CN210346071U - Cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification - Google Patents

Cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification Download PDF

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Publication number
CN210346071U
CN210346071U CN201921061939.3U CN201921061939U CN210346071U CN 210346071 U CN210346071 U CN 210346071U CN 201921061939 U CN201921061939 U CN 201921061939U CN 210346071 U CN210346071 U CN 210346071U
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pipeline
flow channel
heat exchanger
communicated
main plate
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郝雅博
秦燕
梁维好
徐志明
周冬根
陈少伟
涂为媛
崔超岭
卫光普
郑蕴涵
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Hang Yang Group Co ltd
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Hangzhou Hangyang 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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J2200/40—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2270/24—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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Abstract

The utility model discloses an integrated cryogenic separation device that takes off ethylene, dehydrogenation, demethanization, denitrogenation, including molecular sieve absorption unit, cryogenic separation device cold box unit, CO cyclic compressor unit, molecular sieve absorption unit, intercommunication between cryogenic separation device cold box unit, intercommunication between CO cyclic compressor unit, mist send to molecular sieve absorption unit and purify, the gas after the purification gets into cryogenic separation device cold box unit and separates, CO cyclic compressor unit provides pressure for cryogenic separation device cold box unit, has the deethylenizationThe function is that the obtained high-purity CO product gas can be separated, the purity can reach more than 99 percent, and H in the gas2And CH4The content is less than 50ppm, the recovery rate is high, the problem that ethylene and methane are easy to freeze at low temperature in the separation process can be solved, the energy consumption is low, the investment is small, and the adjustment is easy.

Description

Cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification
Technical Field
The invention relates to a cryogenic separation device, in particular to a cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification, and belongs to the field of chemical industry.
Background
The ethylene glycol production capacity and yield can not meet the increasing market demands of domestic polyester and the like, the self-supporting rate is less than 60 percent, and the method mainly depends on import. At present, the technology for preparing the ethylene glycol by taking the synthesis gas as the raw material makes a major breakthrough, has great economic advantages, is developed vigorously, and greatly promotes the rapid increase of the demand of the CO cryogenic separation device. The raw materials for producing the ethylene glycol comprise coal gasified synthesis gas, natural gas converted synthesis gas, coke oven gas converted synthesis gas and calcium carbide furnace tail gas synthesis gas, the raw material gas of the coal gasified synthesis gas after conversion and low-temperature methanol washing is usually clean, but the synthesis gas of the natural gas, the coke oven gas and the calcium carbide furnace tail gas conversion usually contains a small amount of olefin components, so that carbon dioxide and olefin which are competitive adsorption exists in a molecular sieve in a cryogenic separation device are adsorbed, and equipment and pipelines are frozen at low temperature by the olefin in a cold box, therefore, a novel molecular sieve adsorbent is required to be adopted, the function of removing ethylene is realized, and a CO cryogenic separation device cold box for removing hydrogen, methane and nitrogen is used for obtaining high-purity CO product gas.
At present, the cryogenic separation method of CO has issued CO/H patents2The single-tower flow of the binary component, Chinese patent document CN200980113560.5) describes that the hydrogen removal is realized, but the purity of CO reaches 98.5 percent to the maximum extent, the purity is lower, the requirement of high-purity CO product gas (more than or equal to 99 percent) cannot be met, and the impurity N is2、 CH4The further purification and separation of (1) is that the double-tower and three-tower processes adopted in the Chinese patent CN201480063530.9 and the three-tower process adopted in the nitrogen circulating refrigeration process are adopted in the Chinese patent CN201611184618.3 to purify and separate CO, but a cryogenic separation device for purifying and separating olefin and H-containing gas is not developed in the market at present2、N2、CH4The mixed gas is separated to obtain high-purity CO.
Disclosure of Invention
The invention aims to provide a cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification, which is mainly used for separating and treating a mixed gas containing olefin, hydrogen, carbon monoxide, nitrogen and methane, wherein the mixed gas is mainly derived from synthesis gas converted from calcium carbide furnace tail gas, natural gas, coke oven tail gas and the like, has the deethylenization function, can separate and obtain high-purity CO product gas with the purity of over 99 percent, wherein H is2And CH4The content is less than 50ppm, the recovery rate is higher, and high-purity CH is byproduct4The product gas can meet the requirements of various synthesis devices, and can solve the problem that ethylene and methane are easy to freeze at low temperature in the separation process, and has low energy consumption, small investment and easy adjustment.
In order to achieve the purpose, the invention is realized by the following technical scheme:
the utility model provides an integrated cryogenic separation device that takes off ethylene, dehydrogenation, demethanization, denitrogenation, includes molecular sieve adsorption unit, cryogenic separation device cold box unit, CO cycle compressor unit, intercommunication between molecular sieve adsorption unit, cryogenic separation device cold box unit, intercommunication between cryogenic separation device cold box unit, CO cycle compressor unit, mist send to the molecular sieve adsorption unit and purify, and the gas after the purification gets into cryogenic separation device cold box unit and separates, CO cycle compressor unit provides pressure for cryogenic separation device cold box unit.
As an improvement, the cold box unit of the cryogenic separation device comprises a first main plate fin type heat exchanger, a second main plate fin type heat exchanger, a deethylenizer, a hydrogen-rich gas separation tank, a dehydrogenation tower, a demethanizer, a denitrogenation tower top condenser, a denitrogenation tower reflux tank, a plurality of pipelines and a plurality of throttle valves, wherein the first main plate fin type heat exchanger, the second main plate fin type heat exchanger, the deethylenizer, the hydrogen-rich gas separation tank, the dehydrogenation tower, the demethanizer, the denitrogenation tower top condenser and the denitrogenation tower reflux tank are communicated through the pipelines and the throttle valves, the deethylenizer condenser is arranged in an inner cavity at the upper part of the deethylenizer, the deethylenizer reboiler is arranged in an inner cavity at the lower part of the deethylenizer, the demethanizer condenser is arranged in an inner cavity at the upper part of the demethanizer, the demethanizer top reboiler is arranged in an inner, the condenser comprises a flow channel a, a flow channel B, a flow channel C, a flow channel D, a flow channel E, a flow channel F, a flow channel G, a flow channel H, a flow channel I, a flow channel J, a flow channel K and a flow channel L, wherein 13 mutually independent flow channels are arranged in a second main plate fin type heat exchanger, the second main plate fin type heat exchanger comprises a flow channel A, a flow channel B, a flow channel C, a flow channel D, a flow channel E, a flow channel F, a flow channel G, a flow channel H, a flow channel I, a flow channel J, a flow channel K, a flow channel L and a flow channel M, and 3 mutually independent flow channels are arranged in a condenser at the top of a.
