CN106642988A - System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG - Google Patents

System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG Download PDF

Info

Publication number
CN106642988A
CN106642988A CN201611113494.XA CN201611113494A CN106642988A CN 106642988 A CN106642988 A CN 106642988A CN 201611113494 A CN201611113494 A CN 201611113494A CN 106642988 A CN106642988 A CN 106642988A
Authority
CN
China
Prior art keywords
heat exchanger
nitrogen
pipeline
tower
gas
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.)
Granted
Application number
CN201611113494.XA
Other languages
Chinese (zh)
Other versions
CN106642988B (en
Inventor
徐小勤
张斌
张海军
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.)
Zhongkerio Energy Technology Wuxi Co ltd
Original Assignee
In Keruiao Energy Polytron Technologies Inc
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 In Keruiao Energy Polytron Technologies Inc filed Critical In Keruiao Energy Polytron Technologies Inc
Priority to CN201611113494.XA priority Critical patent/CN106642988B/en
Publication of CN106642988A publication Critical patent/CN106642988A/en
Application granted granted Critical
Publication of CN106642988B publication Critical patent/CN106642988B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • F25J3/0228—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
    • F25J3/0204—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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • 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
    • F25J3/0261—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 carbon monoxide
    • 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
    • F25J3/0276—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/N2 mixtures, i.e. of ammonia 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
    • F25J2200/72—Refluxing the column with at least a part of the totally 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising 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
    • F25J2270/18—External refrigeration with incorporated cascade 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
    • 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
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Disclosed is a system of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG. The system comprises a first heat exchanger, a second heat exchanger, a dehydrogenation tower, a liquid nitrogen wash tower, a methane tower, a nitrogen refrigerating system and a medium voltage nitrogen inlet pipe, wherein the medium voltage nitrogen inlet pipe is connected to a medium voltage nitrogen gas source, the medium voltage nitrogen inlet pipe is connected to the liquid nitrogen wash tower after passing the first heat exchanger, the second heat exchanger and a third heat exchanger, the medium voltage nitrogen inlet pipe is communicated with a first pipeline through a first inlet pipe, a communication point between the first inlet pipe and the first pipeline is located between a nitrogen compressor unit and the first heat exchanger, and the first inlet pipe is provided with a first valve. According to the system of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG, qualified syngas for synthetic ammonia is produced, and an LNG product with a high additional value is obtained at the same time; in addition, when a synthesis ammonia system stops, stable operation of the system can be guaranteed under the situation that a raw material of ammonia synthesis is not produced.

