CN110553463A - Energy-saving optimization system and process of HyCO cryogenic separation device - Google Patents

Energy-saving optimization system and process of HyCO cryogenic separation device Download PDF

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Publication number
CN110553463A
CN110553463A CN201910806372.6A CN201910806372A CN110553463A CN 110553463 A CN110553463 A CN 110553463A CN 201910806372 A CN201910806372 A CN 201910806372A CN 110553463 A CN110553463 A CN 110553463A
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CN
China
Prior art keywords
heat exchanger
tower
denitrification tower
denitrification
gas
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CN201910806372.6A
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Chinese (zh)
Inventor
章有虎
李元海
杨巧玉
李斌
乔玉珍
刘苗苗
朱明明
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HANGZHOU ZHONGTAI CRYOGENIC TECHNOLOGY Co Ltd
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HANGZHOU ZHONGTAI CRYOGENIC TECHNOLOGY Co Ltd
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Priority to CN201910806372.6A priority Critical patent/CN110553463A/en
Publication of CN110553463A publication Critical patent/CN110553463A/en
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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
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—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
    • 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
    • F25J3/0252—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
    • F25J2200/72—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal 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
    • F25J2270/12—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
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide refrigeration cycle
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Abstract

The invention discloses an energy-saving optimization system and process of a HyCO cryogenic separation device, and belongs to the field of chemical processes. The HyCO cryogenic separation device comprises a CO compressor, a denitrification tower top condenser, a denitrification tower bottom process liquid throttling valve, a demethanizer, a second heat exchanger, a circulating CO throttling valve, a stripping tower bottom-to-denitrification tower throttling valve, a hydrogen-rich flash tank-to-stripping tower process liquid throttling valve, a stripping tower, a first heat exchanger and a washing liquid throttling valve; the process flow of the device throttles the process liquid after the process liquid exits the denitrification tower and sends the process liquid to the top of the denitrification tower to serve as a cold source at the top of the denitrification tower to enter a condenser at the top of the denitrification tower, so that the requirement of the device on a circulating medium is reduced, and the energy consumption of the device is reduced. The process medium is vaporized and then sent to the bottom of the demethanizer while being used as a cold source, so that the requirement of a reboiler at the bottom of the demethanizer on the circulating medium is reduced, and the energy consumption of the device is reduced.

Description

Energy-saving optimization system and process of HyCO cryogenic separation device
Technical Field
The invention relates to an energy-saving optimization system of a HyCO cryogenic separation device and a process thereof, in particular to an optimization process flow which uses process liquid after throttling treatment as a nitrogen removal tower top cold source.
Background
HyCO is mainly a mixed gas of hydrogen and carbon monoxide, a HyCO separation device is mainly used for separating different substances according to different boiling points of the different substances, generally one separation tank and two towers are used for separation, one tower is mainly used for removing H 2 dissolved in liquid CO, the other tower is used for removing CH 4, the two towers are used for separation, the purity of CO in a gas product is not high, and particularly when the N 2 component in the raw material is more, the purity of a CO product is seriously reduced, so that the product is unqualified.
The HyCO system comprises a liquid nitrogen tank, a synthetic gas separation device and a torch, wherein a circulating pipeline is arranged at the bottom of the liquid nitrogen tank, the outlet end of the pipeline is connected with a torch pipeline, liquid is discharged into the torch, and the synthetic gas separation device vaporizes low-temperature liquid-phase substances and guides the vaporized low-temperature liquid-phase substances into the torch to be combusted through an outlet pipeline. Because there are a large amount of low temperature liquid phase substances in the HyCO cryogenic separation device, so need a torch to discharge a large amount of cryogenic liquid, need vaporize at first then discharge the gaseousness into the torch and burn again, because there may be terminal gaseousness before advancing the torch and be difficult to get into the torch system, in order to ensure process safety, designed to sweep nitrogen gas and guaranteed to advance the torch pipeline can all get into the torch and burn.
