CN109269223B - Purification of CO and CH 4 Cryogenic separation system and method - Google Patents

Purification of CO and CH 4 Cryogenic separation system and method Download PDF

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Publication number
CN109269223B
CN109269223B CN201811095074.2A CN201811095074A CN109269223B CN 109269223 B CN109269223 B CN 109269223B CN 201811095074 A CN201811095074 A CN 201811095074A CN 109269223 B CN109269223 B CN 109269223B
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tower
separation
heat exchanger
denitrification
evaporator
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CN109269223A (en
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曹卫华
文向南
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Sichuan Shudao Equipment Technology Co ltd
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Sichuan Shudao Equipment Technology Co ltd
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    • 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
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    • 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
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    • 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
    • F25J3/0252—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 hydrogen
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    • 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
    • F25J3/0257—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 nitrogen
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    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • 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
    • F25J2270/14—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
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide 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
    • F25J2270/42—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
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    • 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
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    • 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
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

The invention discloses a method for purifying CO and CH 4 Cryogenic separation system and methodThe method comprises a heat exchanger, a synthetic gas rectifying tower, a hydrogen stripping tower and CO/CH 4 The separation tower, the denitrification tower and the condensation evaporator are arranged at the bottom of the hydrogen stripping tower, and the bottom evaporator of the hydrogen stripping tower, CO/CH 4 The bottom of the separation tower is provided with CO/CH 4 The evaporator at the bottom of the separation tower is arranged on the CO/CH 4 The top of the separation tower, the condensing evaporator is arranged at the bottom of the denitrification tower, and each part forms a separation system to carry out heat exchange, rectification, dehydrogenation, methane purification, CO purification, product pressurization and other processes. The invention improves the recovery rate of methane by arranging the synthetic gas rectifying tower; the liquid methane is supercooled and throttled, so that the power consumption of the refrigeration compressor is reduced; setting condensing evaporator to make CO/CH 4 The separation tower and the denitrification tower are connected into a whole, so that the rectification power consumption is greatly reduced; the pressure of the CO product is increased by arranging the CO self-booster, so that the rectification power consumption is further reduced.

Description

Purification of CO and CH 4 Cryogenic separation system and method
Technical Field
The invention relates to the technical field of cryogenic gas separation, in particular to a method for purifying CO and CH 4 Is provided.
Background
CO is an important oxo feed gas from which almost all organic chemicals can be produced. The synthesis gas for preparing CO at present mainly comes from pressurized gasification of coal or steam conversion of natural gas/naphtha, and in addition to CO, hydrogen and methane, the synthesis gas prepared by coal gasification also contains a small amount of oxygen, nitrogen and argon, so that the purity requirements on raw material CO in the process of producing chemical products such as ethylene glycol, acetic acid and dimethyl diamide are very high (more than or equal to 98.5 percent), and therefore, the hydrogen, methane, oxygen, nitrogen, argon and the like in the synthesis gas need to be removed. The cryogenic separation technology has mature process, stable operation, large treatment capacity, high product purity and high yield, and is the preferred technology for CO separation at present.
Can effectively recycle and purify CH while purifying CO in a deep cooling way 4 The production of LNG (liquefied natural gas) or SNG (synthetic natural gas) reduces the venting of hydrocarbon gases and can also increase the economic benefit of the plant. Purification of CO and CH in cryogenic 4 The synthesis gas obtained is mainly H 2 And the CO content is dominant, and can be used as a raw material gas for hydrogen production or methanol synthesis.
U.S. Pat. No. 3,124, cryogenic Separation of Synthesis Gas and Chinese invention patent CN 104326472 B 'System for preparing CO by nitrogen cycle process' and CO/CH in method thereof 4 The separation tower and the denitrification tower both adopt conventional evaporators and condensers, so that the defects of high energy consumption and high investment exist, and the pressure of CO product gas is low.
Disclosure of Invention
In order to solve the problems, the invention provides a method for purifying CO and CH 4 Is provided.
