CN210569510U - Multi-strand backflow ethane recovery device - Google Patents

Multi-strand backflow ethane recovery device Download PDF

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Publication number
CN210569510U
CN210569510U CN201920993041.3U CN201920993041U CN210569510U CN 210569510 U CN210569510 U CN 210569510U CN 201920993041 U CN201920993041 U CN 201920993041U CN 210569510 U CN210569510 U CN 210569510U
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heat exchanger
demethanizer
stage
gas
supercooling heat
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CN201920993041.3U
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Chinese (zh)
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王轲
李长俊
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Southwest Petroleum University
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Southwest Petroleum University
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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
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • 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

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The utility model discloses a stranded backward flow ethane recovery unit, including feed gas precooling heat exchanger, one-level low temperature separator, one-level supercooling heat exchanger, second grade cryogenic separation ware, second grade supercooling heat exchanger, demethanizer, defeated air compressor outward, the second air cooler, first air cooler, still include with feed gas precooling heat exchanger, the expander set, the one-level cryogenic separation ware that one-level supercooling heat exchanger all links to each other, with one-level supercooling heat exchanger, second grade supercooling heat exchanger, the second grade cryogenic separation ware that demethanizer all links to each other, with first air cooler, defeated air compressor outward that the second air cooler all links to each other. The utility model discloses an use multistage separation, manyStage precooling improves the reflux at the top of the demethanizer, applies multi-strand reflux to greatly improve the temperature distribution and mass transfer effect at the upper part of the demethanizer, improves the ethane recovery rate and improves the CO at the upper part of the demethanizer2Freezing and blocking the residual quantity.