Generally, when the HyCO cryogenic separation device adopts a three-tower process flow, dehydrogenation, denitrification and demethanization are sequentially carried out, wherein the process flow adopted in the process is that part of condensed process media passing through a first heat exchanger and a second heat exchanger are sent to a hydrogen-rich gas flash tank, hydrogen-rich gas is flashed out and sent to the second heat exchanger and a cooling tank after the first heat exchanger is reheated, and then liquid at the bottom of the hydrogen-rich gas flash tank is throttled by a throttle valve and sent to a stripping tower to remove residual hydrogen; the gas at the top of the tower is sent to a second heat exchanger and a first heat exchanger for rewarming and then is discharged from a cold box, and the liquid at the bottom of the tower is throttled and then is sent to a denitriding tower containing a circulating medium as a cold source to remove nitrogen; the nitrogen-rich gas at the top of the denitrification tower is reheated by the second heat exchanger and the first heat exchanger, then is discharged from the cold box, and the process liquid at the bottom of the denitrification tower is throttled and then is directly sent to a demethanizer containing a circulating medium to remove methane; and the methane-rich liquid at the bottom of the demethanizer is discharged out of the cold box after being subjected to rewarming by the second heat exchanger and the first heat exchanger, and the carbon monoxide product gas at the top of the demethanizer is sent to the heat exchanger and discharged out of the cold box after being subjected to rewarming.
In the general process flow, a circulating medium except process liquid is required to be used as a cold source in a denitrification tower, and meanwhile, the liquid at the bottom of a demethanizer is required to be vaporized by the external circulating medium;
disclosure of Invention
the invention aims to overcome the defects of the prior art and provides an energy-saving optimization system of a HyCO cryogenic separation device by using process liquid as a cold source and a process thereof.
An energy-saving optimization system of a HyCO cryogenic separation device is characterized by comprising a CO compressor, a denitrification tower top condenser, a denitrification tower bottom process liquid throttling valve, a demethanizer, a second heat exchanger, a circulating CO throttling valve, a stripping tower bottom to denitrification tower throttling valve, a hydrogen-rich flash tank to stripping tower process liquid throttling valve, a stripping tower, a first heat exchanger and a washing liquid throttling valve;
The system receives purified gas from upstream, a purified gas pipeline passes through the first heat exchanger and the second heat exchanger and then is connected with the hydrogen-rich gas flash tank, and the hydrogen-rich gas flash tank is used for separating hydrogen-rich gas; a purified gas pipeline from the hydrogen-rich gas flash tank is connected with a feed inlet of the stripping tower after passing through the hydrogen-rich gas flash tank to a process liquid throttling valve of the stripping tower; a flash steam flow is separated from a discharge port at the top of the stripping tower, and a discharge port at the bottom of the stripping tower is connected to a feed port of the denitrification tower after passing through a conveying pipeline from the bottom of the stripping tower to a throttle valve of the denitrification tower;
A nitrogen-rich stream is produced at a discharge port at the top of the denitrification tower and leaves the system after passing through a condenser at the top of the denitrification tower, a second heat exchanger and a first heat exchanger in sequence for heat exchange; a discharge port at the bottom of the denitrification tower is connected to a feed port of the demethanizer through a pipeline after passing through a process liquid throttle valve at the bottom of the denitrification tower and a condenser at the top of the denitrification tower, wherein a process fluid at the bottom of the denitrification tower is used as a cold source of the condenser at the top of the denitrification tower;
A discharge hole at the bottom of the demethanizer produces methane-rich gas, and a methane-rich gas stream leaves the system after passing through a second heat exchanger and a first heat exchanger for heat exchange; a discharge hole in the top of the demethanizer produces CO product gas, a CO product gas flow enters a circulating pipeline, and the circulating pipeline sequentially passes through a second heat exchanger, a first heat exchanger, a CO compressor, the first heat exchanger, a second heat exchanger and a circulating CO throttle valve and then enters the second heat exchanger again to form circulation; the circulating pipeline produces a pressurized CO product gas and a circulating CO medium from a CO compressor; the recycle CO medium portion is directed from the recycle line and through the wash liquor throttle line into the demethanizer.
the energy-saving optimized process system of the HyCO cryogenic separation device is characterized in that a hydrogen-rich gas flow stream separated by the hydrogen-rich gas flash tank leaves the system after passing through the second heat exchanger and the first heat exchanger.