As an improvement, an inlet pipeline of a cold box unit of a cryogenic separation device is communicated with the upper end of a flow channel B in a first main plate fin type heat exchanger, the lower end of the flow channel B is communicated with a feed inlet in the middle of a deethylenizer through a pipeline, a deethylenizer condenser is arranged in an inner cavity in the upper part of the deethylenizer and is used for condensing gas at the top of a tower, the deethylenizer condenser is respectively communicated with a first CO circulating refrigeration pipeline and a second CO circulating refrigeration pipeline, a deethylenizer reboiler is arranged in an inner cavity in the lower part of the deethylenizer and is respectively communicated with a third CO circulating refrigeration pipeline and a fourth CO circulating refrigeration pipeline and is used for heating liquid at the bottom of the tower through CO circulating gas, the bottom of the deethylenizer is communicated with the lower end of a flow channel c of the first main plate fin type heat exchanger through a valve, the upper end of the flow channel c is connected with an ethylene, the lower end of the flow passage B is communicated with the middle inlet of the hydrogen-rich gas separation tank through a pipeline, and gas after being cooled and condensed by the second main plate fin type heat exchanger is subjected to gas-liquid separation in the hydrogen-rich gas separation tank.
As an improvement, the hydrogen-rich gas separation tank is connected with the lower end of a flow channel C of the main plate fin type heat exchanger through a pipeline, the upper end of the flow channel C is communicated with the lower end of a flow channel e of the main plate fin type heat exchanger through a pipeline, the cold energy is recovered by the first main plate fin type heat exchanger and the second main plate fin type heat exchanger and then is connected with a hydrogen-rich gas collection device through a pipeline, the liquid led out from the bottom of the hydrogen-rich gas separation tank through a pipeline is divided into two branches, one branch is communicated with the lower end of a flow channel D of the second main plate fin type heat exchanger after passing through a pipeline and a throttle valve, the upper end outlet of the flow channel D is connected with the middle inlet of the dehydrogenation tower through a pipeline, and the other branch is.
As an improvement, a dehydrogenation tower reboiler is arranged in an inner cavity at the lower part of the dehydrogenation tower, the dehydrogenation tower reboiler is respectively communicated with a fifth CO circulating refrigeration pipeline and a sixth CO circulating refrigeration pipeline and is used for providing reboiling heat for the dehydrogenation tower by CO circulating gas, the top of the dehydrogenation tower is communicated with the lower end of a flow channel E of a second main plate fin type heat exchanger through a pipeline, the upper end of the flow channel E is communicated with the lower end of a flow channel f of a first main plate fin type heat exchanger through a pipeline, and the flow channel E is connected with a hydrogen-containing tail gas collecting device through a pipeline after cold energy is recovered by the first main plate fin type heat exchanger and the second main plate; the liquid led out from the bottom of the dehydrogenation tower through the pipeline is communicated with the lower end of a flow channel F of the second main plate fin type heat exchanger after passing through the throttle valve and the pipeline, the liquid is reheated by the second main plate fin type heat exchanger and is connected with the inlet in the middle of the pipeline demethanizer, and the methane component in the gas is removed in the demethanizer.
As an improvement, a demethanizer condenser is arranged in an inner cavity at the upper part of the demethanizer and is used for condensing gas at the top of the demethanizer, and the demethanizer condenser is respectively communicated with a No. seven CO circulating refrigeration pipeline and a No. eight CO circulating refrigeration pipeline; a demethanizer reboiler is arranged in an inner cavity at the lower part of the demethanizer and is respectively communicated with a NO. nine CO circulating refrigeration pipeline and a NO. ten CO circulating refrigeration pipeline; the bottom of the demethanizer is communicated with the lower end of a flow channel k of the first main plate fin heat exchanger through a pipeline, and methane gas reheated by the first main plate fin heat exchanger is connected with a methane gas CNG (compressed natural gas) collecting device through a pipeline; the top of the demethanizer is connected with the inlet at the middle part of the denitrogenation tower through a pipeline.
As an improvement, an outlet at the top of the denitrification tower is communicated with the upper end of a flow channel o of a condenser at the top of the denitrification tower through a pipeline, the lower end of the flow channel o is connected with an inlet at the middle part of a reflux tank of the denitrification tower through a pipeline, the top of the reflux tank of the denitrification tower is communicated with the lower end of a flow channel K of a second main plate fin heat exchanger through a pipeline, the upper end of the flow channel K is communicated with the lower end of a flow channel j of a first main plate fin heat exchanger through a pipeline, nitrogen-rich gas after cold energy is recovered by the first main plate fin heat exchanger and the second main plate fin heat exchanger is connected with a nitrogen-rich tail gas collecting device through a pipeline, and the bottom of the reflux tank of the denitrification tower is.
As an improvement, a bottom pipeline of the denitrification tower is divided into two branches, wherein a pipeline in one branch is communicated with the lower end of a flow channel M of the second main plate fin type heat exchanger, and a middle outlet of the flow channel M is connected with a lower gas phase inlet of the denitrification tower through a pipeline; the bottom of the denitrification tower is communicated with the lower end of a flow channel p of a condenser at the top of the denitrification tower through a pipeline and a throttle valve in the other branch, and a CO liquid pipeline subjected to throttling expansion is communicated with a converging pipeline.