Description

Multi-strand backflow ethane recovery device
Technical Field
The utility model relates to a natural gas treatment process technical field specifically is a stranded backward flow ethane recovery unit.
Background
In recent years, with the continuous development of natural gas treatment technology, a natural gas condensate recovery process mainly based on expansion machine refrigeration is rapidly developed, the expansion machine refrigeration process obtains enough cold energy by using the pressure difference of raw material gas, the larger the expansion ratio is, the more the cold energy obtained by a condensate recovery system is, and the higher the condensate recovery rate is.
The existing typical ethane recovery flow diagram is shown in fig. 2, the flow is that the raw material gas enters a low-temperature separator after the raw material gas meets the heat exchange of a cold heat exchanger for cooling, the gas phase of the low-temperature separator is divided into two paths, the first path of gas is sent to the middle part of a demethanizer after being expanded, depressurized and cooled by an expander, and the second path of gas is sent to the middle upper part of the demethanizer after being subjected to the heat exchange of the cold heat exchanger for pressure regulation and temperature reduction; the liquid phase of the low-temperature separator enters the middle lower part of the demethanizer after being depressurized and cooled. Part of the externally conveyed dry gas is refluxed, subjected to heat exchange by a cold heat exchanger, reduced in pressure and temperature, and then enters the top of the demethanizer.
For medium-pressure (4 MPa-6 MPa) raw material gas, the process needs to obtain higher ethane recovery rate (higher than 94%), and only the reflux quantity of the external gas is continuously increased, but the top tower plate of the demethanizer can generate CO2Freezing and blocking, and increasing the power consumption of the external gas transmission compressor, thereby increasing the main body energy consumption of the ethane recovery device.
In order to overcome the defects of the typical ethane recovery flow (figure 2), control the freezing and blocking problem of the demethanizer and reduce the main energy consumption of the ethane recovery device, a device for recovering the medium-pressure natural gas ethane with high ethane recovery rate is urgently needed to solve the problems of high energy consumption and freezing and blocking of the demethanizer under the high ethane recovery rate.
Disclosure of Invention
The utility model discloses a combine together multistage separation, stranded backward flow technique, provide a stranded backward flow ethane recovery unit, this method is effective to improve the ethane rate of recovery to more than 94%, has reduced the main part device energy consumption simultaneously and has solved and has restrained carbon dioxide and has frozen stifled problem.
In order to solve the technical problem, the utility model provides a such stranded backward flow ethane recovery unit, as shown in figure 1, including raw material gas precooling heat exchanger, one-level low temperature separator, one-level supercooling heat exchanger, second grade low temperature separator, second grade supercooling heat exchanger, demethanizer, outer gas transmission compressor, the second air cooler, first air cooler, still include with raw material gas precooling heat exchanger, the expander set, the equal continuous one-level low temperature separator of one-level supercooling heat exchanger, with one-level supercooling heat exchanger, second grade supercooling heat exchanger, the equal continuous second grade low temperature separator of demethanizer, with first air cooler, the equal continuous outer gas transmission compressor of second air cooler.
As a further improvement, the feed gas precooling heat exchanger is connected with a first-stage low-temperature separator, and a gas phase separated by the first-stage low-temperature separator is connected with an expansion unit and the middle part of a demethanizer.
As a further improvement, the liquid phase separated by the first-stage low-temperature separator is output in two paths, and the first path of liquid phase is mixed into the gas phase of the first-stage low-temperature separator and is connected with the first-stage supercooling heat exchanger and the second-stage low-temperature separator; the second liquid phase is connected with the bottom of the demethanizer. As a further improvement, the first path of liquid phase flow of the first-stage low-temperature separator accounts for 6-18% of the liquid phase flow of the separated liquid phase of the first-stage low-temperature separator.
As a further improvement, the secondary low-temperature separator separates the gas phase and is connected with the secondary supercooling heat exchanger and the upper part of the demethanizer; the separated liquid phase of the second-stage low-temperature separator is connected with the middle upper part of the demethanizer; the demethanizer overhead gas phase is sequentially communicated with a secondary supercooling heat exchanger, a primary supercooling heat exchanger, a raw material gas precooling heat exchanger, an expansion unit compression end, a first air cooler, an external gas transmission compressor and a second air cooler.
As a further improvement, the gas phase at the outlet of the second air cooler is divided into two paths, and the first path of gas phase is connected with the top of the feed gas precooling heat exchanger, the first-stage supercooling heat exchanger, the second-stage supercooling heat exchanger and the demethanizer; the second path of gas phase is output as the output dry gas.
As a further improvement, the first path of gas phase flow of the air cooler outlet gas phase accounts for 6-28% of the air cooler outlet gas phase flow.
The utility model has the advantages that:
(1) the multistage separation and multi-strand reflux precooling are adopted to improve the temperature and component distribution at the upper part of the demethanizer, improve the content of methane components in reflux gas, and reduce the above-ethane heavy components and CO in reflux2Content effectively solves CO2Freezing and blocking problems are solved, and the ethane recovery rate is greatly improved;
(2) on the premise of ensuring high ethane recovery rate and high output pressure, the energy consumption of the ethane recovery main body device is greatly reduced, and the economic benefit is greatly improved.
Drawings
FIG. 1 is a process flow diagram of the present invention
Shown in FIG. 1: e11-raw material gas precooling heat exchanger, E12-first-stage supercooling heat exchanger, V11-first-stage low-temperature separator, K11-expansion end of expansion unit, T11-demethanizer, E13-second-stage supercooling heat exchanger, V12-second-stage low-temperature separator, K11-compression end of expansion unit, A11-first air cooler, K12-external gas compressor, A12-second air cooler and E14-demethanizer bottom reboiler.
FIG. 2 is a flow diagram of a typical prior art ethane recovery process