Specifically, a method for purifying CO and CH 4 Comprises a heat exchanger, a synthetic gas rectifying tower, a hydrogen stripping tower and a CO/CH (carbon monoxide)/CH (hydrogen dioxide) 4 The separation tower, the denitrification tower and the condensation evaporator are arranged at the bottom of the hydrogen stripping tower, and the bottom evaporator of the hydrogen stripping tower, CO/CH 4 The bottom of the separation tower is provided with CO/CH 4 An evaporator at the bottom of the separation tower; the first runner I in the heat exchanger is communicated with the bottom inlet of the synthesis gas rectifying tower, a liquid phase outlet of the synthesis gas rectifying tower is provided with a first branch and a second branch, the first branch is connected with the middle inlet end of the hydrogen stripping tower through a first valve V1, the second branch is connected with the inlet end of a fourth runner IV in the heat exchanger, and the outlet end of the fourth runner IV is connected with the top inlet end of the hydrogen stripping tower through a second valve V2; the liquid phase outlet of the hydrogen stripping tower is provided with a first branch and a second branch, and the first branch is connected with CO/CH through a third valve V3 4 The middle upper inlet end of the separation tower is connected with the inlet end of a fifth flow passage V in the heat exchanger through a fourth valve V4, and the outlet end of the fifth flow passage V in the heat exchanger is connected with CO/CH 4 The middle lower inlet end of the separation tower is connected;
the denitrification tower is arranged on the CO/CH 4 The top of the separation tower, the condensing evaporator is arranged at the bottom of the denitrification tower, and the CO/CH 4 The liquid phase outlet of the separation tower is connected with an eighth runner VIII in the heat exchanger; CO/CH 4 The gas phase outlet of the separation tower is connected with the inlet of a condensing evaporator, and the outlet of the condensing evaporator is connected with CO/CH 4 The inlet of the separator at the top of the separation tower is connected with the CO/CH 4 Liquid phase outlet and CO/CH of separator at top of separation tower 4 The top inlet of the separation tower is connected with the CO/CH 4 Gas phase outlet of separator at top of separation tower and sixth flow passage VI in heat exchangerThe inlet end of the sixth runner VI is connected with the middle inlet end of the denitrification tower through a fifth valve V5; the liquid phase outlet of the denitrification tower is connected with the inlet end of the CO self-booster through a sixth valve V6, and the outlet end of the CO self-booster is connected with a tenth flow passage X in the heat exchanger.
Further, a gas phase outlet of the synthesis gas rectifying tower is connected with an inlet end of a condenser at the top of the synthesis gas rectifying tower, an outlet end of the condenser at the top of the synthesis gas rectifying tower is connected with an inlet of a separator at the top of the synthesis gas rectifying tower, a liquid phase outlet of the separator at the top of the synthesis gas rectifying tower is connected with an inlet at the top of the synthesis gas rectifying tower, and a gas phase outlet of the separator at the top of the synthesis gas rectifying tower is connected with a second flow passage II in the heat exchanger.
Further, the gas phase outlet of the hydrogen stripping tower is connected with a third flow passage III in the heat exchanger.
Further, two branches are arranged at the outlet end of an eighth runner VIII in the heat exchanger, the first branch is sent out in the form of LNG products through a seventh valve V7, and the second branch is connected with a ninth runner IX in the heat exchanger through an eighth valve V8.
Further, a gas phase outlet of the denitrification tower is connected with an inlet end of a tower top condenser of the denitrification tower, an outlet of the tower top condenser of the denitrification tower is connected with an inlet of a tower top separator of the denitrification tower, a liquid phase outlet of the tower top separator of the denitrification tower is connected with a top inlet of the denitrification tower, and a gas phase outlet of the tower top separator of the denitrification tower is connected with a seventh flow passage VII in the heat exchanger.
Further, the synthetic gas rectifying tower and the hydrogen stripping tower are arranged up and down.
Further, the bottom evaporator, the condensing evaporator and the CO/CH of the hydrogen stripping tower 4 The evaporator at the bottom of the separation tower can be an internal or external evaporator, or can be a dipping bath siphon type or membrane evaporation type.