As an improvement, high-pressure CO gas from a high-pressure outlet pipeline of a CO circulating compressor unit is communicated with a runner a of a main plate fin type heat exchanger, an upper branch runner outlet of the runner a in the first main plate fin type heat exchanger is communicated with a bottom reboiler of a deethylenizer through a pipeline, an outlet pipeline of the bottom reboiler of the deethylenizer is communicated with a middle and lower branch runner of the runner a of the first main plate fin type heat exchanger, the upper branch runner and the lower branch runner are converged with the runner a, an outlet pipeline at the lower end of the runner a of the first main plate fin type heat exchanger is divided into a first branch pipeline and a second branch pipeline, the first branch pipeline is communicated with an inlet of the bottom reboiler of a dehydrogenation tower, an outlet of the bottom reboiler of the dehydrogenation tower is converged with the pipeline through the pipeline, the second branch pipeline is communicated with an inlet of the bottom reboiler of the demethanizer, an outlet of the bottom reboiler of the demet, one branch is communicated with an inlet of a condenser at the top of a deethylenizer through a throttle valve and a pipeline, an outlet of the condenser at the top of the deethylenizer is communicated with a flow channel A at the middle inlet of a second main plate fin heat exchanger through a pipeline, the upper end of the flow channel A is communicated with an inlet at the lower end of a flow channel d of the main plate fin heat exchanger through a pipeline, and the CO gas with higher pressure after cold recovery is communicated with a third-stage inlet of a CO circulation compressor unit through a pipeline (20); the other branch is communicated with an inlet at the upper end of a flow channel G of the second main plate fin type heat exchanger through a pipeline, an outlet at the lower end of the flow channel G is divided into a first branch pipeline and a second branch pipeline through the pipeline, the second branch pipeline is communicated with an inlet pipeline of a condenser at the top of the demethanizer through a throttle valve and the pipeline, an outlet of the condenser at the top of the demethanizer is communicated with a converging pipeline through the pipeline, the throttle valve is divided into the pipelines, and the pipelines are communicated with the pipeline to provide cold energy for the condenser at the top of the denitrogenation tower; the first branch pipeline is communicated with the converging pipeline through a valve and a pipeline; a low-pressure outlet pipeline from a CO circulating compressor unit is divided into two branches, one branch is communicated with a CO product gas collecting device through a pipeline, the other branch is communicated with an inlet at the upper end of a flow channel g of a first main plate fin type heat exchanger through a pipeline, the lower end of the flow channel g is communicated with an inlet at the upper end of a flow channel H of a second main plate fin type heat exchanger through a pipeline, condensed CO circulating liquid is divided into two branches through a pipeline, and one branch is communicated with a converging pipeline after sequentially passing through the pipeline and a throttle valve; the converging pipeline is communicated with an inlet at the lower end of a flow channel I of the second main plate fin type heat exchanger, an outlet at the upper end of the flow channel I is communicated with an inlet at the lower end of a flow channel h of the first main plate fin type heat exchanger through a pipeline, and medium-pressure grade CO circulating gas after cold energy is recycled by the first main plate fin type heat exchanger and the second main plate fin type heat exchanger is connected with a second-stage inlet of a CO circulating compressor unit through a pipeline; the other branch is communicated with the inlet at the lower end of a flow channel J of the second main plate fin type heat exchanger after passing through a pipeline and a throttle valve in sequence, the outlet at the upper end of the flow channel J is communicated with the inlet at the lower end of a flow channel i of the first main plate fin type heat exchanger through a pipeline, and the low-pressure-grade CO circulating gas after cold recovery is connected with the primary inlet of a CO circulating compressor unit through a pipeline.
The first main plate fin type heat exchanger and the second main plate fin type heat exchanger are provided with liquid nitrogen supplementing channels, external liquid nitrogen is communicated with a liquid nitrogen siphon tank through a pipeline and a throttle valve, liquid at the bottom of the liquid nitrogen siphon tank is communicated with a middle inlet of a flow channel L of the second main plate fin type heat exchanger through a pipeline, gas at the top of the liquid nitrogen siphon tank is communicated with a lower end inlet of a flow channel k in the first main plate fin type heat exchanger after passing through the flow channel L and the pipeline in sequence, and low-pressure nitrogen after cold energy is recovered by the first main plate fin type heat exchanger and the second main plate fin type heat exchanger is connected with a low-pressure nitrogen collecting device through a pipeline;
the ethylene removal tower is a filler rectifying tower, the dehydrogenation tower is a plate rectifying tower or a filler rectifying tower, the demethanizer is a filler rectifying tower, and the denitrification tower is a filler rectifying tower.
Has the advantages that: an inlet pipeline of a cold box unit of the cryogenic separation device is communicated with a flow channel 1b of the first main plate-fin heat exchanger, and is communicated with a feed inlet in the middle of a deethylenizer through a pipeline after being cooled in the flow channel 1b, ethylene in process gas is completely removed in the deethylenizer, and equipment and pipelines are prevented from being frozen at a low-temperature part; has the function of removing ethylene, and can separate and obtain high-purity CO product gas with the purity of over 99 percent and H in the gas2And CH4The content is less than 50ppm, the recovery rate is higher, and high-purity CH is byproduct4The product gas can meet the requirements of various synthesis devices; the method can solve the problem that ethylene and methane are easy to freeze at low temperature in the separation process, and has the characteristics of low energy consumption, small investment, easy adjustment and the like.
Drawings
FIG. 1 is a schematic view of the connection structure of a cryogenic separation plant.
Detailed Description
The present invention will be further described with reference to the drawings attached to the specification, but the present invention is not limited to the following examples.