Description

The system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing
Technical field
The present invention relates to synthesis is produced in the purified treatment field of syngas for synthetic ammonia, more particularly to one kind using liquid nitrogen washing The system of ammonia unstripped gas and LNG.
Background technology
The unstripped gas that ammonia synthesis process needs includes nitrogen and hydrogen, and nitrogen hydrogen ratio is 3:1 or so, if the original of synthesis ammonia Containing liquefied natural gas and carbon monoxide in material gas, synthetic ammonia catalyst can be caused to be poisoned, therefore obtain syngas for synthetic ammonia When, nitrogen hydrogen ratio is not only controlled, while also to control the hazardous medium in unstripped gas.
Methane, carbon monoxide, hydrogen, nitrogen are rich in oven gas, when the unstripped gas of synthesis ammonia is done using oven gas, must The methane and carbon monoxide component in oven gas must be removed.The methane in oven gas can be removed by way of low temperature liquid nitrogen is washed And carbon monoxide, therefore liquid nitrogen washing is the important way of purifying gas as raw material for synthesis of ammonia.Synthesis ammonia system and liquid nitrogen in reality production Wash system to connect by pipeline, when complex structure synthesis ammonia system stops because of maintenance or other reasonses, liquid nitrogen washing system is not yet Obtain not parking, so bringing many unnecessary losses, particularly ice chest to start after stopping needs plenty of time and the energy, existing In technology, lack when synthesis ammonia system stops, it is ensured that the liquid nitrogen washing system of the stable operation of system.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of simple structure, the utilization liquid nitrogen washing system that flow process can switch The system for taking syngas for synthetic ammonia and LNG.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, including：
For making the First Heat Exchanger of unstripped gas tentatively cooling, it is connected by pipeline with unstripped gas source of the gas；
For the second heat exchanger that the unstripped gas for making preliminary cooling is lowered the temperature again, it is connected by pipeline with First Heat Exchanger；
For making the dehydrogenation tower of the unstripped gas dehydrogenation after lowering the temperature again and gas-liquid separation, connected by pipeline with the second heat exchanger Connect；
Gas phase for isolating to unstripped gas carries out the nitrogen wash column that nitrogen is washed and discharges nitrogen hydrogen, arranges with the gas phase of dehydrogenation tower Outlet is connected by pipeline；
The liquid phase that the liquid phase isolated to unstripped gas and nitrogen wash column are discharged carries out rectification process and discharges liquefied natural gas And the methane tower of rich carbon monoxide gas, connected by pipeline with the liquid phase outlet of separator and the liquid phase outlet of nitrogen wash column Connect；
For providing the nitrogen refrigeration system of cold, the nitrogen refrigeration system includes being compressed for the nitrogen of compressed nitrogen Machine unit, the nitrogen that nitrogen compressor unit is compressed by first pipe road direction methane tower, the conveying of dehydrogenation tower, methane tower, dehydrogenation The nitrogen that tower is discharged transports to nitrogen compressor unit by the second pipeline,
Nitrogen is circulated between nitrogen compressor unit and methane tower, dehydrogenation tower, and the first pipeline sequentially passes through the first heat exchange Device, the second heat exchanger, the 3rd heat exchanger, the second pipeline sequentially passes through the 3rd heat exchanger, the second heat exchanger, First Heat Exchanger, the Nitrogen in one pipeline is changed in First Heat Exchanger, the second heat exchanger, the cooling of the 3rd heat exchanger, the nitrogen in the second pipeline the 3rd Cold is provided in hot device, the second heat exchanger, First Heat Exchanger；
Medium pressure nitrogen gas input pipe, medium pressure nitrogen input pipe is connected with medium pressure nitrogen gas source of the gas, the input of medium pressure nitrogen Pipe is connected after First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger with nitrogen wash column, and medium pressure nitrogen gas input pipe is defeated by first Enter pipe and the first pipeline connection, the first input pipe and the first pipeline connectivity points be located at nitrogen compressor unit and First Heat Exchanger it Between, the first valve is provided with the first input pipe.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, medium pressure nitrogen gas input pipe passes through Second input pipe and the first pipeline connection, the second input pipe and the first pipeline connectivity points be located at nitrogen wash column and the 3rd heat exchanger it Between, the second valve is provided with the second input pipe.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, pacify on medium pressure nitrogen gas input pipe The 3rd valve is filled, the 3rd valve is located between nitrogen wash column and the 3rd heat exchanger.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the nitrogen hydrogen of nitrogen wash column is discharged Mouth and the 4th pipeline connection, the 4th pipeline sequentially passes through the 3rd heat exchanger, the second heat exchanger, First Heat Exchanger.