Purification of CO and CH 4 Comprises the following steps:
s1: containing CO, hydrogen and CH 4 And a small amount of purified gas of oxygen, nitrogen and argon is cooled by cold fluid in a first runner I in a heat exchanger and partially cooled by cold fluidAfter condensation, the mixture enters a synthetic gas rectifying tower to carry out first rectification, a gas phase obtained by separation is methane-lean synthetic gas, and a liquid phase obtained by separation is divided into two branches: the first branch is depressurized through a first valve V1 and then directly sent to the middle part of the hydrogen stripping tower to participate in rectification, the second branch enters a fourth flow channel IV, and the liquid phase is supercooled to a certain temperature through a heat exchanger and then depressurized through a second valve V2 and then sent to the top part of the hydrogen stripping tower to be used as reflux liquid;
s2: the liquid phase obtained from the synthetic gas rectifying tower is subjected to rectification dehydrogenation by a hydrogen stripping tower, the separated gas phase is flash steam rich in hydrogen, and the hydrogen-poor liquid phase obtained from the bottom of the hydrogen stripping tower is divided into two branches: the first branch is decompressed by a third valve V3 and then directly sent into CO/CH 4 The middle upper part of the separation tower participates in rectification, the second branch is decompressed by a fourth valve V4 and then enters a fifth flow channel V, and the liquid phase is reheated to a certain temperature by a heat exchanger and then is sent into CO/CH 4 The middle lower part of the separation tower participates in rectification;
s3: the hydrogen-depleted liquid phase obtained from the hydrogen stripper is subjected to CO/CH 4 Rectifying and purifying in a separation tower, in CO/CH 4 Liquid methane is obtained at the bottom of the separation tower and is mixed with CO/CH 4 The CO-rich gas obtained from the top of the separation tower sequentially passes through a condensing evaporator and CO/CH 4 The pressure of the separator at the top of the separation tower, the channel VI in the heat exchanger and the fifth valve V5 is reduced, and then the reduced pressure is sent into a denitrification tower for continuous rectification;
S4：CO/CH 4 the CO-rich gas obtained at the top of the separation tower is subjected to rectification denitrification by the denitrification tower, the gas phase obtained by separation is nitrogen-rich gas, the CO liquid obtained at the bottom of the denitrification tower is sent into a CO self-booster to be gasified and pressurized after the flow rate is regulated by a sixth valve V6, and then enters a tenth flow passage X and is reheated to normal temperature by a heat exchanger to be used as a CO product out-of-limit region.
The synthetic gas rectifying tower can be any one or a combination of a plurality of condensing rectifying type, gas-liquid separation type, liquid CO washing type or liquid methane washing type.
The hydrogen stripping tower and CO/CH 4 The operating pressures of the separation tower and the denitrification tower are respectively 0.5-2.0 MPa.G, 0.4-1.5 MPa.G and 0.2-1.5 MPa.G.
The invention has the beneficial effects that: (1) The inventionThe methane recovery rate is improved by arranging a synthetic gas rectifying tower; (2) The invention adopts the liquid methane supercooling before throttling process, thereby reducing the power consumption of the refrigeration compressor; (3) The invention uses the condensing evaporator to cool CO/CH 4 The separation tower and the denitrification tower are connected into a whole, so that the rectification power consumption is greatly reduced; (4) According to the invention, the pressure of a CO product is increased by arranging the CO self-booster, so that the rectification power consumption is further reduced; (5) The invention has low energy consumption, simple operation and low investment, accords with the large trend of energy conservation and consumption reduction, and has good economic benefit.
Drawings
FIG. 1 is a schematic view of a first embodiment of the present invention;
FIG. 2 is a schematic diagram of a second embodiment of the present invention;
FIG. 3 is a schematic diagram of a third embodiment of the present invention;
FIG. 4 is a schematic diagram of a fourth embodiment of the present invention;
in the figure, a 1-heat exchanger, a 2-synthetic gas rectifying tower, a 3-synthetic gas rectifying tower top condenser, a 4-hydrogen stripping tower, a 5-hydrogen stripping tower bottom evaporator and a 6-CO/CH 4 Separation column, 7-denitrification column, 8-condensation evaporator, 9-CO/CH 4 Separator at top of separation column, condenser at top of 10-denitrification column, separator at top of 11-denitrification column, 12-CO/CH 4 The separation column bottom evaporator, a 13-CO self-booster, a 14-synthesis gas rectifying column top separator, a 15-low temperature separator, a 16-low temperature flash tank, an I-first flow passage, an II-second flow passage, a III-third flow passage, an IV-fourth flow passage, a V-fifth flow passage, a VI-sixth flow passage, a VII-seventh flow passage, a VIII-eighth flow passage, an IX-ninth flow passage, an X-tenth flow passage, a V1-first valve, a V2-second valve, a V3-third valve, a V4-fourth valve, a V5-fifth valve, a V6-sixth valve, a V7-seventh valve and a V8-eighth valve.