As shown in fig. 1, a specific embodiment of a cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification is shown, and the cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification comprises a molecular sieve adsorption unit i, a cryogenic separation device cold box unit ii and a CO circulating compressor unit iii, wherein the molecular sieve adsorption unit i and the cryogenic separation device cold box unit ii are communicated, the cryogenic separation device cold box unit ii and the CO circulating compressor unit iii are communicated, a mixed gas is sent to the molecular sieve adsorption unit i for purification, the purified gas enters the cryogenic separation device cold box unit ii for separation, and the CO circulating compressor unit iii provides pressure for the cryogenic separation device cold box unit ii;
the method comprises the steps of firstly conveying mixed gas containing ethylene, carbon monoxide, hydrogen, methane and a small amount of nitrogen to a molecular sieve adsorption unit I through a pipeline, filling a molecular sieve in the molecular sieve adsorption unit I, adsorbing carbon dioxide, methanol or water and other easily-solidified components at low temperature in the mixed gas on the premise of not adsorbing ethylene by the molecular sieve, preventing the substances from freezing the pipeline and equipment, introducing purified gas into a cold box II of a cryogenic separation device for separation and purification, and providing pressure for the cold box unit II of the cryogenic separation device by a CO circulating compressor unit III.
The cryogenic separation device cold box unit II comprises a first main plate fin type heat exchanger 1, a second main plate fin type heat exchanger 2, a deethylenizer 3, a hydrogen-rich gas separation tank 6, a dehydrogenation tower 7, a demethanizer 9, a denitrogenation tower top condenser 13, a denitrogenation tower reflux tank 14, a plurality of pipelines and a plurality of throttle valves, wherein the first main plate fin type heat exchanger 1, the second main plate fin type heat exchanger 2, the deethylenizer 3, the hydrogen-rich gas separation tank 6, the dehydrogenation tower 7, the demethanizer 9, the denitrogenation tower top condenser 13 and the denitrogenation tower reflux tank 14 are communicated through the pipelines and the throttle valves, a reboiler condenser 5 is arranged in an upper cavity of the deethylenizer 3, a deethylenizer 4 is arranged in a lower cavity of the deethylenizer 3, a dehydrogenation tower reboiler 8 is arranged in a lower cavity of the dehydrogenation tower 7, a demethanizer condenser 11 is arranged in an upper cavity of the demethanizer 9, the main plate fin heat exchanger 1 is provided with 12 mutually independent flow channels, which include a flow channel a101, a flow channel B102, a flow channel C103, a flow channel D104, a flow channel E105, a flow channel F106, a flow channel G107, a flow channel H108, a flow channel I109, a flow channel J110, a flow channel K111 and a flow channel L112, the second main plate fin heat exchanger 2 is provided with 13 mutually independent flow channels, which include a flow channel a201, a flow channel B202, a flow channel C203, a flow channel D204, a flow channel E205, a flow channel F206, a flow channel G207, a flow channel H208, a flow channel I209, a flow channel J210, a flow channel K211, a flow channel L212 and a flow channel M213, and the overhead condenser 13 of the denitrification tower is provided with 3 mutually independent flow channels, which include a flow channel o301, a;
the number of the pipelines is 70, marked by natural numbers of 15 to 84, the number of the throttle valves is 11, marked by V1 to V11 in sequence, the pipelines are used for communicating between towers, heat exchangers and the like, and the throttle valves are arranged on the pipelines for throttling.
An inlet pipeline 15 of a cold box unit II of the cryogenic separation device is communicated with the upper end of a flow channel b102 in a main plate fin type heat exchanger 1, the lower end of the flow channel b102 is communicated with a feed inlet in the middle of a deethylenizer 3 through a pipeline 16, firstly, the process gas is cooled to about minus 135 ℃ in the main plate fin type heat exchanger 1, then, the ethylene in the process gas is completely removed in the deethylenizer 3, the freezing of the ethylene in a low-temperature part is avoided, a deethylenizer condenser 5 is arranged in an inner cavity in the upper part of the deethylenizer 3 and is used for condensing the gas at the top of the tower, the deethylenizer condenser 5 is respectively communicated with a first CO circulating refrigeration pipeline 63 and a second CO circulating refrigeration pipeline 18, a deethylenizer reboiler 4 is arranged in an inner cavity in the lower part of the deethylenizer 3, the deethylenizer reboiler 4 is respectively communicated with a third CO circulating refrigeration pipeline, the bottom of the ethylene removal tower 3 is communicated with the lower end of a flow channel c103 of the first main plate fin type heat exchanger 1 through a pipeline 21, a valve V1 and a pipeline 22, the upper end of the flow channel c103 is connected with an ethylene tail gas ETH collecting device through a pipeline 23, the top of the ethylene removal tower 3 is connected with the upper end of a flow channel B202 of the second main plate fin type heat exchanger 2 through a pipeline 17, the lower end of the flow channel B202 is communicated with the middle inlet of the hydrogen-rich gas separation tank 6 through a pipeline 24, and gas which is cooled and condensed to-175-181 ℃ through the second main plate fin type heat exchanger 2 is subjected to gas-liquid separation in the hydrogen-rich gas separation tank.
The hydrogen-rich gas separation tank 6 is connected with the lower end of a flow channel C203 of the main plate fin type heat exchanger 2 through a pipeline 25, the upper end of the flow channel C203 is communicated with the lower end of a flow channel e105 of the main plate fin type heat exchanger 1 through a pipeline 26, the cold energy is recovered by the first main plate fin type heat exchanger 1 and the second main plate fin type heat exchanger 2 and then is connected with a hydrogen-rich gas HG collecting device through a pipeline 27, the liquid led out from the bottom of the hydrogen-rich gas separation tank 6 through a pipeline 28 is divided into two branches, one branch passes through a pipeline 29 and then passes through a throttle valve V2 and a, the lower end of a flow channel D204 of the second main plate fin type heat exchanger 2 is communicated, an outlet at the upper end of the flow channel D204 is connected with an inlet at the middle part of the dehydrogenation tower 7 through a pipeline 31, the other branch is connected with an inlet at the upper part of the dehydrogenation tower 7 through a throttle valve V3 and a pipeline 32, and hydrogen components in gas are removed in the dehydrogenation tower 7.