the energy-saving optimization process of the HyCO cryogenic separation device of the system is characterized by comprising the following steps of:
1) The purified gas at the upstream is cooled by a first heat exchanger and a second heat exchanger and then is sent to a hydrogen-rich gas flash tank, and hydrogen-rich gas is separated;
2) The purified gas discharged from the hydrogen-rich gas flash tank passes through the hydrogen-rich gas flash tank to a process liquid throttling valve of the stripping tower and is sent to the stripping tower, the flash steam is separated out, and then the cooled gas is discharged from a cold box through a second heat exchanger and a first heat exchanger;
3) purified gas discharged from the stripping tower passes through the bottom of the stripping tower to a throttle valve of the denitrification tower and is sent to the denitrification tower, nitrogen-rich gas is separated out, and then the purified gas is discharged from a cold box through a second heat exchanger and a first heat exchanger; the bottom temperature of the denitrogenation tower is about-163 ℃, and the top temperature is about-164.5 ℃. As the pressure of the process liquid at the bottom of the denitrogenation tower is about 1MPaG, the pressure requirement of the product outlet cold box of the HyCO cryogenic separation device is about 0.7MPa, and the temperature of the process liquid at the bottom of the denitrogenation tower is reduced from minus 163 ℃ to minus 166.5 ℃ when the process liquid is throttled from 1.0MPa to 0.7MPa, the temperature requirement of a cold source at the top of the denitrogenation tower can be met. Therefore, the process liquid at the bottom of the denitrification tower passes through the process liquid throttle valve at the bottom of the denitrification tower and is sent to a condenser at the top of the denitrification tower to be used as a cold source, and the gasified process liquid is sent to a demethanizer;
4) After the gas discharged from the nitrogen removal tower top condenser is treated by a demethanizer, methane-rich gas is separated out, and then the gas is discharged from a cold box through a second heat exchanger and a first heat exchanger;
5) the CO product gas separated from the top of the demethanizer (5) enters a circulating pipeline, and the circulating pipeline produces pressurized CO product gas and circulating CO medium from a CO compressor (1);
6) the recycle CO medium fraction is led out of the recycle line and returned to the demethanizer (5) via a wash liquid throttle valve (13).
the invention makes up the defects of the common HyCO cryogenic separation device in the field of energy-saving optimization systems and processes thereof. By using the invention, the process liquid is used as a cold source of the condenser of the denitrification tower, so that great contribution is made to the environmental protection and energy consumption aspects of the whole process flow, the requirement of the condenser at the top of the denitrification tower on a circulating medium is reduced, and the requirement of the reboiler at the bottom of the demethanizer on the circulating medium is reduced, thereby optimizing the device flow, reducing the energy consumption of the device and saving the cost. The method is not only beneficial to production, but also meets the requirements of energy conservation and emission reduction in China.
drawings
FIG. 1 is an energy-saving optimization system of a HyCO cryogenic separation plant of the present invention;
FIG. 2 is a flow of the condensation of a denitrogenation column of an energy-saving optimization system of a HyCO cryogenic separation plant according to the present invention;
FIG. 3 is a demethanizer flow for an energy-efficient optimization system of a HyCO cryogenic separation plant of the present invention;
In the figure, a CO compressor 1, a denitrification tower top condenser 2, a denitrification tower 3, a denitrification tower bottom process liquid throttling valve 4, a demethanizer 5, a second heat exchanger 6, a circulating CO throttling valve 7, a stripping tower bottom to denitrification tower throttling valve 8, a hydrogen-rich flash tank 9, a hydrogen-rich flash tank to stripping tower process liquid throttling valve 10, a stripping tower 11, a first heat exchanger 12 and a washing liquid throttling valve 13 are arranged.
Detailed Description
as shown in fig. 1, an energy-saving optimization system of a HyCO cryogenic separation device comprises a CO compressor 1, a denitrification overhead condenser 2, a denitrification tower 3, a denitrification tower bottom process liquid throttling valve 4, a demethanizer 5, a second heat exchanger 6, a circulating CO throttling valve 7, a stripping tower bottom to denitrification tower throttling valve 8, a hydrogen-rich flash tank 9, a hydrogen-rich flash tank to stripping tower process liquid throttling valve 10, a stripping tower 11, a first heat exchanger 12 and a washing liquid throttling valve 13;
according to an embodiment of the invention, the system receives purified gas from upstream, the purified gas pipeline passes through the first heat exchanger 12 and the second heat exchanger 6 and is connected with the hydrogen-rich flash tank 9, and the hydrogen-rich flash tank is used for separating hydrogen-rich gas; a purified gas pipeline from the hydrogen-rich gas flash tank is connected with a feed inlet of a stripping tower 11 after passing through the hydrogen-rich gas flash tank to a stripping tower process liquid throttling valve 10; a flash steam flow is separated from a discharge port at the top of the stripping tower 11, and a discharge port at the bottom of the stripping tower is connected to a feed port of the denitrification tower 3 after passing through the bottom of the stripping tower to a denitrification tower throttle valve 8 through a conveying pipeline;
as shown in fig. 2 and 3, according to an embodiment of the present invention, a nitrogen-rich stream is produced at a discharge port at the top of the denitrification tower 3, and the nitrogen-rich stream leaves the system after passing through the denitrification tower top condenser 2, the second heat exchanger 6 and the first heat exchanger 12 for heat exchange in sequence; a discharge port at the bottom of the denitrification tower 3 is connected to a feed port of a demethanizer 5 through a pipeline after passing through a denitrification tower bottom process liquid throttling valve 4 and a denitrification tower top condenser 2, wherein the process fluid at the bottom of the denitrification tower 3 is used as a cold source of the denitrification tower top condenser 2;
a discharge hole at the bottom of the demethanizer 5 produces methane-rich gas, and a methane-rich gas stream leaves the system after heat exchange through a second heat exchanger 6 and a first heat exchanger 12; a discharge hole in the top of the demethanizer 5 produces CO product gas, a CO product gas flow enters a circulating pipeline, and the circulating pipeline sequentially passes through the second heat exchanger 6, the first heat exchanger 12, the CO compressor 1, the first heat exchanger 12, the second heat exchanger 6 and the circulating CO throttle valve 7 and then enters the second heat exchanger 6 again; the circulating pipeline produces pressurized CO product gas and circulating CO medium from the CO compressor 1; the recycle CO medium is piped to the demethanizer 5 through a scrubbing liquid throttle 13.
