CN109439368B - Process for producing and treating hydrocarbon-rich synthetic gas - Google Patents

Process for producing and treating hydrocarbon-rich synthetic gas Download PDF

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CN109439368B
CN109439368B CN201811183731.9A CN201811183731A CN109439368B CN 109439368 B CN109439368 B CN 109439368B CN 201811183731 A CN201811183731 A CN 201811183731A CN 109439368 B CN109439368 B CN 109439368B
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gas
tower
heat exchanger
main heat
sent
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CN109439368A (en
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孔秋生
胡冠峰
李繁荣
肖敦峰
胡四斌
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China Wuhuan Engineering Co Ltd
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China Wuhuan Engineering 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/041—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/043—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by fractional condensation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
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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
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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
    • F25J3/0238—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 2 carbon atoms or more
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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
    • 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
    • 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
    • F25J3/0257—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
    • 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
    • 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
    • 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
    • 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Abstract

The invention discloses a production treatment process of hydrocarbon-rich synthetic gas, which solves the problems of long flow path and high investment of the existing hydrocarbon-rich synthetic gas, and the technical proposal is that the hydrocarbon-rich synthetic gas is firstly cooled by a 1# main heat exchanger and then sent into a heavy hydrocarbon separator for gas-liquid separation, heavy hydrocarbon in a liquid phase is separated out, the gas is discharged from the top of the heavy hydrocarbon separator, a tower bottom reboiler sent into a methane rectifying tower provides heat for the methane rectifying tower and then enters a tower bottom reboiler of the gas stripping tower for providing heat for the gas stripping tower, and finally, the gas is secondarily cooled by a 2# main heat exchanger and then enters a condensing tower for condensation; and the gas phase at the top of the condensing tower is condensed by a condenser at the top of the condensing tower and is separated by a separator at the top of the condensing tower to obtain hydrogen-rich gas, and the hydrogen-rich gas is sequentially sent into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating and then sent out of a battery limit. The invention has simple process flow, low investment and operation cost, reduced heat loss and effective gas emission and prolonged service life of the system.

