CN212274412U - Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas - Google Patents

Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas Download PDF

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Publication number
CN212274412U
CN212274412U CN202021758804.5U CN202021758804U CN212274412U CN 212274412 U CN212274412 U CN 212274412U CN 202021758804 U CN202021758804 U CN 202021758804U CN 212274412 U CN212274412 U CN 212274412U
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China
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pipeline
heat exchanger
gas
main heat
tower
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CN202021758804.5U
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Inventor
张武
郝凯钟
赵杰
史红兵
陈亮亮
任剑峰
刘利伟
赵南
保雄飞
田园
马鹏
何彦涛
李宗荣
李伟
李国太
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Zhongke Ruiao Energy Technology Co ltd
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Zhongke Ruiao Energy Technology Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—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
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops

Abstract

The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, include: a primary heat exchanger; the rectifying tower is connected with the main heat exchanger through a pipeline; the product separator is connected with the tower bottom outlet of the rectifying tower through a pipeline; the tower top condenser is connected with the rectifying tower through a pipeline; the cooling tower top separator, the noncondensable gas export of cooling tower top separator and first tube coupling, cooling tower top separator passes through the pipeline and is connected with the rectifying column. The technical scheme of the utility model energy consumption is low, and is energy-concerving and environment-protective, can change waste into valuables, makes the product added value improve greatly.