Detailed Description
For a clearer understanding of technical features, objects, and effects of the present invention, a specific embodiment of the present invention will be described with reference to the accompanying drawings.
Example 1
As shown in FIG. 1, a method for purifying CO and CH 4 Is divided into (1) by deep coolingThe separation system comprises a heat exchanger 1, a synthetic gas rectifying tower 2, a synthetic gas rectifying tower top condenser 3, a hydrogen stripping tower 4, a hydrogen stripping tower bottom evaporator 5 and CO/CH 4 Separation column 6, denitrification column 7, condensation evaporator 8, CO/CH 4 A separation tower top separator 9, a denitrification tower top condenser 10, a denitrification tower top separator 11 and CO/CH 4 A separation column bottom evaporator 12, a CO self-booster 13 and a synthesis gas rectifying column top separator 14; the heat exchanger 1 is internally provided with a first flow passage I, a second flow passage II, a third flow passage III, a fourth flow passage IV, a fifth flow passage V, a sixth flow passage VI, a seventh flow passage VII, an eighth flow passage VIII, a ninth flow passage IX and a tenth flow passage X; the synthesis gas rectifying tower top condenser 3 is internally provided with a runner A and a runner B, the denitrification tower top condenser 10 is internally provided with a runner C and a runner D, the CO self-booster 13 is internally provided with a runner E and a runner F, the hydrogen stripping tower bottom evaporator 5 is arranged in the hydrogen stripping tower 4 and is positioned at the bottom thereof, and the CO/CH is provided with a nitrogen removal device 4 The evaporator 12 at the bottom of the separation tower is arranged at the CO/CH 4 Within and at the bottom of the separation column 6. The condensing evaporator 8 is connected with CO/CH 4 Between the separation column 6 and the denitrification column 7, specifically, the denitrification column 7 is provided in CO/CH 4 The top of the separation tower 6, and the condensing evaporator 8 is arranged at the bottom of the denitrification tower 7. The outlet end of a first flow passage I in the heat exchanger 1 is connected with the inlet of the bottom of the synthetic gas rectifying tower 2, the gas phase outlet of the synthetic gas rectifying tower 2 is connected with the inlet end of a flow passage A in a condenser 3 of the top of the synthetic gas rectifying tower, the outlet of the flow passage A in the condenser 3 of the top of the synthetic gas rectifying tower is connected with the inlet of a separator 14 on the top of the synthetic gas rectifying tower, the liquid phase outlet of the separator 14 on the top of the synthetic gas rectifying tower is connected with the inlet end of a second flow passage II in the heat exchanger 1, the liquid phase outlet of the synthetic gas rectifying tower 2 is connected with two branches, the first branch is connected with the middle inlet end of a hydrogen stripping tower 4 through a first valve V1, the second branch is connected with the inlet end of a fourth flow passage IV in the heat exchanger 1, and the outlet end of the fourth flow passage IV in the heat exchanger 1 is connected with the top inlet end of the hydrogen stripping tower 4 through a second valve V2;
in this embodiment, the gas phase outlet of the hydrogen stripper 4 is connected to the third part of the heat exchanger 1The inlet end of the flow channel III is connected with a liquid phase outlet of the hydrogen stripping tower 4, and two branches are connected with the liquid phase outlet of the hydrogen stripping tower 4, wherein the first branch is connected with CO/CH through a third valve V3 4 The middle upper inlet end of the separation tower 6 is connected with the inlet end of a fifth flow passage V in the heat exchanger 1 through a fourth valve V4, and the outlet end of the fifth flow passage V in the heat exchanger 1 is connected with CO/CH 4 The middle lower inlet end of the separation column 6 is connected.
