CN212538461U - Take multistage separation to be applicable to propane recovery unit of super rich gas - Google Patents

Take multistage separation to be applicable to propane recovery unit of super rich gas Download PDF

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Publication number
CN212538461U
CN212538461U CN202021445594.4U CN202021445594U CN212538461U CN 212538461 U CN212538461 U CN 212538461U CN 202021445594 U CN202021445594 U CN 202021445594U CN 212538461 U CN212538461 U CN 212538461U
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China
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tower
temperature separator
cold
propane
rich gas
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CN202021445594.4U
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Chinese (zh)
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黄靖珊
蒋洪
王再伟
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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
    • F25J3/0242—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 3 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
    • F25J3/0247—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 4 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • F25J2200/08—Processes or apparatus using separation by rectification in a triple 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
    • F25J2200/74—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons

Abstract

The utility model discloses a take propane recovery unit of multistage separation to be applicable to super rich gas, including main cold box, one-level low temperature separator, reabsorption tower, deethanization tower, expansion unit, deethanization tower reboiler, deethanization tower top reflux pump, air cooler, still include the second grade low temperature separator that is connected with one-level low temperature separator, with the reflux drum that deethanization tower top of the tower is connected, the supercooling cold box that is connected with the heavy contact tower. The device of the utility model is simple in structure, guarantee the light hydrocarbon and retrieve the quality, improve the propane rate of recovery, the propane rate of recovery is more than 98%, and the device improves light hydrocarbon and retrieves economic benefits under the low energy consumption condition.