A dehydrogenation tower reboiler 8 is arranged in an inner cavity at the lower part of the dehydrogenation tower 7 and used for heating liquid at the tower bottom, the dehydrogenation tower reboiler 8 is respectively communicated with a fifth CO circulating refrigeration pipeline 57 and a sixth CO circulating refrigeration pipeline 58 and used for providing reboiling heat for the dehydrogenation tower 7 by CO circulating gas, the top of the dehydrogenation tower 7 is communicated with the lower end of a flow channel E205 of a second main plate fin type heat exchanger 2 through a pipeline 33, the upper end of the flow channel E205 is communicated with the lower end of a flow channel f106 of the first main plate fin type heat exchanger 1 through a pipeline 34, and the first main plate fin type heat exchanger 1 and the second main plate fin type heat exchanger 2 are connected with a hydrogen-containing tail gas FHG collecting device through a pipeline 35 after cold energy; the liquid led out from the bottom of the dehydrogenation tower 7 through the pipeline 36 passes through the throttle valve V4 and the pipeline 37 and then is communicated with the lower end of the flow channel F206 of the second main plate fin heat exchanger 2, the liquid is reheated through the second main plate fin heat exchanger 2 and is connected with the middle inlet of the demethanizer 9 through the pipeline 38, and the methane component in the gas is removed in the demethanizer 9.
A demethanizer condenser 11 is arranged in an inner cavity at the upper part of the demethanizer 9 and is used for condensing gas at the top of the demethanizer 9, and the demethanizer condenser 11 is respectively communicated with a No. seven CO circulating refrigeration pipeline 69 and a No. eight CO circulating refrigeration pipeline 70 and is used for providing cold energy for the demethanizer 9 by CO circulating liquid; a demethanizer reboiler 10 is arranged in an inner cavity at the lower part of the demethanizer 9 and is used for heating liquid at the bottom of the tower, and the demethanizer reboiler 10 is respectively communicated with a NO. nine CO circulating refrigeration pipeline 59 and a NO. ten CO circulating refrigeration pipeline 60 and is used for providing reboiling heat for the demethanizer 9 by CO circulating gas; the bottom of the demethanizer 9 is communicated with the lower end of a flow channel k111 in the first main plate fin heat exchanger 1 through a pipeline 39, and methane gas CNG reheated by the first main plate fin heat exchanger 1 is connected with a methane gas CNG collecting device through a pipeline 40; the top of the demethanizer 9 is connected to the inlet of the middle portion of the denitrogenation column 12 through a pipe 41, and then the nitrogen component in the process gas is removed in the denitrogenation column 12.
An outlet at the top of the denitrification tower 12 is communicated with the upper end of a flow channel o301 of a condenser 13 at the top of the denitrification tower through a pipeline 47, the lower end of the flow channel o301 is connected with an inlet at the middle part of a reflux tank 14 of the denitrification tower through a pipeline 48, the top of the reflux tank 14 of the denitrification tower is communicated with the lower end of a flow channel K211 of a second main plate fin heat exchanger 2 through a pipeline 44, the upper end of the flow channel K211 is communicated with the lower end of a flow channel j110 of a first main plate fin heat exchanger 1 through a pipeline 45, nitrogen-rich gas FNG after cold recovery through the first main plate fin heat exchanger 1 and the second main plate fin heat exchanger 2 is connected with a nitrogen-rich tail gas FNG collecting device through a pipeline 46, and the bottom of the reflux tank 14 of the denitrification tower is connected with a liquid.
The pipeline 50 at the bottom of the denitrification tower 12 is divided into two branches, wherein the pipeline 42 in one branch is communicated with the lower end of a flow channel M213 of the second main plate fin heat exchanger 2, the middle outlet of the flow channel M213 is connected with the lower gas phase inlet of the denitrification tower 12 through a pipeline 43, and the function of the pipeline is to provide reboiling heat for the denitrification tower 12 by using the main plate fin heat exchanger 2; the bottom of the denitrification tower 12 is communicated with the lower end of a flow channel p302 of the condenser 13 at the top of the denitrification tower through the other branch by a throttle valve V5 and a pipeline 51, the upper end of the flow channel p302 is communicated with a pipeline 52, and the CO liquid pipeline 52 subjected to throttle expansion is communicated with a converging pipeline 73, so that cold energy is provided for the condenser 13 of the denitrification tower.
The high-pressure CO gas from a high-pressure outlet pipeline 53 of a CO circulating compressor unit III is communicated with a flow channel a101 of a first main plate fin type heat exchanger 1, the outlet of an upper branch flow channel 1a-1 of the flow channel a101 in the first main plate fin type heat exchanger 1 is communicated with a reboiler 4 at the bottom of a deethylenizer tower through a pipeline 54 to provide reboiling heat for the deethylenizer 3, the outlet pipeline 55 of the reboiler 4 at the bottom of the deethylenizer tower is communicated with a middle and lower branch flow channel 1a-2 of the flow channel a101 of the first main plate fin type heat exchanger 1, the upper branch flow channel 1a-1 and the lower branch flow channel 1a-2 are converged with the flow channel a, the outlet pipeline 56 at the lower end of the flow channel a101 of the first main plate fin type heat exchanger 1 is divided into a branch pipeline 57 and a branch pipeline 59, the first branch pipeline 57 is communicated with the inlet of a reboiler 8 at the bottom, in the process, heat is provided for the dehydrogenation tower 7, a second branch pipeline 59 is communicated with the inlet of the reboiler 10 at the bottom of the demethanizer, the outlet of the reboiler 10 at the bottom of the demethanizer is converged with a pipeline 61 through a pipeline 60, and in the process, heat is provided for the demethanizer 9; the pipeline 61 is divided into two branches after being converged, wherein one branch is communicated with an inlet of a condenser 5 at the top of the deethylenizer tower through a pipeline 62, a throttle valve V6 and a pipeline 63 to provide cold energy for the condenser 5 at the