Description

Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas
Technical Field
The utility model relates to a chemical industry field especially relates to an equipment of propane, propylene, ethylene are retrieved to chemical industry tail gas.
Background
Ethylene, propylene and propane are important chemical raw materials.
Ethylene, propylene and propane products are valuable resources in refining and chemical enterprises and are the most basic chemical raw materials. In the production process of preparing olefin from methanol, a part of products such as ethylene, propylene, propane and the like are taken away along with methane tail gas in an olefin separation unit and are used as torch gas or fuel gas, so that resource waste is caused. However, if the products such as ethylene, propylene, propane and the like in the methane tail gas are extracted for independent use, the added value of the products is greatly improved. Wherein the value of the fuel gas is about 1000 yuan/ton, and the value of the products of ethylene, propylene and propane is about 3500 yuan/ton, and huge waste is caused by directly burning the products of ethylene, propylene and propane in the fuel gas.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide an equipment that can fully extract the component in the methane tower tail gas and prepare the chemical industry tail gas recovery propane of hydrocarbon mixture product, propylene, ethylene.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, include:
the main heat exchanger is used for cooling chemical tail gas;
the rectifying tower is used for rectifying the cooled chemical tail gas to obtain a gas phase and a liquid phase and is connected with the main heat exchanger through a pipeline;
the product separator is used for separating the liquid phase to obtain a C2+ product and fuel gas and is connected with the bottom outlet of the rectifying tower through a pipeline;
the tower top condenser is used for cooling the gas phase and is connected with the rectifying tower through a pipeline;
the cooling tower top separator is used for separating the cooled gas phase to obtain non-condensable gas, a non-condensable gas outlet of the cooling tower top separator is connected with a first pipeline, and the cooling tower top separator is connected with the rectifying tower through a pipeline;
the first pipeline is connected with an inlet of a first-stage expander after sequentially passing through the tower top condenser and the main heat exchanger, so that the non-condensable gas in the first pipeline is subjected to expansion, temperature and pressure reduction treatment by the first-stage expander after being reheated by the tower top condenser and the main heat exchanger, an outlet of the first-stage expander is connected with a second pipeline, the second pipeline is connected with an inlet of a second-stage expander after passing through the main heat exchanger, so that the non-condensable gas in the second pipeline is subjected to expansion, temperature and pressure reduction treatment by the second-stage expander after being cooled by the main heat exchanger, an outlet of the second-stage expander is connected with a third pipeline, and the third pipeline sequentially passes through the tower top condenser and the main heat exchanger, so that the non-condensable gas in the third pipeline provides cold for the tower top.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, wherein, the export is passed through the fourth tube coupling at the bottom of the tower of product separator and rectifying column, be provided with low temperature hydrocarbon mixing pump on the fourth pipeline.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, wherein, the product separator is connected behind main heat exchanger to the fourth pipeline to make the liquid phase in the fourth pipeline provide cold volume for main heat exchanger.
The technical scheme of the utility model can fully extract the component in the methane tower tail gas, prepare the hydrocarbon mixture product, improve economic benefits, also improve methane tail gas's utilization efficiency, make its added value promote by a wide margin.
Drawings
Fig. 1 is a schematic structural diagram of the equipment for recovering propane, propylene and ethylene from chemical tail gas of the present invention.
Detailed Description
As shown in figure 1, the utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas includes:
a main heat exchanger E102 for cooling chemical tail gas;
the rectifying tower T101 is used for rectifying the cooled chemical tail gas to obtain a gas phase and a liquid phase and is connected with the main heat exchanger through a pipeline;
a product separator V101 for separating the liquid phase to obtain a C2+ product and a fuel gas, which is connected with the bottom outlet of the rectifying tower through a pipeline;
the tower top condenser E103 is used for cooling the gas phase and is connected with the rectifying tower through a pipeline;
a cooling tower top separator V102 for separating the cooled gas phase to obtain non-condensable gas, wherein a non-condensable gas outlet of the cooling tower top separator is connected with the first pipeline 10, and the cooling tower top separator is connected with the rectifying tower through a pipeline;
the first pipeline 10 is connected with an inlet of a first-stage expander C101 after sequentially passing through a tower top condenser and a main heat exchanger, so that the noncondensable gas in the first pipeline is subjected to expansion, temperature reduction and pressure reduction treatment by the first-stage expander after the tower top condenser and the main heat exchanger are rewarming, an outlet of the first-stage expander is connected with a second pipeline 20, the second pipeline is connected with an inlet of a second-stage expander C102 after passing through the main heat exchanger, so that the noncondensable gas in the second pipeline is subjected to expansion, temperature reduction and pressure reduction treatment by the second-stage expander after being cooled by the main heat exchanger, an outlet of the second-stage expander is connected with a third pipeline, and the third pipeline 30 sequentially passes through the tower top condenser and the main heat exchanger, so that the noncondensable gas in the third pipeline provides cold for the.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, wherein, the export is passed through the fourth tube coupling at the bottom of the tower of product separator and rectifying column, be provided with low temperature hydrocarbon mixing pump P101 on the fourth pipeline 40.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas, wherein, the product separator is connected behind main heat exchanger to the fourth pipeline to make the liquid phase in the fourth pipeline provide cold volume for main heat exchanger.
The utility model discloses an equipment of propane, propylene, ethylene are retrieved to chemical industry tail gas relates to methyl alcohol system alkene demethanizer tower top tail gas recovery propane, propylene, ethylene.
The demethanizer of the olefin separation unit of the MTO device recovers C2 and above components in the raw material gas by adopting a low-temperature propane or propylene washing mode, and tail gas obtained by washing and dissolving propane in the demethanizer contains a large amount of methane, hydrogen, nitrogen, carbon monoxide, ethylene, propane, propylene, C4 and the like.
The tail gas at the top of the methane tower is firstly cooled to a certain temperature by a heat exchanger, the cooled feed gas is separated by a low-temperature rectifying tower, and qualified C2+ products are produced at the bottom of the tower and are sent out of a battery compartment after being pressurized and reheated by a low-temperature hydrocarbon mixing pump. The noncondensable gas (fuel gas) produced from the top of the tower is reheated to a certain temperature by a heat exchanger, enters a first-stage expansion machine to be expanded to a certain pressure, enters the heat exchanger again to exchange heat to a certain temperature, enters a second-stage expansion machine to be expanded to a certain pressure and temperature to provide cold energy of the lowest temperature region for the top of the rectifying tower. And the tail gas after being reheated at the top of the rectifying tower is reheated again by the main heat exchanger and is sent to a fuel gas pipe network.
The utility model discloses an equipment of propane, propylene, ethylene are retrieved to chemical industry tail gas utilizes demethanizer tower top tail gas, draws C2+ product wherein in the mode methane tower tail gas through expander expansion refrigeration, cryrogenic rectification separation, and residual gas sends into the fuel gas pipe network as fuel gas.
The tail gas after propane washing and dissolving in the demethanizer contains a large amount of methane, hydrogen, nitrogen, carbon monoxide, ethylene, propane, propylene, C4, etc. The tail gas at the top of the methane tower is firstly cooled to a certain temperature by a heat exchanger, the cooled feed gas is separated by a low-temperature rectifying tower, and qualified C2+ products are produced at the bottom of the tower and are sent out of a battery compartment after being pressurized and reheated by a low-temperature hydrocarbon mixing pump. The noncondensable gas (fuel gas) produced from the top of the tower is reheated to a certain temperature by a heat exchanger, enters a first-stage expansion machine to be expanded to a certain pressure, enters a heat exchanger again to exchange heat to a certain temperature, then enters a second-stage expansion machine to be expanded to a certain pressure and temperature to provide cold energy for the top of the rectifying tower. And the tail gas after being reheated at the top of the rectifying tower is reheated again by the main heat exchanger and is sent to a fuel gas pipe network.
The main heat exchanger can be plate-fin type, wound tube type or plate type.
The tail gas at the top of the methane tower is firstly cooled to a certain temperature by a heat exchanger, and the cooled feed gas is separated by a low-temperature rectifying tower, wherein the cooling temperature range is generally from-30 ℃ to-120 ℃.
Qualified C2+ products are produced from the bottom of the tower, and C2+ generally comprises ethylene, propylene, propane, isobutane, n-butane and the like.
The non-condensable gas (fuel gas) produced from the tower top is firstly passed through a heat exchanger and reheated to a certain temperature, and the reheating range is generally between-130 deg.C and-50 deg.C.
The non-condensable gas enters a primary expansion machine to be expanded to a certain pressure, and the pressure range after expansion is generally between 1.8MPa and 1.2 MPa.
The expander is of a turbine type, and an oil bearing expander and a gas bearing expander can be generally selected.
The non-condensable gas enters the heat exchanger again to exchange heat to a certain temperature, then enters the secondary expansion machine to be expanded to a certain pressure and temperature, and the temperature range of the non-condensable gas entering the secondary expansion machine is generally between 60 ℃ below zero and 120 ℃ below zero. The pressure range after secondary expansion is generally between 1.6MPa and 0.1 MPa.
The non-condensable gas provides cold energy of the lowest temperature region for the top of the rectifying tower, and the temperature of the top of the rectifying tower is generally between-120 ℃ and-145 ℃.
The recovery rate of the C2+ hydrocarbon mixture can reach between 92% and 98%.
And C2+ products are pressurized and reheated by a low-temperature hydrocarbon mixing pump and then are sent out of a battery limit area, and the products are directly sent to an olefin separation device for separation after being reheated.
The C2+ product passes through a low-temperature hydrocarbon mixing pump which can be a shield pump, a low-temperature immersed pump, a centrifugal pump and a reciprocating pump.
The utility model discloses an equipment of propane, propylene, ethylene is retrieved to chemical industry tail gas is reliable and stable, the energy consumption is low, can change waste into valuables, make the product added value improve greatly.
The tail gas of the demethanizer passes through a reboiler E101 and a main heat exchanger, is cooled to minus 30 ℃ to minus 130 ℃, enters a low-temperature rectifying tower, liquid-phase products are extracted from the top of the tower, are subjected to pressure boosting through a low-temperature hydrocarbon mixing pump, are re-heated through the main heat exchanger and are sent out of a battery limit.
The gas phase at the top of the tower can be condensed by a condenser at the top of the tower, then the liquid phase flows back to the tower, the gas phase enters a first-stage expansion machine through a cooler for reheating to-120 ℃ to-60 ℃ through a main heat exchanger, the expanded tail gas enters a second-stage expansion machine for heat exchange after heat exchange and reheating, the expanded tail gas and the tail gas at the top of the low-temperature rectification tower exchange heat, and finally the tail gas is reheated by the main heat exchanger and sent out of a boundary area. The cooling capacity of the whole system is provided by the expansion machine.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (3)