The CO/CH 4 The liquid phase outlet of the separation tower 6 is connected with the inlet end of the eighth runner VIII in the heat exchanger 1, the outlet end of the eighth runner VIII in the heat exchanger 1 is divided into two branches, the first branch is sent out in the form of LNG products through a seventh valve V7, and the second branch is connected with the inlet end of the ninth runner IX in the heat exchanger 1 through an eighth valve V8, and CO/CH is realized 4 The gas phase outlet of the separation tower 6 is connected with the inlet of a condensing evaporator 8, and the outlet of the condensing evaporator 8 is connected with CO/CH 4 The inlet of the separator 9 at the top of the separation column is connected with CO/CH 4 Liquid phase outlet of separator 9 at top of separation column and CO/CH 4 The top inlet of the separation column 6 is connected with CO/CH 4 The gas phase outlet of the separator 9 at the top of the separation tower is connected with the inlet end of a sixth flow passage VI in the heat exchanger 1, and the outlet end of the sixth flow passage VI in the heat exchanger 1 is connected with the middle inlet end of the denitrification tower 7 through a fifth valve V5.
In this embodiment, the liquid phase outlet of the denitrification tower 7 is connected to the inlet end of the flow channel E in the CO self-booster 13 through the sixth valve V6, the outlet end of the flow channel E in the CO self-booster 13 is connected to the inlet end of the tenth flow channel X in the heat exchanger 1, the gas phase outlet of the denitrification tower 7 is connected to the inlet end of the flow channel C in the denitrification tower top condenser 10, the outlet of the flow channel C in the denitrification tower top condenser 10 is connected to the inlet of the denitrification tower top separator 11, the liquid phase outlet of the denitrification tower top separator 11 is connected to the top inlet of the denitrification tower 7, and the gas phase outlet of the denitrification tower top separator 11 is connected to the inlet end of the seventh flow channel VII in the heat exchanger 1.
In this embodiment, the heat exchangers 1 are a plurality of heat exchangers connected in parallel and in series at the same time; the bottom evaporator 5, the condensing evaporator 8 and the CO/CH of the hydrogen stripping tower 4 The evaporator 12 at the bottom of the separation tower is a built-in dipping siphon type; the synthetic gas rectifying tower 2 and hydrogen gasThe lifting tower 4 is in an up-down coaxial arrangement structure; the installation position of the CO self-booster 13 is lower than that of the condensation evaporator 8, and the installation height difference is H.
Purifying CO and CH by using the system 4 Comprises the following steps:
s1, CO, hydrogen and CH 4 And a small amount of purified gas of oxygen, nitrogen and argon enters the heat exchanger 1 through the first flow passage I, the purified gas is cooled by cold fluid in the heat exchanger 1 and is partially condensed, then enters the synthetic gas rectifying tower 2 for first rectification, the separated gas phase is the synthetic gas lean in methane, the synthetic gas enters the second flow passage II and is reheated to normal temperature through the heat exchanger 1 and then enters the boundary area, and the separated process liquid phase in the synthetic gas rectifying tower 2 is divided into two branches: the first branch is depressurized through a first valve V1 and then directly sent to the middle part of the hydrogen stripping tower 4 to participate in rectification, the second branch enters a fourth flow passage IV, and the liquid phase is supercooled to a certain temperature through a heat exchanger 1 and then depressurized through a second valve V2 and then sent to the top of the hydrogen stripping tower 4 to be used as reflux liquid;
s2, through rectification dehydrogenation of the hydrogen stripping tower 4, flash gas rich in hydrogen is obtained at the top of the hydrogen stripping tower 4, enters a third flow passage III, is reheated to normal temperature by the heat exchanger 1 and then exits from a boundary zone, and hydrogen-lean liquid obtained at the bottom of the hydrogen stripping tower 4 is divided into two branches: the first branch is decompressed by a third valve V3 and then directly sent into CO/CH 4 The middle upper part of the separation tower 6 participates in rectification, the second branch is decompressed by a fourth valve V4 and then enters a fifth flow channel V, and the liquid phase is reheated to a certain temperature by the heat exchanger 1 and then is sent into CO/CH 4 The middle lower part of the separation tower 6 participates in rectification, the evaporator 5 at the bottom of the hydrogen stripping tower provides ascending evaporation gas for the hydrogen stripping tower 4, and a refrigerant is used as a heat source;