Description

Process for producing and treating hydrocarbon-rich synthetic gas
Technical Field
The invention relates to a production process of synthesis gas, in particular to a production treatment process of hydrocarbon-rich synthesis gas.
Background
At present, CO and hydrogen-rich gas in hydrocarbon-rich synthesis gas are generally separated out through a cryogenic separation process in the production process of ethylene glycol products by coal chemical enterprises and reach the specification required by an ethylene glycol device, the hydrogen-rich gas is purified and enters the ethylene glycol device through a PSA device after being separated out through cryogenic separation, and other hydrocarbon components are generally used as tail gas to be sent to a fuel gas pipe network. And for the hydrocarbon-rich synthetic gas with high hydrocarbon content, the hydrocarbon component is separated by arranging an LNG cold box to prepare commercial LNG or SNG.
If the hydrocarbon-rich syngas is required to satisfy the requirement of the ethylene glycol synthesis plant and qualified SNG or LNG is also produced as a byproduct, the following process is usually adopted: firstly, an LNG cold box is adopted to separate hydrocarbon components to obtain LNG with qualified components, then a set of CO cryogenic separation device is added to further separate and purify CO-rich gas to prepare CO product gas meeting the requirements of an ethylene glycol device, and based on the process, a set of cryogenic device needs to be added, so that the problems of long process, high investment and operation cost, high energy consumption and large emission are caused.
Disclosure of Invention
The invention aims to solve the technical problems and provide a production treatment process of hydrocarbon-rich synthesis gas, which has the advantages of simple process flow, low investment and operation cost, heat loss reduction, effective gas emission reduction and system service life prolongation.
The technical scheme is as follows: cooling the hydrocarbon-rich synthesis gas by the # 1 main heat exchanger, sending the cooled hydrocarbon-rich synthesis gas into a heavy hydrocarbon separator for gas-liquid separation, separating out liquid-phase heavy hydrocarbon, discharging the gas from the top of the heavy hydrocarbon separator, sending the gas into a tower bottom reboiler of a methane rectifying tower to provide heat for the methane rectifying tower, then sending the gas into the tower bottom reboiler of the gas stripping tower to provide heat for the gas stripping tower, and finally, cooling the gas by the # 2 main heat exchanger for the second time, and then, sending the gas into a condensing tower for condensation; and the gas phase at the top of the condensing tower is condensed by a condenser at the top of the condensing tower and is separated by a separator at the top of the condensing tower to obtain hydrogen-rich gas, and the hydrogen-rich gas is sequentially sent into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating and then sent out of a battery limit.
And the tower bottom liquid of the condensing tower is fed into a stripping tower through a pressure reducing valve to extract residual hydrogen, and the hydrogen-containing flash steam at the top of the stripping tower is led out and then sequentially fed into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating and then can be taken as methanol synthesis gas to be sent out of a boundary region.
And feeding the tower bottom liquid at the bottom of the gas stripping tower into a methane rectifying tower for rectification and separation, wherein the tower bottom liquid separated by the methane rectifying tower is methane, and after being led out, the tower bottom liquid is sequentially fed into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating to obtain methane gas and then the methane gas is sent out of a boundary region.
And the gas led out from the top of the methane rectifying tower is condensed by a condenser at the top of the rectifying tower and is separated by a separator at the top of the rectifying tower to obtain CO gas, the CO gas is sent into a denitrification tower through a pressure reducing valve for further denitrification, the liquid at the bottom of the denitrification tower is qualified CO product gas, and the gas is led out and then sequentially sent into a 2# main heat exchanger and a 1# main heat exchanger for reheating to obtain methane gas, and the methane gas is sent out of a boundary area.
And the top gas of the denitrification tower is condensed by a condenser at the top of the denitrification tower and is separated by a separator at the top of the denitrification tower to obtain nitrogen-containing waste gas, and the nitrogen-containing waste gas is led out and then sequentially sent into a 2# main heat exchanger and a 1# main heat exchanger for reheating to obtain methane gas which is sent out of a boundary region.
In the treatment process, the condenser at the top of each tower provides cold energy by nitrogen, and the nitrogen which provides the cold energy returns to the nitrogen compressor for pressurization and reuse.
Has the advantages that:
(1) the hydrocarbon-rich synthesis gas production treatment process can synchronously produce the methanol synthesis gas, the CO product gas and the LNG, breaks through the separation task that the hydrocarbon-rich synthesis gas can be completed by a plurality of cold boxes, reduces the emission of effective gas, simplifies the flow, reduces the energy consumption and the investment cost, and can reduce the loss of cold energy and reduce the energy consumption by coupling the CO cold box and the LNG cold box.
(2) The nitrogen compressor is arranged to provide cold for the condenser at the top of each tower, and compared with other refrigeration processes, the nitrogen compressor process has the advantages of small occupied area, low investment and convenience in operation and maintenance.