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the gas phase outlet of dehydrogenation tower Nitrogen wash column is connected by the 3rd pipeline, the 3rd pipeline is by the 3rd heat exchanger, so that the gas phase in the 3rd pipeline is cooled.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the liquefied natural gas of methane tower Outlet is connected with LNG discharge pipe, and LNG discharge pipe enters after the second heat exchanger with first throttle valve Mouth connection, so as to pass through first throttle after the liquefied natural gas in LNG discharge pipe is cooled by the second heat exchanger Valve throttling cools.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, also include for providing cold Cryogen refrigeration system, the cryogen refrigeration system includes refrigerant compressor unit and second throttle, the 3rd choke valve, cold The vapor phase refrigerant that agent compressor unit is compressed by the 5th pipeline to second throttle conveying, vapor phase refrigerant is by second section Refrigerant compressor unit is returned by the 7th pipeline after stream valve throttling cooling, the 5th pipeline sequentially passes through First Heat Exchanger, methane Inlet communication after the tower bottom reboiler of tower, the second heat exchanger with second throttle, the 7th pipeline sequentially passes through the second heat exchanger With First Heat Exchanger, the vapor phase refrigerant in the 5th pipeline First Heat Exchanger, the second heat exchanger, methane tower tower bottom reboiler Middle cooling, the vapor phase refrigerant in the 7th pipeline provides cold, refrigerant compressor unit in the second heat exchanger, First Heat Exchanger The liquid phase refrigerant compressed to the conveying of the 3rd choke valve by the 6th pipeline, the 3rd choke valve and the 7th pipeline connection, liquid phase Cold-producing medium returns refrigerant compressor unit after being lowered the temperature by the throttling of the 3rd choke valve by the 7th pipeline, and the 6th pipeline is changed through first Hot device.
The invention provides the system that a kind of utilization liquid nitrogen washing produces syngas for synthetic ammonia and LNG, is producing qualified conjunction While ammonification unstripped gas, the LNG product of high added value is obtained, and when synthesis ammonia system stops, conjunction can not produced During ammonification raw material, it is ensured that the system stable operation.
Description of the drawings
Fig. 1 is the structural representation of the system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG.
Specific embodiment
As shown in figure 1, the system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, including：
For making the First Heat Exchanger E1 of unstripped gas tentatively cooling, it is connected by pipeline with unstripped gas source of the gas；
For the second heat exchanger E2 that the unstripped gas for making preliminary cooling is lowered the temperature again, connected by pipeline with First Heat Exchanger E1 Connect；
For making the dehydrogenation tower T1 of the unstripped gas dehydrogenation after lowering the temperature again and gas-liquid separation, with the second heat exchanger E2 by pipe Road connects；
Gas phase for isolating to unstripped gas carries out the nitrogen wash column T2 that nitrogen is washed and discharges nitrogen hydrogen, the gas with dehydrogenation tower T1 Phase outlet is connected by pipeline；
The liquid phase that the liquid phase isolated to unstripped gas and nitrogen wash column T2 are discharged carries out rectification process and to discharge liquefaction natural The methane tower T3 of gas and rich carbon monoxide gas, leads to the liquid phase outlet of dehydrogenation tower T1 and the liquid phase outlet of nitrogen wash column T2 Cross pipeline connection；
For providing the nitrogen refrigeration system of cold, nitrogen refrigeration system includes the nitrogen compressor list for compressed nitrogen Unit, nitrogen compressor unit by the first pipeline 1 to methane tower T3, the dehydrogenation tower T1 nitrogen that compressed of conveying, it is methane tower T3, de- The nitrogen that hydrogen tower T1 is discharged transports to nitrogen compressor unit by the second pipeline 2, and nitrogen is in nitrogen compressor unit and methane tower Circulate between T3, dehydrogenation tower T1, the first pipeline 1 sequentially passes through First Heat Exchanger E1, the second heat exchanger E2, the 3rd heat exchanger E3, Second pipeline 2 sequentially passes through the 3rd heat exchanger E3, the second heat exchanger E2, First Heat Exchanger E1, and the nitrogen in the first pipeline 1 is One heat exchanger E1, the second heat exchanger E2, the 3rd heat exchanger E3 cooling, the nitrogen in the second pipeline 2 the 3rd heat exchanger E3, second Cold is provided in heat exchanger E2, First Heat Exchanger E1；
Medium pressure nitrogen gas input pipe 10, medium pressure nitrogen gas input pipe 10 is connected with medium pressure nitrogen gas source of the gas, medium pressure nitrogen gas input pipe 10 It is connected with nitrogen wash column T2 after First Heat Exchanger E1, the second heat exchanger E2, the 3rd heat exchanger E3, medium pressure nitrogen gas input pipe 10 leads to Cross the first input pipe 11 to connect with the first pipeline 1, the first input pipe 11 and the connectivity points of the first pipeline 1 are located at nitrogen compressor unit Between First Heat Exchanger E1, the first valve V1 is provided with the first input pipe 11.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, medium pressure nitrogen gas input pipe 10 leads to Cross the second input pipe 12 to connect with the first pipeline 1, the second input pipe 12 and the connectivity points of the first pipeline 1 are located at nitrogen wash column T2 and the 3rd Between heat exchanger E3, the second valve V2 is provided with the second input pipe 12.