s3, through CO/CH 4 The liquid methane is obtained at the bottom of the separation tower 6 after rectification and purification, enters an eighth runner VIII, is supercooled to a certain temperature by a heat exchanger 1 and is divided into two branches: the first branch is depressurized by a seventh valve V7 and then is used as an LNG product outlet area, the second branch is depressurized by an eighth valve V8 and then enters a ninth runner IX, and is reheated to normal temperature by a heat exchanger 1 and then is used as an outlet area, and the LNG product outlet area is formed by CO/CH 4 Separation tower 6 roofThe CO-rich gas obtained by the part is sequentially sent to a condensation evaporator 8 and CO/CH 4 The pressure of a separator 9 at the top of the separation tower, a channel VI in the heat exchanger 1 and a fifth valve V5 is reduced, and then the reduced pressure is sent into a denitrification tower 7 for continuous rectification, and a condensing evaporator 8 is CO/CH 4 The separation tower 6 provides reflux liquid, and CO liquid at the bottom of the denitrification tower 7 is used as a cold source;
s4, through rectification denitrification of the denitrification tower 7, nitrogen-rich gas obtained at the top of the denitrification tower sequentially passes through a denitrification tower top condenser 10, a denitrification tower top separator 11 and a seventh flow passage VII, and is reheated to a normal temperature and then is discharged to a boundary region through a heat exchanger 1, CO liquid obtained at the bottom of the denitrification tower 7 is sent into a CO self-booster 13 to be gasified and pressurized after the flow rate of the CO liquid is regulated through a sixth valve V6, then enters a tenth flow passage X, is reheated to the normal temperature through the heat exchanger 1 and is discharged to the boundary region as CO products, a condensing evaporator 8 provides ascending evaporation gas for the denitrification tower 7, and CO/CH is adopted 4 The CO-rich gas at the top of the separation tower 6 is used as a heat source, the top condenser 10 of the denitrification tower provides reflux liquid for the denitrification tower 7, and a refrigerant is used as a cold source.
In the present embodiment, the refrigeration cycle may be any one or a combination of a nitrogen compression refrigeration cycle, a nitrogen compression expansion cycle, a CO compression refrigeration cycle, a CO compression expansion cycle, and a mixed refrigerant compression refrigeration cycle; the synthetic gas rectifying tower (2) can be any one or a combination of a plurality of condensation rectifying type, gas-liquid separation type, liquid CO washing type or liquid methane washing type; the hydrogen stripping tower 4 and CO/CH 4 The operating pressures of the separation tower 6 and the denitrification tower 7 are respectively 0.5-2.0 MPa.G, 0.4-1.5 MPa.G and 0.2-1.5 MPa.G.
Embodiment two: as shown in fig. 2, the present embodiment is different from the first embodiment in that: the low-temperature separator 15 is adopted to replace the synthetic gas rectifying tower 2, and is suitable for occasions with lower methane content in the purified gas, thereby further reducing energy consumption and investment.
Embodiment III: as shown in fig. 3, the present embodiment is different from the first embodiment in that: the use of a low temperature flash tank 16 in place of the hydrogen stripper 4 can reduce energy consumption and capital costs for some applications.
Embodiment four: as shown in fig. 4, the present embodiment is different from the first embodiment in that: the liquid phase outlet of the synthetic gas rectifying tower 2 is connected with two branches, the first branch is connected with the top inlet end of the hydrogen stripping tower 4 through a second valve V2, the second branch is connected with the inlet end of a fourth flow passage IV in the heat exchanger 1, and the outlet end of the fourth flow passage IV in the heat exchanger 1 is connected with the middle inlet end of the hydrogen stripping tower 4 through a first valve V1 for occasions with low recovery rate requirements on CO, so that the energy consumption and investment of the device can be reduced.