top of the deethylenizer tower, an outlet of the condenser 5 at the top of the deethylenizer tower is communicated with a flow channel A201 at the middle part of the second main plate fin heat exchanger 2 through a pipeline 18, the upper end of the flow channel A201 is communicated with an inlet at the lower end of a flow channel d104 of the main plate fin heat exchanger 1 through a pipeline 19, and the CO gas with higher pressure after cold energy recovery is communicated with a tertiary inlet of a CO circulation compressor; the other branch is communicated with an inlet at the upper end of a flow channel G of the second main plate fin type heat exchanger 2 through a pipeline 64, an outlet at the lower end of the flow channel G207 is divided into a first branch pipeline 66 and a second branch pipeline 68 through a pipeline 65, the second branch pipeline 68 is communicated with an inlet pipeline of a demethanizer overhead condenser 9 through a throttle valve V7 and a pipeline 69, an outlet of the demethanizer overhead condenser 9 is communicated with a converging pipeline 73 through a pipeline 70 to provide cold for the demethanizer overhead condenser 9, a pipeline 71 is branched out of the throttle valve V7, the pipeline 71 is communicated with a pipeline 52 after being sequentially connected with a flow channel q303 and a pipeline 72 to provide cold for the denitrogenator overhead condenser 13; the first branch pipe 66 is communicated with the confluence pipe 73 through a valve V8 and a pipe 67; a low-pressure outlet pipeline from a CO circulating compressor unit III is divided into two parts, one part is communicated with a CO product gas CO collecting device through a pipeline 85 and is output to a downstream synthesis device as CO product gas, the other part is communicated with an inlet at the upper end of a flow channel g107 of a first main plate fin type heat exchanger 1 through a pipeline 74, the lower end of the flow channel g107 is communicated with an inlet at the upper end of a flow channel H208 of a second main plate fin type heat exchanger 2 through a pipeline 75, condensed CO circulating liquid is divided into two branches through a pipeline 76, and one branch is communicated with a converging pipeline 73 through a pipeline 81, a throttle valve V9 and a pipeline 82 to provide medium-pressure cold energy for the heat exchangers; the converging pipeline 73 is communicated with the inlet at the lower end of a flow channel I209 of the second main plate fin heat exchanger 2, the outlet at the upper end of the flow channel I209 is communicated with the inlet at the lower end of a flow channel h108 of the first main plate fin heat exchanger 1 through a pipeline 83, and the medium-pressure grade CO circulating gas after cold recovery through the first main plate fin heat exchanger 1 and the second main plate fin heat exchanger 2 is connected with the second-stage inlet of a CO circulating compressor unit III through a pipeline 84; the other branch is communicated with the inlet at the lower end of a flow channel J210 of the second main plate fin type heat exchanger 2 through a pipeline 77, a throttle valve V10 and a pipeline 78, the outlet at the upper end of the flow channel J210 is communicated with the inlet at the lower end of a flow channel i109 of the first main plate fin type heat exchanger 1 through a pipeline 79, and the low-pressure-grade CO circulating gas after cold recovery is connected with the inlet at the first stage of the CO circulating compressor unit III through a pipeline 80.
The first main plate fin type heat exchanger 1 and the second main plate fin type heat exchanger 2 are provided with liquid nitrogen supplementing channels, external liquid nitrogen is communicated with a liquid nitrogen siphon tank 88 through a pipeline LN and a throttle valve V11, the evaporation of the liquid nitrogen adopts a thermosyphon method, liquid at the bottom of the liquid nitrogen siphon tank 88 is communicated with the middle inlet of a flow channel L212 of the second main plate fin type heat exchanger 2 through a pipeline 87, gas at the top of the liquid nitrogen siphon tank 88 is communicated with the lower end inlet of a flow channel K111 in the first main plate fin type heat exchanger 1 after sequentially passing through the flow channel L212 and a pipeline 89, and low-pressure nitrogen after cold recovery through the first main plate fin type heat exchanger 1 and the second main plate fin type heat exchanger 2 is connected with a low-pressure nitrogen NG (nitrogen gas) collecting device through a pipeline 90;
the ethylene removal tower 5 is a filler rectifying tower, the dehydrogenation tower 7 is a plate rectifying tower or a filler rectifying tower, the demethanizer 9 is a filler rectifying tower, and the denitrogenation tower 12 is a filler rectifying tower.
A first main plate fin type heat exchanger 1, a second main plate fin type heat exchanger 2, a deethylenizer 4 at the bottom of a deethylenizer tower, a condenser 5 at the top of a deethylenizer tower, a reboiler 8 at the bottom of a dehydrogenation tower, a reboiler 10 at the bottom of a demethanizer tower, a condenser 9 at the top of the demethanizer tower and a condenser 13 at the top of a denitrificaion tower all adopt plate fin type heat exchangers, internal thermosyphons exchange heat and cold, and the deformed main plate fin type heat exchangers can be placed outside a rectifying tower to provide heat for the rectifying tower by adopting an external thermosyph.
Finally, it should be noted that the present invention is not limited to the above embodiments, and many variations are possible. All modifications which can be derived or suggested by a person skilled in the art from the disclosure of the present invention are to be considered within the scope of the invention.

Claims (10)

1. A cryogenic separation device integrating ethylene removal, dehydrogenation, demethanization and denitrification is characterized in that: including molecular sieve adsorption unit, cryogenic separation device cold box unit, CO circulating compressor unit, intercommunication between molecular sieve adsorption unit, cryogenic separation device cold box unit, intercommunication between cryogenic separation device cold box unit, CO circulating compressor unit, mixed gas send to molecular sieve adsorption unit and purifies, and the gas after the purification gets into cryogenic separation device cold box unit and separates, CO circulating compressor unit provides pressure for cryogenic separation device cold box unit.
2. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 1, wherein: the cold box unit of the cryogenic separation device comprises a first main plate fin type heat exchanger, a second main plate fin type heat exchanger, a deethylenizer, a hydrogen-rich gas separation tank, a dehydrogenation tower, a demethanizer, a denitrogenation tower top condenser, a denitrogenation tower reflux tank, a plurality of pipelines and a plurality of throttle valves, wherein the first main plate fin type heat exchanger, the second main plate fin type heat exchanger, the deethylenizer, the hydrogen-rich gas separation tank, the dehydrogenation tower, the demethanizer, the denitrogenation tower top condenser and the denitrogenation tower reflux tank are communicated through the pipelines and the throttle valves, the deethylenizer condenser is arranged in an inner cavity at the upper part of the deethylenizer, a deethylenizer lower inner cavity is provided with a deethylenizer, a reboiler is arranged in an inner cavity at the lower part of the dehydrogenation tower, a demethanizer condenser is arranged in an inner cavity at the upper part of the demethanizer, the condenser comprises a flow channel a, a flow channel B, a flow channel C, a flow channel D, a flow channel E, a flow channel F, a flow channel G, a flow channel H, a flow channel I, a flow channel J, a flow channel K and a flow channel L, wherein 13 mutually independent flow channels are arranged in a second main plate fin type heat exchanger, the second main plate fin type heat exchanger comprises a flow channel A, a flow channel B, a flow channel C, a flow channel D, a flow channel E, a flow channel F, a flow channel G, a flow channel H, a flow channel I, a flow channel J, a flow channel K, a flow channel L and a flow channel M, and 3 mutually independent flow channels are arranged in a condenser at the top of a.
3. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 2, wherein: an inlet pipeline of a cold box unit of the cryogenic separation device is communicated with the upper end of a flow channel B in a first main plate fin type heat exchanger, the lower end of the flow channel B is communicated with a feed inlet in the middle of a deethylenizer through a pipeline, a deethylenizer condenser is arranged in an inner cavity in the upper part of the deethylenizer and is used for condensing gas at the top of the tower, the deethylenizer condenser is respectively communicated with a first CO circulating refrigeration pipeline and a second CO circulating refrigeration pipeline, a deethylenizer reboiler is arranged in an inner cavity in the lower part of the deethylenizer and is respectively communicated with a third CO circulating refrigeration pipeline and a fourth CO circulating refrigeration pipeline and is used for heating liquid at the bottom of the tower through CO circulating gas, the bottom of the deethylenizer is communicated with the lower end of a flow channel c of the first main plate fin type heat exchanger after passing through a valve, the upper end of the flow channel c is connected, the lower end of the flow passage B is communicated with the middle inlet of the hydrogen-rich gas separation tank through a pipeline, and gas after being cooled and condensed by the first main plate-fin heat exchanger is subjected to gas-liquid separation in the hydrogen-rich gas separation tank.
4. The cryogenic separation plant integrating deethylenization, dehydrogenation, demethanization, and denitrogenation according to claim 2 or 3, wherein: the hydrogen-rich gas separation tank is connected with the lower end of a flow channel C of the main plate fin heat exchanger through a pipeline, the upper end of the flow channel C is communicated with the lower end of a flow channel e of the main plate fin heat exchanger through a pipeline, the first main plate fin heat exchanger and the second main plate fin heat exchanger are connected with a hydrogen-rich gas collection device through pipelines after cold energy is recovered, liquid led out from the bottom of the hydrogen-rich gas separation tank through a pipeline is divided into two branches, one branch is communicated with the lower end of a flow channel D of the second main plate fin heat exchanger after passing through a pipeline and a throttle valve, the upper end outlet of the flow channel D is connected with the middle inlet of the dehydrogenation tower through a pipeline, and the other branch is connected with the upper inlet of the dehydrogenation tower.
5. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 4, wherein: a dehydrogenation tower reboiler is arranged in an inner cavity at the lower part of the dehydrogenation tower, the dehydrogenation tower reboiler is respectively communicated with a fifth CO circulating refrigeration pipeline and a sixth CO circulating refrigeration pipeline and is used for providing reboiling heat for the dehydrogenation tower by CO circulating gas, the top of the dehydrogenation tower is communicated with the lower end of a flow channel E of a second main plate fin type heat exchanger through a pipeline, the upper end of the flow channel E is communicated with the lower end of a flow channel f of a first main plate fin type heat exchanger through a pipeline, and the flow channel E is connected with a hydrogen-containing tail gas collecting device through a pipeline after cold energy is recovered by the first main plate fin type heat exchanger and the second main; the liquid led out from the bottom of the dehydrogenation tower through the pipeline is communicated with the lower end of a flow channel F of the second main plate fin type heat exchanger after passing through the throttle valve and the pipeline, the liquid is reheated by the second main plate fin type heat exchanger and is connected with the inlet in the middle of the pipeline demethanizer, and the methane component in the gas is removed in the demethanizer.
6. The cryogenic separation plant integrating deethylenization, dehydrogenation, demethanization, and denitrogenation according to claim 2 or 5, wherein: a demethanizer condenser is arranged in an inner cavity at the upper part of the demethanizer and is used for condensing gas at the top of the demethanizer, and the demethanizer condenser is respectively communicated with a No. seven CO circulating refrigeration pipeline and a No. eight CO circulating refrigeration pipeline; a demethanizer reboiler is arranged in an inner cavity at the lower part of the demethanizer and is respectively communicated with a NO. nine CO circulating refrigeration pipeline and a NO. ten CO circulating refrigeration pipeline; the bottom of the demethanizer is communicated with the lower end of a flow channel k of the first main plate fin heat exchanger through a pipeline, and methane gas reheated by the first main plate fin heat exchanger is connected with a methane gas collecting device through a pipeline; the top of the demethanizer is connected with the inlet at the middle part of the denitrogenation tower through a pipeline.
7. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 6, wherein: the export of denitrogenation tower top is linked together through the runner o upper end of pipeline with denitrogenation tower top condenser, runner o lower extreme is connected through the middle part entry of pipeline with denitrogenation tower reflux tank, denitrogenation tower reflux tank top is linked together through the lower extreme of pipeline K of pipeline with No. two mainboard fin heat exchangers, the lower extreme of runner K upper end through the runner j of pipeline with a mainboard fin heat exchanger is linked together, through a mainboard fin heat exchanger, No. two nitrogen-rich gas after mainboard fin heat exchanger retrieves cold volume is connected with nitrogen-rich tail gas collection device through the pipeline, denitrogenation tower reflux tank bottom is connected with denitrogenation tower upper portion liquid phase entry through the pipeline, be used for denitrogenation tower regulating column internal reflux ratio.