(3) The denitrification tower and the methane rectifying tower are arranged, so that the specification of the CO product gas is ensured to meet the requirement of an ethylene glycol device, and the influence of the inert gas of the synthesis loop is greatly reduced after CH4, N2 and Ar are removed.
(4) Set up heavy hydrocarbon separator, the feed gas that gets into the tower through the heat exchanger cooling is below 160 ℃ below zero, and heavy hydrocarbon component can solidify under such low temperature, therefore feed gas cooling in-process, if there is heavy hydrocarbon component's existence, will take place to solidify in the heat exchanger, set up raw material gas separator, with liquid heavy hydrocarbon branch out, can effectively alleviate hydrocarbon component and solidify in the heat exchanger, block up the heat exchanger, extension system life.
Drawings
FIG. 1 is a process flow diagram of the present invention.
The system comprises a 1-1# main heat exchanger, a 2-2# main heat exchanger, a 3-stripper tower bottom reboiler, a 4-rectifier tower bottom reboiler, a 5-rectifier tower top condenser, a 6-denitrogenation tower top condenser, a 7-condenser tower top condenser, an 8-condensing tower, a 9-stripper tower, a 10-methane rectifying tower, an 11-denitrogenation tower, a 12-heavy hydrocarbon separator, a 13-condenser tower top separator, a 14-rectifier tower top separator, a 15-denitrogenation tower top separator and a 16-nitrogen compressor.
Detailed Description
Referring to fig. 1, the present invention is described in detail below with reference to a hydrocarbon-rich syngas from upstream coal gasification/coke oven gas purified by molecular sieves, the main components of the hydrocarbon-rich syngas comprising:
after the rich hydrocarbon is synthesized and is once cooled to 120-140 through the 1# main heat exchanger 1, the heavy hydrocarbon component is cooled to be a liquid phase, the heavy hydrocarbon enters the heavy hydrocarbon separator 12, the heavy hydrocarbon of the liquid phase is separated, the gas is sent into the reboiler 4 at the bottom of the methane rectifying tower to provide heat for the methane rectifying tower 10 and then enters the reboiler 3 at the bottom of the gas stripping tower to provide heat for the gas stripping tower 9, then the raw gas enters the 2# main heat exchanger 2 to be cooled for the second time to 160 ℃, the gas after being cooled again enters the condensing tower 8 to be subjected to rectification separation, the gas phase at the top of the condensing tower 8 is further condensed through the condenser 7 at the top of the condensing tower and is separated into condensate through the condenser 13 at the top of the condensing tower, the liquid enters the tower as reflux liquid, and the gas phase is hydrogen-rich gas and is sent out of.
The tower bottom liquid of the condensing tower 8 is sent into a stripping tower 9 through a pressure reducing valve, residual hydrogen in the tower bottom liquid is stripped out to be hydrogen-containing flash evaporation gas in the stripping tower 9 and is led out from the top of the tower, and the hydrogen-containing flash evaporation gas can be sent out of a boundary zone as methanol synthesis gas after being reheated by a main 2# main heat exchanger 2 and a 1# main heat exchanger 1;
tower bottoms (mainly N2 and CO) of the gas stripping tower 9 are sent to a methane rectifying tower 10 for rectification, the rectified gas is condensed and separated by a rectifying tower top condenser 5 and a rectifying tower top separator 14 to obtain condensate which flows back to the tower, and the gas phase is sent to a denitrification tower 11; the tower bottom liquid at the tower bottom of the methane rectifying tower 10 is qualified methane, can be directly led out as LNG, or is reheated by the No. 2 main heat exchanger 2 and the No. 1 main heat exchanger 1 to obtain methane gas which is sent out of a battery limit.
The top gas of the methane rectifying tower 10 is used for producing CO product gas, and in order to ensure that the CO product gas meets the synthesis requirement of ethylene glycol and further reduce the influence of inert gas on a synthesis device, a denitrification tower 11 is arranged for further purifying the CO product gas. Gas at the top of the methane rectifying tower 10 is sent into a denitrification tower 11 through a pressure reducing valve, a denitrification tower top condenser 6 and a denitrification tower top separator 15 are arranged at the top of the denitrification tower 11, a liquid phase of the separator provides reflux liquid for the denitrification tower 11, and a gas phase of nitrogen-containing waste gas is sent out of a boundary area after being reheated by a No. 2 main heat exchanger 2 and a No. 1 main heat exchanger 1; the bottom liquid of the denitrification tower 11 is qualified CO product gas, and is sent out of a boundary area after being reheated by the No. 2 main heat exchanger 2 and the No. 1 main heat exchanger 1.
All the overhead condensers in the process are supplied with cold energy by nitrogen, and the nitrogen which is supplied with the cold energy is returned to a nitrogen compressor (K201) for pressurization and recycling.
The indexes of various gases obtained after the treatment of the invention are as follows:
(1) CO product gas
Item Specification of
CO，v％≥ 99
H2，ppm(v)≤ 100
Cl，ppm(v)≤ 0.01
CH4，ppm(v)≤ 100
O2，ppm(v)≤ 60
CO2，pmm(v)≤ 5
As，ppm(v)≤ 0.1
Water content, v% is less than or equal to 0.01
Total sulfur, ppm (v) less than or equal to 0.1
(2) The methane gas/LNG product meets the current national standards or general indicators.
(3) The hydrogen-rich gas meets the requirement of a methanol synthesis raw material gas that the H2/CO ratio is 2.2-3.