Claims (10)

1. Purification of CO and CH 4 Is characterized by comprising a heat exchanger (1), a synthetic gas rectifying tower (2), a hydrogen stripping tower (4) and CO/CH 4 The separation tower (6), the denitrification tower (7) and the condensation evaporator (8), the bottom of the hydrogen stripping tower (4) is provided with a hydrogen stripping tower bottom evaporator (5), and CO/CH 4 The bottom of the separation tower (6) is provided with CO/CH 4 A separation tower bottom evaporator (12); the first runner (I) in the heat exchanger (1) is communicated with the bottom inlet of the synthesis gas rectifying tower (2), a liquid phase outlet of the synthesis gas rectifying tower (2) is provided with a first branch and a second branch, the first branch is connected with the middle inlet end of the hydrogen stripping tower (4) through a first valve (V1), the second branch is connected with the inlet end of a fourth runner (IV) in the heat exchanger (1), and the outlet end of the fourth runner (IV) is connected with the top inlet end of the hydrogen stripping tower (4) through a second valve (V2); the liquid phase outlet of the hydrogen stripping tower (4) is provided with a first branch and a second branch, the first branch is connected with CO/CH through a third valve (V3) 4 The middle upper inlet end of the separation tower (6) is connected, the second branch is connected with the inlet end of a fifth flow passage (V) in the heat exchanger (1) through a fourth valve (V4), and the outlet end of the fifth flow passage (V) in the heat exchanger (1) is connected with CO/CH 4 The middle lower inlet end of the separation tower (6) is connected;
the denitrification tower (7) is arranged on the CO/CH 4 The top of the separation tower (6), the condensing evaporator (8) is arranged at the bottom of the denitrification tower (7), and the CO/CH 4 The liquid phase outlet of the separation tower (6) is connected with an eighth runner (VIII) in the heat exchanger (1); CO/CH 4 The gas phase outlet of the separation tower (6) is connected with the inlet of the condensing evaporator (8), and the condensingThe outlet of the evaporator (8) and the CO/CH 4 The inlet of the separator (9) at the top of the separation tower is connected with CO/CH 4 Liquid phase outlet and CO/CH of separator (9) at top of separation tower 4 The top inlet of the separation tower (6) is connected with the CO/CH 4 The gas phase outlet of the separator (9) at the top of the separation tower is connected with the inlet end of a sixth flow passage (VI) in the heat exchanger (1), and the outlet end of the sixth flow passage (VI) is connected with the middle inlet end of the denitrification tower (7) through a fifth valve (V5); the liquid phase outlet of the denitrification tower (7) is connected with the inlet end of the CO self-booster (13) through a sixth valve (V6), and the outlet end of the CO self-booster (13) is connected with a tenth flow passage (X) in the heat exchanger (1).
2. A purification of CO, CH according to claim 1 4 The cryogenic separation system is characterized in that a gas phase outlet of the synthetic gas rectifying tower (2) is connected with an inlet end of a synthetic gas rectifying tower top condenser (3), an outlet end of the synthetic gas rectifying tower top condenser (3) is connected with an inlet of a synthetic gas rectifying tower top separator (14), a liquid phase outlet of the synthetic gas rectifying tower top separator (14) is connected with a top inlet of the synthetic gas rectifying tower (2), and a gas phase outlet of the synthetic gas rectifying tower top separator (14) is connected with a second flow channel (II) in the heat exchanger (1).
3. A purification of CO, CH according to claim 1 4 Is characterized in that the gas phase outlet of the hydrogen stripping tower (4) is connected with a third flow passage (III) in the heat exchanger (1).
4. A purification of CO, CH according to claim 1 4 The cryogenic separation system is characterized in that two branches are arranged at the outlet end of an eighth runner (VIII) in the heat exchanger (1), the first branch is sent out in the form of LNG products through a seventh valve (V7), and the second branch is connected with a ninth runner (IX) in the heat exchanger (1) through an eighth valve (V8).
5. A purification of CO, CH according to claim 1 4 The cryogenic separation system is characterized in that a gas phase outlet of the denitrification tower (7) is connected with an inlet end of a denitrification tower top condenser (10), an outlet of the denitrification tower top condenser (10) is connected with an inlet of a denitrification tower top separator (11), a liquid phase outlet of the denitrification tower top separator (11) is connected with a top inlet of the denitrification tower (7), and a gas phase outlet of the denitrification tower top separator (11) is connected with a seventh flow passage (VII) in the heat exchanger (1).
6. A purification of CO, CH according to claim 1 4 The cryogenic separation system is characterized in that the synthetic gas rectifying tower (2) and the hydrogen stripping tower (4) are arranged up and down.