Description

Take multistage separation to be applicable to propane recovery unit of super rich gas
Technical Field
The utility model relates to a natural gas lime set retrieves technical field, especially relates to a take propane recovery unit that multistage separation is applicable to super rich gas.
Background
With the development of natural gas industrial technology, oil and gas field enterprises realize economic benefits and social benefits brought by a light hydrocarbon recovery process, and pay great attention to the construction of a propane recovery project. The most typical propane recovery flow scheme currently in domestic use is a direct heat exchange flow scheme as shown in figure 2. The process includes pre-cooling material gas in the main cold box, separating liquid phase in the low temperature separator, separating gas phase in the lower part of the deethanizing tower, separating gas phase in the heavy contact tower, and heat exchange of the overhead material flow in the heavy contact tower. The process mainly realizes the recovery of propane and the components above propane in the natural gas through the refrigeration of an expander. The method is characterized in that condensate at the bottom of the heavy contact tower directly enters a deethanizer, and a reflux tank is not arranged at the top of the deethanizer, so that propane entering the heavy contact tower and hydrocarbon components above the propane are increased, and the condensation absorption effect of the heavy contact tower is seriously influenced. When the raw material gas is richer, more raw material gas precooling amount is needed for propane recovery, so that the refrigeration load is increased, and the energy consumption of the compressor is increased.
In order to overcome the defects of the processes, reduce the energy consumption of a propane recovery device system and improve the recovery rate of propane, a medium-pressure rich-gas propane recovery device suitable for raw material gas with rich quality is urgently needed.
SUMMERY OF THE UTILITY MODEL
The utility model discloses make the improvement to the problem that above-mentioned exists, promptly the utility model aims to solve the technical problem that a take propane recovery unit that multistage separation is applicable to super rich gas is provided, the device can improve the propane rate of recovery, adopts the reducible feed gas precooling volume of two-stage separation, reduces the cryogenic cold volume consumption of propane to the cold volume of minimum consumes the condensation and goes out more heavy hydrocarbon, and the heat integration effect improves in the cold box, and compressor power consumption further reduces, and propane recovery unit's economic benefits obtains effectively promoting.
In order to solve the technical problem, the utility model provides a such take propane recovery unit of multistage separation be applicable to super rich gas, as shown in figure 1, including main cold box, one-level low temperature separator, reabsorption tower, deethanizer, expansion unit, deethanizer reboiler, deethanizer overhead reflux pump, air cooler, its characterized in that still includes the second grade low temperature separator who is connected with one-level low temperature separator, the reflux drum that is connected with the deethanizer top of the tower, the supercooling cold box that is connected with the heavy contact tower.
As a further improvement, the top of the deethanizer is connected with a supercooling cold box and a reflux tank, the gas phase of the reflux tank is connected with the supercooling cold box and the top of the heavy contact tower, and the liquid phase of the reflux tank is connected with a reflux pump and the top of the deethanizer.
As a further improvement, the bottom of the heavy contact tower is connected with a booster pump, a supercooling cold box and the middle upper part of the deethanizer.
As a further improvement, the main cooling box adopts a multi-strand plate-fin heat exchanger, the integrated exchange cold and heat flow is two heat flows and three cold flows, and the super-cooling box is used for integrating the two heat flows and the two cold flows in the cooling box.
As a further improvement, two hot flows of the main cold box are respectively a raw material gas and a gas phase from the top of the first-stage low-temperature separator, three cold flows are respectively a material flow from the top of the heavy contact tower through the cold box, a liquid flow from the bottoms of the two low-temperature separators, and propane refrigerating capacity is added.
As a further improvement, the two hot material flows of the supercooling cold box are respectively a material flow coming out of the top of the deethanization tower, a gas phase material flow of a reflux tank, the two cold material flows are respectively a material flow coming out of the top of the heavy contact tower, and a material flow coming out of the bottom of the heavy contact tower and pressurized by a pump.
As a further improvement, the gas phase of the first-stage low-temperature separator is connected with the second-stage low-temperature separator through a main cooling box, and the liquid phase of the first-stage low-temperature separator and the liquid phase of the second-stage low-temperature separator are mixed through a throttle valve and are connected with the deethanizer through the main cooling box.
As a further improvement, the gas phase separated by the first-stage low-temperature separator accounts for 60-70% of the total flow.
The utility model has the advantages that:
(1) two low-temperature separators are added in front of the heavy contact tower, two-stage separation is adopted, the refrigeration consumption of the added propane is reduced, more heavy hydrocarbons are condensed out by less cold energy, the pre-cooling capacity of the raw material gas is reduced, and the energy consumption of a main device is reduced;
(2) the device adopts the multi-strand plate-fin heat exchanger, fully utilizes the heat source of the raw material gas, and the condensate at the bottom of the heavy contact tower enters the supercooling cold box for heat exchange to provide cold energy, so that compared with the conventional propane recovery process, the device improves the cold and heat utilization rate, improves the heat integration effect, and effectively reduces the cooling public engineering load of refrigerant circulation;