1. The utility model provides an equipment of propane, propylene, ethylene are retrieved to chemical industry tail gas which characterized in that includes:
the main heat exchanger is used for cooling chemical tail gas;
the rectifying tower is used for rectifying the cooled chemical tail gas to obtain a gas phase and a liquid phase and is connected with the main heat exchanger through a pipeline;
the product separator is used for separating the liquid phase to obtain a C2+ product and fuel gas and is connected with the bottom outlet of the rectifying tower through a pipeline;
the tower top condenser is used for cooling the gas phase and is connected with the rectifying tower through a pipeline;
the cooling tower top separator is used for separating the cooled gas phase to obtain non-condensable gas, a non-condensable gas outlet of the cooling tower top separator is connected with a first pipeline, and the cooling tower top separator is connected with the rectifying tower through a pipeline;
the first pipeline is connected with an inlet of a first-stage expander after sequentially passing through the tower top condenser and the main heat exchanger, so that the non-condensable gas in the first pipeline is subjected to expansion, temperature and pressure reduction treatment by the first-stage expander after being reheated by the tower top condenser and the main heat exchanger, an outlet of the first-stage expander is connected with a second pipeline, the second pipeline is connected with an inlet of a second-stage expander after passing through the main heat exchanger, so that the non-condensable gas in the second pipeline is subjected to expansion, temperature and pressure reduction treatment by the second-stage expander after being cooled by the main heat exchanger, an outlet of the second-stage expander is connected with a third pipeline, and the third pipeline sequentially passes through the tower top condenser and the main heat exchanger, so that the non-condensable gas in the third pipeline provides cold for the tower top.
2. The equipment for recovering propane, propylene and ethylene from the chemical engineering tail gas as claimed in claim 1, wherein the product separator is connected with the outlet at the bottom of the rectifying tower through a fourth pipeline, and a cryogenic mixed hydrocarbon pump is arranged on the fourth pipeline.
3. The equipment for recovering propane, propylene and ethylene from the chemical engineering tail gas according to claim 2, wherein the fourth pipeline passes through the main heat exchanger and then is connected with the product separator, so that the liquid phase in the fourth pipeline provides cold energy for the main heat exchanger.
CN202021758804.5U 2020-08-21 2020-08-21 Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas Active CN212274412U (en)

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Application Number Priority Date Filing Date Title
CN202021758804.5U CN212274412U (en) 2020-08-21 2020-08-21 Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202021758804.5U CN212274412U (en) 2020-08-21 2020-08-21 Equipment for recovering propane, propylene and ethylene from chemical engineering tail gas

Publications (1)

Publication Number Publication Date
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