7. A purification of CO, CH according to claim 1 4 Is characterized in that the bottom evaporator (5), the condensing evaporator (8) and the CO/CH of the hydrogen stripping tower 4 The evaporator (12) at the bottom of the separation tower can be an internal or external evaporator, or can be a dipping siphon type evaporator or a membrane evaporation type evaporator.
8. Purification of CO and CH 4 Is characterized by comprising the following steps:
s1: containing CO, hydrogen and CH 4 And a small amount of purified gas of oxygen, nitrogen and argon is cooled by cold fluid in a first runner (I) in a heat exchanger (1) and is partially condensed, and then enters a synthetic gas rectifying tower (2) to carry out primary rectification, the separated gas phase is methane-lean synthetic gas, and the obtained liquid phase is divided into two branches: the first branch is directly sent to the middle part of the hydrogen stripping tower (4) to participate in rectification after being depressurized by a first valve (V1), the second branch enters a fourth flow channel (IV), and the liquid phase is supercooled to a certain temperature by a heat exchanger (1) and then is sent to the top of the hydrogen stripping tower (4) to be used as reflux after being depressurized by a second valve (V2);
s2: the liquid phase obtained by the synthetic gas rectifying tower (2) passes through a hydrogen stripping tower(4) The separated gas phase is flash steam rich in hydrogen, and the hydrogen-lean liquid phase obtained at the bottom of the hydrogen stripping tower (4) is divided into two branches: the first branch is decompressed by a third valve (V3) and then directly fed into CO/CH 4 The middle upper part of the separation tower (6) participates in rectification, the second branch is decompressed by a fourth valve (V4) and then enters a fifth flow passage (V), and the liquid phase is reheated to a certain temperature by a heat exchanger (1) and then is sent into CO/CH 4 The middle lower part of the separation tower (6) participates in rectification;
s3: the hydrogen-depleted liquid phase obtained from the hydrogen stripping column (4) is subjected to CO/CH 4 The separation tower (6) is used for rectification and purification, and CO/CH 4 The liquid methane is obtained at the bottom of the separation tower (6) and is mixed with CO/CH 4 The CO-rich gas obtained at the top of the separation tower (6) sequentially passes through a condensation evaporator (8) and CO/CH 4 The separator (9) at the top of the separation tower, a channel VI in the heat exchanger (1) and a fifth valve (V5) are decompressed and then sent into a denitrification tower (7) for continuous rectification;
S4：CO/CH 4 the CO-rich gas obtained at the top of the separation tower (6) is subjected to rectification denitrification by the denitrification tower (7), the gas phase obtained by separation is nitrogen-rich gas, the CO liquid obtained at the bottom of the denitrification tower (7) is sent into the CO self-booster (13) for gasification and pressurization after the flow rate is regulated by the sixth valve (V6), and then enters the tenth flow passage (X) and is reheated to normal temperature by the heat exchanger (1) to be used as a CO product outlet area.
9. A purification of CO, CH according to claim 8 4 The cryogenic separation method is characterized in that the synthetic gas rectifying tower (2) can be any one or more of condensation rectifying type, gas-liquid separation type, liquid CO washing type or liquid methane washing type.
10. A purification of CO, CH according to claim 8 4 Is characterized in that the hydrogen stripping tower (4) and CO/CH are adopted 4 The operating pressures of the separation tower (6) and the denitrification tower (7) are respectively 0.5-2.0 MPa. G, 0.4-1.5 MPa. G and 0.2-1.5 MPa. G.
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CN107473223A (en) * 2017-08-15 2017-12-15 成都深冷液化设备股份有限公司 A kind of CO cryogenic separation system and method using nitrogen cycle
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CN205784230U (en) * 2016-05-27 2016-12-07 开封空分集团有限公司 High purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane
CN107328166A (en) * 2017-07-27 2017-11-07 成都深冷液化设备股份有限公司 One kind uses bicirculating CO cryogenic separations system and its separation method
CN107367127A (en) * 2017-08-15 2017-11-21 成都深冷液化设备股份有限公司 A kind of cryogenic separation CO, H2Nitrogen cycle methane wash system and method
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