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, on medium pressure nitrogen gas input pipe 10 3rd valve V3 is installed, the 3rd valve V3 is located between nitrogen wash column T2 and the 3rd heat exchanger E3.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the nitrogen hydrogen row of nitrogen wash column T2 Outlet is connected with the 4th pipeline 4, and the 4th pipeline 4 sequentially passes through the 3rd heat exchanger E3, the second heat exchanger E2, First Heat Exchanger E1.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the gas phase of dehydrogenation tower T1 is discharged Mouth connects nitrogen wash column T2 by the 3rd pipeline 3, and the 3rd pipeline 3 passes through the 3rd heat exchanger E3, so that the gas phase quilt in the 3rd pipeline 3 Cooling.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, the liquefaction of methane tower T3 is natural Gas outlet is connected with LNG discharge pipe 30, LNG discharge pipe 30 after the second heat exchanger E2 with first segment The entrance connection of stream valve V71, so that the liquefied natural gas in LNG discharge pipe 30 is by the second heat exchanger E2 cooling drops Cooled by the throttling of first throttle valve V71 after temperature.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, also include for providing cold Cryogen refrigeration system, cryogen refrigeration system includes refrigerant compressor unit and second throttle 72, the 3rd choke valve 73, cold Agent compressor unit conveys the vapor phase refrigerant compressed to second throttle 72 by the 5th pipeline 5, and vapor phase refrigerant is by Refrigerant compressor unit is returned by the 7th pipeline 7 after the throttling cooling of two choke valve 72, the 5th pipeline 5 sequentially passes through the first heat exchange Inlet communication after device E1, the tower bottom reboiler of methane tower T3, the second heat exchanger E2 with second throttle 72, the 7th pipeline 7 according to It is secondary through the second heat exchanger E2 and First Heat Exchanger E1, the vapor phase refrigerant in the 5th pipeline 5 is changed in First Heat Exchanger E1, second In hot device E2, the tower bottom reboiler of methane tower T3 cool down, the vapor phase refrigerant in the 7th pipeline 7 the second heat exchanger E2, first Cold is provided in heat exchanger E1, refrigerant compressor unit conveys the liquid phase compressed to the 3rd choke valve 73 by the 6th pipeline 6 Cold-producing medium, the 3rd choke valve 73 is connected with the 7th pipeline 7, and liquid phase refrigerant is throttled after lowering the temperature by the 7th by the 3rd choke valve 73 Pipeline 7 returns refrigerant compressor unit, and the 6th pipeline 6 is through First Heat Exchanger E1.
Technical scheme discloses a kind of one kind of achievable handoff functionality and produces synthesis ammonia original using liquid nitrogen washing The system of material gas and LNG.
When technical scheme works, unstripped gas is initially charged the removing of dehydrogenation tower most of Jing after heat exchanger cooling Methane, subsequently into nitrogen wash column, by methane and carbon monoxide below 1ppm is removed to, final acquisition nitrogen hydrogen, cold in unstripped gas Coagulate the liquid phase for and enter methane tower, obtain LNG product and rich carbon monoxide tail gas.When liquid nitrogen wash journey is not needed, flow process is also Can switch, i.e., nitrogen wash column does not have liquid nitrogen to enter, the system that utilization liquid nitrogen washing of the invention produces syngas for synthetic ammonia and LNG Can be with stable operation.
The azeotrope compressor that refrigerant compressor unit includes can be centrifugal compressor, helical-lobe compressor, reciprocal pressure Contracting machine, drive form can be steam drive, electric drive.
The nitrogen compressor that nitrogen compressor unit includes can be centrifugal compressor, helical-lobe compressor, reciprocating compressor, Drive form can be steam drive, electric drive.
Azeotrope used by refrigerant compressor unit is nitrogen, methane, ethene, ethane, propylene, propane, isobutene, different Any combination of butane, isopentane.
Dehydrogenation tower, methane tower, nitrogen wash column can be packed tower, plate column, bubble column, sieve-plate tower.
The system that the utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and LNG, wherein, in medium pressure nitrogen gas input pipe 10 Medium pressure nitrogen gas import be provided with stop valve V10.
The present invention provides the system that a kind of utilization liquid nitrogen washing produces syngas for synthetic ammonia and LNG, is producing qualified synthesis While ammonia unstripped gas, the LNG product of high added value is obtained, and when synthesis ammonia system stops, synthesis can not produced During ammonia raw material, the system stable operation, at this moment unstripped gas go successively to, nitrogen wash column does not work substantially, with save energy and nitrogen, Ice chest (including First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger and refrigeration system) works on, while the system continues The nitrogen hydrogen of rich carbon monoxide gas, qualified LNG product and somewhat lower purity is discharged, is opened again after synthesis ammonia system is keeped in repair Dynamic, the system can be immediately accessed, and normal production is put into quickly, thus avoid a large amount of losses.