(3) the device has the advantages of simple process flow, easy operation, compact structural arrangement, less equipment investment and low engineering investment cost.
(4) Under the condition that the recovery rate of propane is higher than 98%, the system energy consumption is reduced, and the economic benefit of enterprises is increased.
Drawings
FIG. 1 is a process flow diagram of the present invention;
in the figure, a main cooling box-1, a primary low-temperature separator-2, a secondary low-temperature separator-3, an expansion unit-4, a heavy contact tower-5, a pump-6, a supercooling cooling box-7, a reflux tank-8, a reflux pump-9, a deethanizer-10, a reboiler-11, a turboexpander compression end-12 and an air cooler-13.
FIG. 2 is a flow chart of a propane recovery process which is currently most widely used in China;
shown in FIG. 2 are a cold box-1, a low temperature separator-2, an expander train-3, a heavy contact column-4, a pump-5, a deethanizer-6, an air cooler-7, an expander compressor-8, and a reboiler-9.
Fig. 3 is a process flow diagram of an embodiment of the invention;
as shown in figure 3, a main cooling box-1, a primary low-temperature separator-2, a secondary low-temperature separator-3, an expansion unit-4, a heavy contact tower-5, a pump-6, a sub-cooling box-7, a reflux tank-8, a reflux pump-9, a deethanizer-10, a reboiler-11, a turboexpander compression end-12, an air cooler-13, a debutanizer-14, a debutanizer reflux pump-15, an air cooler-16, a debutanizer reflux tank-17, coolers-18 and 20 and a debutanizer reboiler-19.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to fig. 1 in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example one
As shown in fig. 1, the gas composition and working conditions of the feed gas are as follows:
scale of raw material gas treatment: 100 x 104m3/d
Raw material gas pressure: 5.1MPa
The station entering temperature is as follows: 30 deg.C
Dry gas output pressure: 6.1MPa
The composition of the feed gas is shown in Table 1
TABLE 1 feed gas composition
Composition of N2 CO2 C1 C2 C3 iC4 nC4
mol％ 1.0603 1.7672 76.5787 10.2498 6.3619 1.4138 1.7672
Composition of iC5 nC5 C6 C7 C8 C9 C10
mol％ 0.2828 0.2592 0.12 0.11 0.02 0.01 _
As shown in figure 3, the utility model discloses an ethane recovery process with multi-stage separation, the raw material gas (5.1MPa, 30 ℃) enters into a first-stage low-temperature separator 2 for gas-liquid separation after being cooled by a main cooling box 1, and the separated gas phase (4.10MPa, -48 ℃) of the first-stage low-temperature separator 2 enters into a second-stage low-temperature separator 3 after being refrigerated by the main cooling box (2.95MPa, -78.17 ℃). The gas phase of the second-stage low-temperature separator 3 enters the bottom of the heavy contact tower 5 through the refrigeration of an expansion end of a turboexpander 4 (1.8MPa and 63.45 ℃). The liquid phases at the bottom ends of the first-stage low-temperature separator 2 and the second-stage low-temperature separator 3 are mixed and regulated to (2.2MPa, -32.16 ℃) and then are subjected to heat exchange and temperature rise (2.18MPa, 25 ℃) by the main cooling box 1, and then the middle part of the deethanizer 10 is obtained. The gas phase discharged from the top of the heavy contact tower 5 (1.78MPa and-73.63 ℃) is heated to (1.76MPa and-37.08 ℃) through a cold box 7, then heated to 24.91 ℃ through a main cold box 1, compressed 12(6.15MPa and 145.3 ℃) through an expansion unit, cooled to 50 ℃ through an air cooler 13, and then enters an external natural gas pipeline for external transportation (6.13MPa and 50 ℃). The liquid phase (1.8 MPa-66.8 ℃) at the bottom of the heavy contact tower 5 is pressurized to 2.0MPa by a pump, enters a supercooling cold box, is heated to-25 ℃ and enters the middle upper part of the deethanizer 10. The gas phase discharged from the top of the deethanizer 10 is cooled to-32 ℃ through a cold box 7 and enters a reflux tank. The gas phase discharged from the reflux tank 8 (1.92MPa and 32 ℃) is cooled to-70 ℃ through a cold box 7 and then flows back from the top of the heavy contact tower 5 through a throttle valve (1.8MPa and 71.7 ℃), and the flow accounts for 75 percent of the total flow. The liquid phase discharge (1.92 MPa-32 ℃) of the reflux tank 8 is pressurized to 2.0MPa by a pump and is used as the top reflux of the deethanizer 10. The condensate (2.0MPa, 71.7 ℃) from the bottom of the deethanizer 10 is condensate containing propane and heavy components above propane, the propane yield (4821.24kg/h) is high, and the propane recovery rate is 99.02%.
The condensed liquid at the bottom of the deethanization 10 tower enters the middle upper part of a debutanizer 14 after being depressurized by a throttle valve (1.7MPa, 64.39 ℃), the gas phase discharge (1.6MPa, 67.43 ℃) at the top of the debutanizer 14 is cooled to 50 ℃ by an air cooler 16 and enters a reflux tank 17, the liquid phase discharge (1.59MPa, 50 ℃) of the reflux tank 17 is pressurized to 1.7MPa by a pump 15 and is divided into two parts: one enters the top of a debutanizer 14 after being depressurized by a throttle valve (1.65MPa, 50.13 ℃), and the flow of the debutanizer accounts for 40 percent of the liquid phase flow of a reflux tank; one is cooled to 40 ℃ by water and used as liquefied petroleum gas (1.2MPa, 39.89 ℃) for outward transportation. The liquid phase discharge (1.65MPa, 149.6 ℃) at the bottom of the debutanizer 14 is cooled to 40 ℃ by water and used as stable light hydrocarbon for outward transportation.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the present invention in any way, and it is not intended to limit the present invention to the embodiments disclosed herein, and modifications, variations or alterations can be made on the technical content disclosed above by those skilled in the art without departing from the scope of the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention are all encompassed within the protective scope of the present invention.