Claims (3)

1. A production treatment process of hydrocarbon-rich synthetic gas is characterized in that the hydrocarbon-rich synthetic gas is cooled by a 1# main heat exchanger and then sent to a heavy hydrocarbon separator for gas-liquid separation, liquid-phase heavy hydrocarbon is separated, gas is discharged from the top of the heavy hydrocarbon separator, a tower bottom reboiler sent to a methane rectifying tower provides heat for the methane rectifying tower and then enters a tower bottom reboiler of a stripper for providing heat for the stripper, and finally, the gas is cooled by a 2# main heat exchanger and then enters a condensing tower for condensation; the gas phase at the top of the condensing tower is condensed by a condenser at the top of the condensing tower and is separated by a separator at the top of the condensing tower to obtain hydrogen-rich gas, and the hydrogen-rich gas is sequentially sent into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating and then sent out of a battery limit zone;
the tower bottom liquid of the condensing tower is fed into a stripping tower through a pressure reducing valve to extract residual hydrogen, and hydrogen-containing flash steam at the top of the stripping tower is led out and then sequentially fed into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating and then can be taken as methanol synthesis gas to be sent out of a boundary region;
feeding the tower bottom liquid at the bottom of the gas stripping tower into a methane rectifying tower for rectification and separation, leading out methane which is the tower bottom liquid separated by the methane rectifying tower, and sequentially feeding the methane into a No. 2 main heat exchanger and a No. 1 main heat exchanger for reheating to obtain methane gas which is sent out of a boundary region;
and the gas led out from the top of the methane rectifying tower is condensed by a condenser at the top of the methane rectifying tower and is separated by a separator at the top of the rectifying tower to obtain CO gas, the CO gas is sent into a denitrification tower through a pressure reducing valve for further denitrification, the liquid at the bottom of the denitrification tower is qualified CO product gas, and the gas is led out and then sequentially sent into a 2# main heat exchanger and a 1# main heat exchanger for reheating to obtain CO product gas which is sent out of a boundary area.
2. The process for producing and treating a hydrocarbon-rich synthesis gas according to claim 1, wherein the nitrogen-containing waste gas is obtained by condensing the top gas of the denitrification tower by a condenser at the top of the denitrification tower and separating the top gas by a separator at the top of the denitrification tower, and the nitrogen-containing waste gas is led out and then sequentially sent to the # 2 main heat exchanger and the # 1 main heat exchanger for reheating to obtain the methane gas which is sent out of the battery limits.
3. The process for the production and treatment of a hydrocarbon-rich synthesis gas according to claim 1 or 2, wherein the condenser at the top of each column is provided with refrigeration by nitrogen, and the refrigeration-completed nitrogen is returned to the nitrogen compressor for pressure reuse.
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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202297535U (en) * 2011-09-30 2012-07-04 新地能源工程技术有限公司 Device for removing hydrogen, nitrogen and carbon monoxide from high methane gas and producing liquefied natural gas
CN106642988A (en) * 2016-12-07 2017-05-10 中科瑞奥能源科技股份有限公司 System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG
CN108474614A (en) * 2015-10-30 2018-08-31 乔治洛德方法研究和开发液化空气有限公司 Method and apparatus for separating synthetic gas

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202297535U (en) * 2011-09-30 2012-07-04 新地能源工程技术有限公司 Device for removing hydrogen, nitrogen and carbon monoxide from high methane gas and producing liquefied natural gas
CN108474614A (en) * 2015-10-30 2018-08-31 乔治洛德方法研究和开发液化空气有限公司 Method and apparatus for separating synthetic gas
CN106642988A (en) * 2016-12-07 2017-05-10 中科瑞奥能源科技股份有限公司 System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG

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