It is azeotrope refrigeration that the utilization liquid nitrogen washing of the present invention produces the refrigeration system of the system of syngas for synthetic ammonia and LNG System and nitrogen throttle refrigeration system.
When azeotrope refrigeration system works, the azeotrope from ice chest compresses and after refrigerated separation Jing compressor, liquid Phase cryogen enters First Heat Exchanger, and cold is provided for First Heat Exchanger Jing after decrease temperature and pressure, and gas phase cryogen sequentially enters first and changes Cold is provided for the second heat exchanger, First Heat Exchanger after hot device, methane tower bottom of towe, the second heat exchanger, and warp knuckle stream, and is finally returned To suction port of compressor.
When nitrogen throttle refrigeration system works, come from the low-pressure nitrogen of ice chest Jing after nitrogen compressor compresses, sequentially enter First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger, go out after the 3rd heat exchanger and are divided into two strands, and one enters dehydrogenation tower, in addition one Enter methane tower, respectively dehydrogenation column overhead, methane column overhead provides cold.
Medium pressure nitrogen gas sequentially enters First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger, goes out after the 3rd heat exchanger and enters nitrogen Wash top of tower.
Jing after First Heat Exchanger, the second heat exchanger cool, into dehydrogenation tower, bottom of towe liquid phase enters methane to unstripped gas Tower, gas phase is entered after the further cooling of the 3rd heat exchanger, and from bottom nitrogen wash column is entered, in nitrogen wash column, from the liquid nitrogen that tower top is sprayed into Methane and carbon monoxide in unstripped gas is removed into below 1ppm, qualified nitrogen hydrogen product is finally obtained, is gone out after rewarming and is System, the liquid-phase product of bottom of towe enters methane tower, and in methane column overhead rich CO gas are obtained, and in bottom of towe liquid first is obtained Alkane, and obtain qualified LNG product Jing after the second heat exchanger further cooling.
The utilization liquid nitrogen washing of the present invention produces syngas for synthetic ammonia and the system of LNG includes a set of switch valve, in middle pressure Nitrogen inlet is provided with stop valve V10, and when synthesis ammonia system stops, this valve is closed, and on the first input pipe 11 the first valve is provided with V1, when synthesis ammonia system stops, this valve is opened, and the 3rd valve V3 is installed on medium pressure nitrogen gas input pipe 10, when synthesis ammonia system stops, This valve is closed, and the second valve V2 is provided with the second input pipe 12, and when synthesis ammonia system stops, this valve is opened.
The utilization liquid nitrogen washing of the present invention produces the advantage of the system of syngas for synthetic ammonia and LNG：This system can produce conjunction Ammonification raw material and LNG, and when synthesis ammonia system stops, system can also stable operation.
When the utilization liquid nitrogen washing of the present invention is produced the system of syngas for synthetic ammonia and LNG and is worked, azeotrope Jing compressors After compression and refrigerated separation, liquid phase cryogen enters First Heat Exchanger, is First Heat Exchanger Jing after the decrease temperature and pressure of the 3rd choke valve 73 Cold is provided, gas phase cryogen enters First Heat Exchanger, methane tower T3, the second heat exchanger, Jing after the decrease temperature and pressure of second throttle 72, Cold is provided for the second heat exchanger, is gone out after converging with liquid phase cryogen after the second heat exchanger and is gone out system, and return to suction port of compressor.
Nitrogen Jing nitrogen compressors compress laggard ice chest, sequentially enter First Heat Exchanger, the second heat exchanger, the 3rd heat exchange Device, goes out after the 3rd heat exchanger and is divided into two strands, and one enters dehydrogenation tower T1, and in addition one enters methane tower T3, and cold, and Jing are provided respectively Cooling box after heat exchanger rewarming, and return to nitrogen suction port of compressor.
Unstripped gas sequentially enters First Heat Exchanger, the second heat exchanger, and dehydrogenation tower T1, the liquid phase of dehydrogenation tower bottom enters methane Tower T3, gas phase enters the bottom of nitrogen wash column T2 Jing after the 3rd heat exchanger E3 further cooling, in nitrogen wash column, unstripped gas and liquid nitrogen Caloic exchange is carried out, the methane and carbon monoxide in unstripped gas is removed into below 1ppm, the liquid phase of bottom of towe enters methane tower, gas Phase goes out system Jing after heat exchanger rewarming.In methane tower, rich CO gas are obtained from tower top, system, liquid phase are gone out after rewarming Further lower the temperature and Jing after first throttle valve throttling Jing heat exchanger, you can obtain qualified LNG product.
When synthesis ammonia system stops, that is, when not needing nitrogen wash journey, now stop valve V10 is closed, and the first valve V1 is opened, 3rd valve V3 is closed, and the second valve V2 is opened.
The above is only the preferred embodiment of the present invention, it is noted that for those skilled in the art come Say, under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be regarded as Protection scope of the present invention.