8. The cryogenic separation plant integrating deethylenization, dehydrogenation, demethanization, denitrification according to claim 2, 5 or 7, wherein: the bottom pipeline of the denitrification tower is divided into two branches, wherein the pipeline in one branch is communicated with the lower end of a flow channel M of the second main plate fin type heat exchanger, and the middle outlet of the flow channel M is connected with the lower gas phase inlet of the denitrification tower through a pipeline; the bottom of the denitrification tower is communicated with the lower end of a flow channel p of a condenser at the top of the denitrification tower through a pipeline and a throttle valve in the other branch, and a CO liquid pipeline subjected to throttling expansion is communicated with a converging pipeline.
9. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 8, wherein: the high-pressure CO gas from a high-pressure outlet pipeline of a CO circulating compressor unit is communicated with a flow channel a of a main plate fin type heat exchanger, an upper branch flow channel outlet of the flow channel a in the first main plate fin type heat exchanger is communicated with a bottom reboiler of a deethylenizer through a pipeline, an outlet pipeline of the bottom reboiler of the deethylenizer is communicated with a middle lower branch flow channel of the flow channel a of the first main plate fin type heat exchanger, the upper branch flow channel and the lower branch flow channel are converged with the flow channel a, an outlet pipeline at the lower end of the flow channel a of the first main plate fin type heat exchanger is divided into a first branch pipeline and a second branch pipeline, the first branch pipeline is communicated with an inlet of the bottom reboiler of the dehydrogenation tower, an outlet of the bottom reboiler of the dehydrogenation tower is converged with the pipeline through the pipeline, the second branch pipeline is communicated with an inlet of the; the pipeline is divided into two branches after being converged, wherein one branch is communicated with an inlet of a condenser at the top of a deethylenizer through a throttle valve and the pipeline, an outlet of the condenser at the top of the deethylenizer is communicated with a flow channel A at the middle inlet of a second main plate fin heat exchanger through the pipeline, the upper end of the flow channel A is communicated with an inlet at the lower end of a flow channel d of the main plate fin heat exchanger through the pipeline, and the CO gas with higher pressure after cold recovery is communicated with a third-stage inlet of a CO circulation compressor unit through the pipeline; the other branch is communicated with an inlet at the upper end of a flow channel G of the second main plate fin type heat exchanger through a pipeline, an outlet at the lower end of the flow channel G is divided into a first branch pipeline and a second branch pipeline through the pipeline, the second branch pipeline is communicated with an inlet pipeline of a condenser at the top of the demethanizer through a throttle valve and the pipeline, an outlet of the condenser at the top of the demethanizer is communicated with a converging pipeline through the pipeline, the throttle valve is divided into the pipelines, and the pipelines are communicated with the pipeline to provide cold energy for the condenser at the top of the denitrogenation tower; the first branch pipeline is communicated with the converging pipeline through a valve and a pipeline; a low-pressure outlet pipeline from a CO circulating compressor unit is divided into two branches, one branch is communicated with a CO product gas collecting device through a pipeline, the other branch is communicated with an inlet at the upper end of a flow channel g of a first main plate fin type heat exchanger through a pipeline, the lower end of the flow channel g is communicated with an inlet at the upper end of a flow channel H of a second main plate fin type heat exchanger through a pipeline, condensed CO circulating liquid is divided into two branches through a pipeline, and one branch is communicated with a converging pipeline after sequentially passing through the pipeline and a throttle valve; the converging pipeline is communicated with an inlet at the lower end of a flow channel I of the second main plate fin type heat exchanger, an outlet at the upper end of the flow channel I is communicated with an inlet at the lower end of a flow channel h of the first main plate fin type heat exchanger through a pipeline, and medium-pressure grade CO circulating gas after cold energy is recycled by the first main plate fin type heat exchanger and the second main plate fin type heat exchanger is connected with a second-stage inlet of a CO circulating compressor unit through a pipeline; the other branch is communicated with the inlet at the lower end of a flow channel J of the second main plate fin type heat exchanger after passing through a pipeline and a throttle valve in sequence, the outlet at the upper end of the flow channel J is communicated with the inlet at the lower end of a flow channel i of the first main plate fin type heat exchanger through a pipeline, and the low-pressure-grade CO circulating gas after cold recovery is connected with the primary inlet of a CO circulating compressor unit through a pipeline.
10. The cryogenic separation plant integrating ethylene removal, dehydrogenation, demethanization and denitrification as claimed in claim 1, wherein: the first main plate fin type heat exchanger and the second main plate fin type heat exchanger are provided with liquid nitrogen supplementing channels, external liquid nitrogen is communicated with a liquid nitrogen siphon tank through a pipeline and a throttle valve, liquid at the bottom of the liquid nitrogen siphon tank is communicated with the middle inlet of a flow channel L of the second main plate fin type heat exchanger through a pipeline, gas at the top of the liquid nitrogen siphon tank is communicated with the lower end inlet of a flow channel k in the first main plate fin type heat exchanger after passing through the flow channel L and the pipeline in sequence, and low-pressure nitrogen after cold energy is recycled by the first main plate fin type heat exchanger and the second main plate fin type heat exchanger is connected with a low-pressure nitrogen collecting device through;
the ethylene removal tower is a filler rectifying tower, the dehydrogenation tower is a plate rectifying tower or a filler rectifying tower, the demethanizer is a filler rectifying tower, and the denitrification tower is a filler rectifying tower.
CN201921061939.3U 2019-07-09 2019-07-09 Cryogenic separation device integrating deethylenization, dehydrogenation, demethanization and denitrification Withdrawn - After Issue CN210346071U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110345709A (en) * 2019-07-09 2019-10-18 杭州杭氧股份有限公司 The cryogenic separation device that a kind of integrated de- ethylene, dehydrogenation, demethanation, denitrification functions are integrated

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110345709A (en) * 2019-07-09 2019-10-18 杭州杭氧股份有限公司 The cryogenic separation device that a kind of integrated de- ethylene, dehydrogenation, demethanation, denitrification functions are integrated
CN110345709B (en) * 2019-07-09 2024-04-12 杭氧集团股份有限公司 Cryogenic separation device integrating functions of de-ethylene, dehydrogenation, de-methane and denitrification

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