Claims (8)

1. The utility model provides a take multistage separation propane recovery unit suitable for super rich gas, includes main cold box, one-level low temperature separator, reabsorption tower, deethanization tower, expander set, deethanization tower reboiler, deethanization tower overhead reflux pump, air cooler, its characterized in that still includes the second grade low temperature separator who is connected with one-level low temperature separator, the reflux drum that is connected with the deethanization tower top, the subcooling cold box that is connected with the heavy contact column.
2. The propane recovery apparatus with multi-stage separation suitable for ultra-rich gas according to claim 1, wherein the deethanizer is connected to the subcooling cooling tank and the reflux drum, the reflux drum is connected to the subcooling cooling tank and the top of the heavy contact column in gas phase, and the reflux drum is connected to the reflux pump and the top of the deethanizer in liquid phase.
3. The propane recovery device with multi-stage separation suitable for super-rich gas according to claim 1, wherein the bottom of the heavy contact tower is connected with a booster pump, a supercooling cold box and the middle-upper part of the deethanizer.
4. The propane recovery device with multi-stage separation function suitable for the ultra-rich gas as claimed in claim 1, wherein the main cooling box adopts a multi-strand plate-fin heat exchanger, the integrated exchange cold and heat flow is composed of two hot flows and three cold flows, and the sub-cooling box is used for integrating the two hot flows and the two cold flows in the cooling box.
5. The propane recovery device with multi-stage separation and suitable for ultra-rich gas as claimed in claim 1, wherein the two hot streams of the main cold box are respectively the raw gas and the gas phase from the top of the first-stage low-temperature separator, the three cold streams are respectively the stream from the top of the heavy contact tower through the cold box, the liquid stream from the bottom of the two low-temperature separators, and the refrigeration capacity of propane is added.
6. The propane recovery device with multi-stage separation suitable for ultra-rich gas of claim 1, wherein the two hot streams of the sub-cooling cold box are respectively the stream coming out from the top of the deethanizer, the gas phase stream of the reflux tank, the two cold streams are respectively the stream coming out from the top of the heavy contact tower, and the stream coming out from the bottom of the heavy contact tower is pressurized by a pump.
7. The propane recovery device with multi-stage separation and suitable for ultra-rich gas as claimed in claim 1, wherein the gas phase of the first-stage low-temperature separator is connected with the second-stage low-temperature separator through a main cooling box, and the liquid phase of the first-stage low-temperature separator and the liquid phase of the second-stage low-temperature separator are mixed under pressure and are connected with the deethanizer through the main cooling box.
8. The propane recovery device with multi-stage separation and suitable for super-rich gas according to claim 1, wherein the gas phase separated by the first-stage low-temperature separator accounts for 60-70% of the total flow.
CN202021445594.4U 2020-07-21 2020-07-21 Take multistage separation to be applicable to propane recovery unit of super rich gas Expired - Fee Related CN212538461U (en)

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CN202021445594.4U CN212538461U (en) 2020-07-21 2020-07-21 Take multistage separation to be applicable to propane recovery unit of super rich gas

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114992983A (en) * 2022-03-21 2022-09-02 江苏卓然恒泰低温科技有限公司 Low-temperature separation cold box for propane dehydrogenation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114992983A (en) * 2022-03-21 2022-09-02 江苏卓然恒泰低温科技有限公司 Low-temperature separation cold box for propane dehydrogenation

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