Claims (7)

1. the system that a kind of utilization liquid nitrogen washing produces syngas for synthetic ammonia and LNG, it is characterised in that include：
For making the First Heat Exchanger of unstripped gas tentatively cooling, it is connected by pipeline with unstripped gas source of the gas；
For the second heat exchanger that the unstripped gas for making preliminary cooling is lowered the temperature again, it is connected by pipeline with First Heat Exchanger；
For making the dehydrogenation tower of the unstripped gas dehydrogenation after lowering the temperature again and gas-liquid separation, it is connected by pipeline with the second heat exchanger；
Gas phase for isolating to unstripped gas carries out the nitrogen wash column that nitrogen is washed and discharges nitrogen hydrogen, the gas phase outlet with dehydrogenation tower Connected by pipeline；
The liquid phase that the liquid phase isolated to unstripped gas and nitrogen wash column are discharged carry out rectification process and discharge liquefied natural gas and The methane tower of rich carbon monoxide gas, is connected with the liquid phase outlet of dehydrogenation tower and the liquid phase outlet of nitrogen wash column by pipeline；
For providing the nitrogen refrigeration system of cold, the nitrogen refrigeration system includes the nitrogen compressor list for compressed nitrogen Unit, the nitrogen that nitrogen compressor unit is compressed by first pipe road direction methane tower, the conveying of dehydrogenation tower, methane tower, dehydrogenation tower row The nitrogen for going out transports to nitrogen compressor unit by the second pipeline, nitrogen nitrogen compressor unit and methane tower, dehydrogenation tower it Between circulate, the first pipeline sequentially passes through First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger, and the second pipeline sequentially passes through the 3rd Heat exchanger, the second heat exchanger, First Heat Exchanger, the nitrogen in the first pipeline is in First Heat Exchanger, the second heat exchanger, the 3rd heat exchange Device is cooled down, and the nitrogen in the second pipeline provides cold in the 3rd heat exchanger, the second heat exchanger, First Heat Exchanger；
Medium pressure nitrogen gas input pipe, medium pressure nitrogen input pipe is connected with medium pressure nitrogen gas source of the gas, medium pressure nitrogen input pipe Jing Cross and be connected with nitrogen wash column after First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger, medium pressure nitrogen gas input pipe passes through the first input pipe With the first pipeline connection, the first input pipe and the first pipeline connectivity points are located between nitrogen compressor unit and First Heat Exchanger, The first valve is provided with first input pipe.
2. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 1, it is characterised in that middle pressure Nitrogen input pipe by the second input pipe and the first pipeline connection, the second input pipe and the first pipeline connectivity points positioned at nitrogen wash column and Between 3rd heat exchanger, the second valve is provided with the second input pipe.
3. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 2, it is characterised in that middle pressure 3rd valve is installed, the 3rd valve is located between nitrogen wash column and the 3rd heat exchanger on nitrogen input pipe.
4. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 3, it is characterised in that nitrogen is washed The nitrogen hydrogen discharge and the 4th pipeline connection of tower, the 4th pipeline sequentially passes through the 3rd heat exchanger, the second heat exchanger, the first heat exchange Device.
5. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 4, it is characterised in that dehydrogenation The gas phase outlet of tower connects nitrogen wash column by the 3rd pipeline, and the 3rd pipeline passes through the 3rd heat exchanger, so that in the 3rd pipeline Gas phase is cooled.
6. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 5, it is characterised in that methane The liquefied natural gas outlet of tower is connected with LNG discharge pipe, LNG discharge pipe after the second heat exchanger with The entrance connection of first throttle valve, so that the liquefied natural gas in LNG discharge pipe is cooled by the second heat exchanger Cooled by first throttle valve throttling afterwards.
7. the system for producing syngas for synthetic ammonia and LNG using liquid nitrogen washing as claimed in claim 6, it is characterised in that also wrap The cryogen refrigeration system for providing cold is included, the cryogen refrigeration system includes refrigerant compressor unit and the second throttling Valve, the 3rd choke valve, the vapor phase refrigerant that refrigerant compressor unit is compressed by the 5th pipeline to second throttle conveying, gas Phase cold-producing medium returns refrigerant compressor unit after being lowered the temperature by second throttle throttling by the 7th pipeline, and the 5th pipeline is sequentially passed through Inlet communication after First Heat Exchanger, the tower bottom reboiler of methane tower, the second heat exchanger with second throttle, the 7th pipeline is successively Vapor phase refrigerant in the second heat exchanger and First Heat Exchanger, the 5th pipeline is in First Heat Exchanger, the second heat exchanger, methane Cool down in the tower bottom reboiler of tower, the vapor phase refrigerant in the 7th pipeline provides cold in the second heat exchanger, First Heat Exchanger, The liquid phase refrigerant that refrigerant compressor unit is compressed by the 6th pipeline to the conveying of the 3rd choke valve, the 3rd choke valve and the 7th Pipeline connection, liquid phase refrigerant is throttled by the 3rd choke valve and passes through the 7th pipeline return refrigerant compressor unit after lowering the temperature, and the 6th Pipeline is through First Heat Exchanger.
CN201611113494.XA 2016-12-07 2016-12-07 System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG Active CN106642988B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201611113494.XA CN106642988B (en) 2016-12-07 2016-12-07 System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201611113494.XA CN106642988B (en) 2016-12-07 2016-12-07 System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG

Publications (2)

Publication Number Publication Date
CN106642988A true CN106642988A (en) 2017-05-10
CN106642988B CN106642988B (en) 2022-07-05

Family

ID=58819899

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201611113494.XA Active CN106642988B (en) 2016-12-07 2016-12-07 System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG

Country Status (1)

Country Link
CN (1) CN106642988B (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109439368A (en) * 2018-10-11 2019-03-08 中国五环工程有限公司 The production treatment process of hydrocarbon-rich synthesis gas
CN111536758A (en) * 2020-04-29 2020-08-14 中科瑞奥能源科技股份有限公司 Coupling system and method for liquid nitrogen washing and cryogenic separation
CN114061265A (en) * 2020-08-04 2022-02-18 杭州中泰深冷技术股份有限公司 Device and method for large-scale combined production of synthetic ammonia and LNG (liquefied natural gas) by using coke-oven gas
CN114383382A (en) * 2021-12-10 2022-04-22 四川杰瑞恒日天然气工程有限公司 LNG preparation system and preparation method
CN114777420A (en) * 2022-03-31 2022-07-22 中科瑞奥能源科技股份有限公司 System and method for recovering argon and high-purity methane in hydrogen system

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8420666D0 (en) * 1983-08-25 1984-09-19 Toyo Engineering Corp Ammonia synthesis processes
CN202834682U (en) * 2012-04-20 2013-03-27 内蒙古鄂尔多斯联合化工有限公司 Structure of six-major-oil-station combining eight-major-unit
CN103043609A (en) * 2012-12-24 2013-04-17 李红凯 Liquid nitrogen washing device with function of producing natural gas
CN105066586A (en) * 2015-09-14 2015-11-18 成都深冷液化设备股份有限公司 Device and method for preparing synthetic ammonia raw material gas and LNG through liquid nitrogen washing
CN105135820A (en) * 2015-09-22 2015-12-09 北京中科瑞奥能源科技股份有限公司 Method and system for manufacturing LNG through gas containing air
CN205641671U (en) * 2016-05-03 2016-10-12 中化重庆涪陵化工有限公司 Synthetic ammonia refrigeration system
CN206291622U (en) * 2016-12-07 2017-06-30 中科瑞奥能源科技股份有限公司 The system that syngas for synthetic ammonia and LNG are produced using liquid nitrogen washing

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8420666D0 (en) * 1983-08-25 1984-09-19 Toyo Engineering Corp Ammonia synthesis processes
CN202834682U (en) * 2012-04-20 2013-03-27 内蒙古鄂尔多斯联合化工有限公司 Structure of six-major-oil-station combining eight-major-unit
CN103043609A (en) * 2012-12-24 2013-04-17 李红凯 Liquid nitrogen washing device with function of producing natural gas
CN105066586A (en) * 2015-09-14 2015-11-18 成都深冷液化设备股份有限公司 Device and method for preparing synthetic ammonia raw material gas and LNG through liquid nitrogen washing
CN105135820A (en) * 2015-09-22 2015-12-09 北京中科瑞奥能源科技股份有限公司 Method and system for manufacturing LNG through gas containing air
CN205641671U (en) * 2016-05-03 2016-10-12 中化重庆涪陵化工有限公司 Synthetic ammonia refrigeration system
CN206291622U (en) * 2016-12-07 2017-06-30 中科瑞奥能源科技股份有限公司 The system that syngas for synthetic ammonia and LNG are produced using liquid nitrogen washing