The energy-saving optimization process of the HyCO cryogenic separation device of the system is characterized by comprising the following steps of:
1) the purified gas at the upstream is sent to a hydrogen-rich gas flash tank 9 after being cooled by a first heat exchanger 12 and a second heat exchanger 6, and hydrogen-rich gas is separated;
2) Purified gas from the hydrogen-rich gas flash tank 9 passes through the hydrogen-rich gas flash tank to a process liquid throttling valve 10 of the stripping tower, is sent to the stripping tower 11, is separated into flash steam, and then is discharged out of a cold box through a second heat exchanger 6 and a first heat exchanger 12;
3) Purified gas from the stripping tower 11 passes through the bottom of the stripping tower to a denitrification tower throttle valve 8 and is sent to a denitrification tower 3, nitrogen-rich gas is separated out, and the purified gas passes through a second heat exchanger 6 and a first heat exchanger 12 and is discharged out of a cold box; the temperature of the bottom of the denitrification tower 3 is about-163 ℃, and the temperature of the top thereof is about-164.5 ℃. As the pressure of the process liquid discharged from the bottom of the denitrification tower 3 is about 1MPaG, the pressure requirement of the product discharged from the cold box of the HyCO cryogenic separation device is about 0.7MPa, and the temperature of the process liquid at the bottom of the denitrification tower 3 is reduced from-163 ℃ to-166.5 ℃ when the pressure is reduced from 1.0MPa to 0.7MPa, the temperature requirement of a cold source at the top of the denitrification tower 3 can be met. Therefore, the process liquid sent to the bottom of the denitrification tower 3 is sent to the top condenser 2 of the denitrification tower as a cold source after passing through the process liquid throttle valve 4 at the bottom of the denitrification tower, and is sent to the demethanizer 5 after being gasified;
4) after the gas out of the denitrification tower top condenser 2 is treated by a demethanizer 5, methane-rich gas is separated out, and then the gas is discharged out of a cold box through a second heat exchanger 6 and a first heat exchanger 12;
5) The CO product gas separated from the top of the demethanizer (5) enters a circulating pipeline, and the circulating pipeline produces pressurized CO product gas and circulating CO medium from a CO compressor (1);
6) The recycle CO medium fraction is led out of the recycle line and returned to the demethanizer (5) via a wash liquid throttle valve (13).
The process liquid is used as the cold source of the condenser of the denitrification tower, the temperature of the process liquid at the bottom of the denitrification tower 3 is reduced after throttling, and the temperature requirement of the cold source at the top of the denitrification tower 3 is met.