Shown in FIG. 2: e21-raw material gas precooling heat exchanger, E22-supercooling heat exchanger, V21-low temperature separator, K21-expansion end of expansion unit, T21-demethanizer, K22-compression end of expansion unit, A21-air cooler and E23-demethanizer bottom reboiler.
FIG. 3 is a process flow diagram of example 1
Shown in FIG. 3: e31-raw material gas precooling heat exchanger, E32-first-stage supercooling heat exchanger, V31-first-stage low-temperature separator, K31-expansion unit expansion end, T31-demethanizer, E33-second-stage supercooling heat exchanger, V32-second-stage low-temperature separator, K31-expansion unit compression end, A31-first air cooler, K32-external gas compressor, A32-second air cooler, E34-demethanizer bottom reboiler, P31-demethanizer bottom pump, T32-deethanizer, E34-cooler, V33-deethanizer reflux tank, P32-deethanizer reflux pump, and E36-deethanizer bottom reboiler.
Detailed Description
The technical solutions in the embodiments of the present invention are fully described in detail below with reference to fig. 3 in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
Example one
The embodiment 1 of the utility model is as shown in the attached figure 3, the material gas quality composition and the calculation basic data are as follows:
scale of raw material gas treatment: 1000X 104m3/d
Raw material gas pressure: 6MPa
The station entering temperature is as follows: 20 deg.C
Dry gas output pressure: not less than 6.0MPa
Ethane product export pressure: not less than 2MPa
Adiabatic efficiency of the compressor: 75% (including external compressor, refrigeration compressor, expander set supercharging end)
Isentropic efficiency of expansion end of expansion unit: 85 percent of
The feed gas composition is shown in table 1.
TABLE 1 feed gas composition
Components N2 CO2 C1 C2 C3 iC4
mol％ 1.4301 0.9030 89.2415 6.2903 1.3901 0.2530
Components nC4 iC5 nC5 C6 C7 -
mol％ 0.2670 0.0790 0.0610 0.0460 0.0390 -
As shown in figure 3, the utility model discloses a multi-reflux natural gas ethane recovery method, the raw gas (6MPa, 20 ℃) entering the ethane recovery device enters the raw gas precooling heat exchanger E31 for cooling and then enters the first-level low-temperature separator V31, the liquid phase of the first-level low-temperature separator V31 is depressurized to (2.60MPa, -76.44 ℃) and enters the middle-lower part of the demethanizer T31; the gas phase (5.94MPa and 51 ℃) of the first-stage low-temperature separator V31 is divided into two paths, wherein the first path (the flow accounts for 79% of the total flow of the gas phase of the first-stage low-temperature separator V31) enters the middle upper part of a demethanizer T31 through the pressure reduction and temperature reduction (2.60MPa and 83.4 ℃) of the expansion end of an expander set K31; the other path of the heat exchange is cooled by the primary supercooling heat exchanger E32 (5.92 MPa-67.4 ℃) and then is depressurized to (5.1 MPa-72.3 ℃) and enters a secondary low-temperature separator V32; the gas phase of the secondary low-temperature separator V32 is subjected to heat exchange and temperature reduction by a secondary supercooling heat exchanger E33 (4.99MPa and 96.2 ℃) and then is subjected to pressure reduction until the pressure is reduced to (2.60MPa and 102.7 ℃) and then enters the upper part of a demethanizer T31; the liquid phase from the two-stage cryogenic separator V32 was depressurized (2.60MPa, -93.46 deg.C) to enter the upper portion of demethanizer T31.
Refluxing partial gas phase (gas flow accounts for 8.86% of total gas phase flow at the outlet of the second air cooler A32) at the outlet of the second air cooler A32, and allowing the gas phase to enter the top of a demethanizer T31 after being cooled, depressurized and adjusted by a feed gas precooling heat exchanger E31, a primary supercooling heat exchanger E32 and a secondary supercooling heat exchanger E33 (2.6 MPa-103.7 ℃); the gas phase at the top of the demethanizer T31 is subjected to heat exchange through a secondary supercooling heat exchanger E33, a primary supercooling heat exchanger E32 and a raw material gas precooling heat exchanger E31 to 16.5 ℃, then sequentially enters a pressurizing end of a first expansion unit K31 for pressurization (2.98MPa and 31.56 ℃), is cooled and cooled by a first air cooler A31 and is pressurized to (6.1MPa and 42.45 ℃) by an external gas compressor K32, is cooled by a second air cooler A32 and then enters an external natural gas pipeline for external transportation, and the flow of external gas is 912 multiplied by 104m3D; three liquid flows are respectively extracted from the middle lower part and the bottom of a demethanizer T31 for side reboiling, wherein liquid flow with the flow rate of 39983kg/h extracted from the middle lower part (2.58MPa, -82.27 ℃) is heated to-58 ℃ by a raw material gas precooling heat exchanger E31 and then flows back to the demethanizer T31, liquid flow with the flow rate of 47092kg/h extracted from the lower part (2.59MPa, -63.25 ℃) is heated to-41 ℃ by a raw material gas precooling heat exchanger E31 and then flows back to the demethanizer T31, liquid flow with the flow rate of 47619kg/h extracted from the bottom part (2.60MPa, -6.13 ℃) is heated to 5.8 ℃ by a raw material gas precooling heat exchanger E31 and then flows back to the demethanizer T31; liquid hydrocarbon (2.60MPa and 9.35 ℃) fractionated from the bottom of a demethanizer T31 is subjected to pressure regulation and then is sent to a deethanizer at 2.65MPa and 9.76 ℃, gas phase (2.5MPa and-1.08 ℃) from the top of a deethanizer T32 is divided into two paths, wherein the first path is used as an ethane product, the flow of the first path accounts for 56% of the total flow of the gas phase at the top of the deethanizer, the second path is cooled to-9 ℃ by a cooler E35 and then enters a deethanizer reflux tank V33, and liquid phase (2.5MPa and-9 ℃) separated from the deethanizer reflux tank V33 is subjected to pressure regulation by a deethanizer reflux pump P32 at 2.6MPa and-8.7 ℃) and then flows back to the top of the deethanizer T32; the liquid hydrocarbon (2.55MPa, 97.83 ℃) fractionated from the bottom of the deethanizer T32 is a condensate containing propane and heavy components above propane (the molar content of ethane is 1 percent), and the yield of the condensate is 18720 kg/h. According to the product variety and quality requirementsThe product is separated into the required products by distillation and cutting. The ethane recovery rate of the condensate recovery device was 95.0%.
The utility model provides an ethane recovery technology of high-pressure natural gas compares with current typical ethane recovery flow, improves ethane rate of recovery 2.8%, increases ethane product volume 4278.9 t/a. The power of the propane refrigeration compressor is reduced by 487.2kW, the compression power consumption of the main device is reduced by 1.5%, and the energy of the ethane recovery device is remarkably saved.
The above description is not intended to limit the present invention in any way, and the present invention has been disclosed in the above embodiments, but not intended to limit the present invention, and any person skilled in the art can make some changes or modify equivalent embodiments with equivalent changes when using the technical content disclosed above without departing from the technical scope of the present invention.