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109439368A (en) * 2018-10-11 2019-03-08 中国五环工程有限公司 The production treatment process of hydrocarbon-rich synthesis gas
CN109439368B (en) * 2018-10-11 2021-04-27 中国五环工程有限公司 Process for producing and treating hydrocarbon-rich synthetic gas
CN111536758A (en) * 2020-04-29 2020-08-14 中科瑞奥能源科技股份有限公司 Coupling system and method for liquid nitrogen washing and cryogenic separation
CN111536758B (en) * 2020-04-29 2024-01-30 中科瑞奥能源科技股份有限公司 Coupling system and method for liquid nitrogen washing and cryogenic separation
CN114061265A (en) * 2020-08-04 2022-02-18 杭州中泰深冷技术股份有限公司 Device and method for large-scale combined production of synthetic ammonia and LNG (liquefied natural gas) by using coke-oven gas
CN114383382A (en) * 2021-12-10 2022-04-22 四川杰瑞恒日天然气工程有限公司 LNG preparation system and preparation method
CN114777420A (en) * 2022-03-31 2022-07-22 中科瑞奥能源科技股份有限公司 System and method for recovering argon and high-purity methane in hydrogen system

Also Published As

Publication number Publication date
CN106642988B (en) 2022-07-05

Similar Documents

Publication Publication Date Title
CN106642988A (en) System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG
CN106979664B (en) Atmospheric carbon dioxide liquifying method
CN100588702C (en) The method and apparatus of the cut of Sweet natural gas of production liquefiable simultaneously and natural gas liquids
CN108458549B (en) System and method for extracting helium from natural gas and liquefying same
CN108592519A (en) Helium and liquefied apparatus and method are put forward from natural gas
CN104513680B (en) Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas
CN103175381B (en) Process for preparing LNG (liquefied natural gas) by low-concentration coal bed gas oxygen-containing cryogenic liquefaction
CN208332859U (en) Helium and liquefied system are proposed from natural gas
CN102408910B (en) Method and device for recovering light hydrocarbon through refrigeration using compound refrigerant and secondary dealkylation
CN104515361B (en) Method for producing liquid carbon dioxide
CN103697660B (en) The device and method of LNG and rich hydrogen production is produced from high methane gas
CN106369935A (en) Air separation system and method utilizing pressure energy of high-pressure natural gas pipeline network
CN203513622U (en) Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG)
CN105066586B (en) Device for preparing raw material gas for synthetic ammonia and L NG by liquid nitrogen washing and preparation method thereof
CN103175380B (en) Device for preparing LNG (liquefied natural gas) by low-concentration coal bed gas oxygen-containing cryogenic liquefaction
CN201532078U (en) Air separating system using liquefied natural gas cold energy
CN206291622U (en) The system that syngas for synthetic ammonia and LNG are produced using liquid nitrogen washing
CN206858511U (en) BOG recovery liquefaction removing Nitrogen in Natural Gases gas process systems
CN206073564U (en) The system for producing syngas for synthetic ammonia and liquefied natural gas
US3721098A (en) Cooling by mixing gaseous streams
CN206291621U (en) Pre-cooling type natural gas liquefaction device and system
CN106123487B (en) A kind of devices and methods therefor that pure neon is produced by ne-He mixture
CN107736435A (en) Process system and process method for carrying out deep-freezing and quick-freezing of seafood by using air
CN202246578U (en) Composite refrigerant refrigerated light secondary-dealkylation hydrocarbon recovering device
CN106871576A (en) Commercial syngas low temperature front-end demethanization method and system

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
CB03 Change of inventor or designer information
CB03 Change of inventor or designer information

Inventor after: Zhang Bin

Inventor after: Zhang Haijun

Inventor before: Xu Xiaoqin

Inventor before: Zhang Bin

Inventor before: Zhang Haijun

GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20240322

Address after: No. 9 Yongsheng Road, Yixing Economic and Technological Development Zone, Wuxi City, Jiangsu Province, 214200

Patentee after: Zhongkerio energy technology (Wuxi) Co.,Ltd.

Country or region after: China

Address before: 100094 Beijing Haidian District Fenghui Middle Road No. 7 New Material Pioneering Building 2 Floor 202

Patentee before: ZHONGKE RUIAO ENERGY TECHNOLOGY CO.,LTD.

Country or region before: China