Claims (3)

1. An energy-saving optimization system of a HyCO cryogenic separation device is characterized by comprising a CO compressor (1), a denitrification tower top condenser (2), a denitrification tower (3), a denitrification tower bottom process liquid throttling valve (4), a demethanizer (5), a second heat exchanger (6), a circulating CO throttling valve (7), a stripping tower bottom to denitrification tower throttling valve (8), a hydrogen-rich flash tank (9), a hydrogen-rich flash tank to stripping tower process liquid throttling valve (10), a stripping tower (11), a first heat exchanger (12) and a washing liquid throttling valve (13);
The system receives purified gas from upstream, a purified gas pipeline passes through a first heat exchanger (12) and a second heat exchanger (6) and then is connected with a hydrogen-rich gas flash tank (9), and the hydrogen-rich gas flash tank is used for separating hydrogen-rich gas; a purified gas pipeline from the hydrogen-rich gas flash tank is connected with a feed inlet of the stripping tower (11) after passing through the hydrogen-rich gas flash tank to a process liquid throttling valve (10) of the stripping tower; a discharge port at the top of the stripping tower (11) separates a flash steam flow, and a discharge port at the bottom of the stripping tower is connected to a feed port of the denitrification tower (3) after passing through the bottom of the stripping tower to a denitrification tower throttle valve (8) through a conveying pipeline;
a discharge port at the top of the denitrification tower (3) produces a nitrogen-rich stream, and the nitrogen-rich stream leaves the system after passing through a denitrification tower top condenser (2), a second heat exchanger (6) and a first heat exchanger (12) for heat exchange in sequence; a discharge port at the bottom of the denitrification tower (3) is connected to a feed port of the demethanizer (5) through a pipeline after passing through a denitrification tower bottom process liquid throttle valve (4) and a denitrification tower top condenser (2), wherein a process fluid at the bottom of the denitrification tower (3) is used as a cold source of the denitrification tower top condenser (2);
A discharge hole at the bottom of the demethanizer (5) produces methane-rich gas, and a methane-rich gas stream leaves the system after heat exchange through a second heat exchanger (6) and a first heat exchanger (12); a discharge hole in the top of the demethanizer (5) produces CO product gas, a CO product gas flow enters a circulating pipeline, and the circulating pipeline sequentially passes through a second heat exchanger (6), a first heat exchanger (12), a CO compressor (1), the first heat exchanger (12), the second heat exchanger (6) and a circulating CO throttle valve (7) and then enters the second heat exchanger (6) again to form circulation; the circulating pipeline produces a pressurized CO product gas and a circulating CO medium from the CO compressor (1); the recycle CO medium portion is directed from the recycle line and through the scrubbing liquid throttle valve (13) line into the demethanizer (5).
2. The energy-saving optimization system of the HyCO cryogenic separation device according to claim 1, characterized in that a hydrogen-rich gas flow stream separated from the hydrogen-rich gas flash tank leaves the system after passing through the second heat exchanger (6) and the first heat exchanger (12).
3. an energy-saving optimization process of a HyCO cryogenic separation device of the system according to claim 1, characterized by comprising the steps of:
1) the purified gas at the upstream is sent to a hydrogen-rich gas flash tank (9) after being cooled by a first heat exchanger (12) and a second heat exchanger (6), and hydrogen-rich gas is separated;
2) Purified gas discharged from the hydrogen-rich flash tank (9) passes through the hydrogen-rich flash tank to a process liquid throttling valve (10) of the stripping tower, is sent to the stripping tower (11), is separated into flash steam, and is discharged from a cold box through a second heat exchanger (6) and a first heat exchanger (12);
3) purified gas discharged from the stripping tower (11) passes through the bottom of the stripping tower to a denitrification tower throttle valve (8), is sent to a denitrification tower (3), is separated to obtain nitrogen-rich gas, and is discharged from a cold box through a second heat exchanger (6) and a first heat exchanger (12); the bottom temperature of the denitrification tower (3) is-163 ℃, and the top temperature is-164.5 ℃; as the pressure of the process liquid discharged from the bottom of the denitrification tower (3) is 1MPaG, the pressure requirement of a product discharge cold box of the HyCO cryogenic separation device is 0.7MPa, and the temperature of the process liquid at the bottom of the denitrification tower (3) is reduced from-163 ℃ to-166.5 ℃ when the process liquid is throttled from 1.0MPa to 0.7MPa, the temperature requirement of a cold source at the top of the denitrification tower (3) is met, the process liquid at the bottom of the denitrification tower is sent to a denitrification tower top condenser (2) as the cold source after passing through a denitrification tower bottom process liquid throttle valve (4), and is sent to the demethanizer (5) after being gasified;
4) after the gas out of the denitrification tower top condenser (2) is treated by a demethanizer (5), methane-rich gas is separated out, and then the gas is discharged out of a cold box through a second heat exchanger (6) and a first heat exchanger (12);
5) The CO product gas separated from the top of the demethanizer (5) enters a circulating pipeline, and the circulating pipeline produces pressurized CO product gas and circulating CO medium from a CO compressor (1);
6) the recycle CO medium fraction is led out of the recycle line and returned to the demethanizer (5) via a wash liquid throttle valve (13).
CN201910806372.6A 2019-08-29 2019-08-29 Energy-saving optimization system and process of HyCO cryogenic separation device Pending CN110553463A (en)

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