Claims (8)

1. The multi-strand reflux ethane recovery device comprises a raw material gas precooling heat exchanger, a first-stage low-temperature separator, a first-stage supercooling heat exchanger, a second-stage low-temperature separator, a second-stage supercooling heat exchanger, a demethanizer, an external gas transmission compressor and a second air cooler, and is characterized by further comprising a first air cooler, a first-stage low-temperature separator, a second-stage low-temperature separator and an external gas transmission compressor, wherein the first-stage low-temperature separator is connected with the raw material gas precooling heat exchanger, an expansion unit and the first-stage supercooling heat exchanger, the second-stage low-temperature separator is connected with the first-stage supercooling heat exchanger, the second-stage supercooling heat exchanger and the demet.
2. A multistrand reflux ethane recovery plant as claimed in claim 1, wherein: the feed gas precooling heat exchanger is connected with the first-stage low-temperature separator, and the gas phase separated by the first-stage low-temperature separator is connected with the expansion unit and the middle part of the demethanizer.
3. The multi-strand reflux ethane recovery device according to claim 1, wherein the liquid phase separated by the first-stage low-temperature separator is output in two paths, and the first liquid phase is mixed into the gas phase of the first-stage low-temperature separator and is connected with the first-stage supercooling heat exchanger and the second-stage low-temperature separator; the second liquid phase is connected with the bottom of the demethanizer.
4. The multi-stream reflux ethane recovery device as claimed in claim 1, wherein the first liquid phase flow rate of the first cryogenic separator accounts for 6-18% of the liquid phase flow rate of the separated liquid phase of the first cryogenic separator.
5. The multi-stream reflux ethane recovery apparatus as claimed in claim 1, wherein the second cryogenic separator separates the gas phase and is connected to the second subcooling heat exchanger and the upper part of the demethanizer; the separated liquid phase of the second-stage low-temperature separator is connected with the middle upper part of the demethanizer; the demethanizer overhead gas phase is sequentially communicated with a secondary supercooling heat exchanger, a primary supercooling heat exchanger, a raw material gas precooling heat exchanger, an expansion unit compression end, a first air cooler, an external gas transmission compressor and a second air cooler.
6. The multi-strand reflux ethane recovery device according to claim 1, wherein the gas phase at the outlet of the second air cooler is divided into two paths, and the first path of gas phase is connected with the top of the raw material gas precooling heat exchanger, the first stage supercooling heat exchanger, the second stage supercooling heat exchanger and the demethanizer; the second path of gas phase is output as the output dry gas.
7. The multi-stream reflux ethane recovery apparatus as recited in claim 1, wherein the first stream of the air cooler outlet gas phase flow rate is 6% to 28% of the air cooler outlet gas phase flow rate.
8. The multi-strand reflux ethane recovery device according to claim 1, wherein two side line reboilers and one side line reboiler are respectively arranged at the middle lower part and the bottom part of the demethanizer to provide cold energy for the raw material gas precooling heat exchanger, and the raw material gas precooling heat exchanger is connected with an external refrigeration cycle.
CN201920993041.3U 2019-06-28 2019-06-28 Multi-strand backflow ethane recovery device Expired - Fee Related CN210569510U (en)

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