device for producing liquefied natural gas (LNG) and removing hydrogen and nitrogen through throttling flash evaporation
CN109028756B (en) A method of coke-stove gas is separated using helium swell refrigeration
CN201377962Y (en) Equipment producing compressed natural gas from mixed gas containing methane
CN205893188U (en) Utilize ft synthesis tail gas system liquefied natural gas's device
CN102277215B (en) Method and device for producing liquefied natural gas (LNG) from coke oven gases through cryogenic distillation

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
AV01 Patent right actively abandoned

Granted publication date: 20141008

Effective date of abandoning: 20160330

AV01 Patent right actively abandoned

Granted publication date: 20141008

Effective date of abandoning: 20160330

C25 Abandonment of patent right or utility model to avoid double patenting