CN115597309B - Propane dehydrogenation product separation method and system - Google Patents

Propane dehydrogenation product separation method and system Download PDF

Info

Publication number
CN115597309B
CN115597309B CN202211291585.8A CN202211291585A CN115597309B CN 115597309 B CN115597309 B CN 115597309B CN 202211291585 A CN202211291585 A CN 202211291585A CN 115597309 B CN115597309 B CN 115597309B
Authority
CN
China
Prior art keywords
reaction gas
product
separation
cooling
exchange device
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202211291585.8A
Other languages
Chinese (zh)
Other versions
CN115597309A (en
Inventor
曹运兵
侯丽丽
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Zhongke Hongneng Beijing Technology Co ltd
Original Assignee
Zhongke Hongneng Beijing Technology Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Zhongke Hongneng Beijing Technology Co ltd filed Critical Zhongke Hongneng Beijing Technology Co ltd
Priority to CN202211291585.8A priority Critical patent/CN115597309B/en
Publication of CN115597309A publication Critical patent/CN115597309A/en
Application granted granted Critical
Publication of CN115597309B publication Critical patent/CN115597309B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
    • 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
    • F25J3/0242—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
    • F25J3/0252—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
    • F25J2200/70—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
    • 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
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression 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
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses a separation method and a separation system of a propane dehydrogenation product, wherein the separation method comprises the following steps: pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas; drying and purifying the first reaction gas to obtain a second reaction gas; introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment to respectively obtain a C3+ product and a third reaction gas; introducing the third reaction gas into a cryogenic separation system for cryogenic separation, separation and rewarming to obtain a hydrogen-rich product, a C2/C1 product and a C3 product respectively; the cryogenic separation system is provided with a heat exchange device which is used for absorbing the heat energy of the third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process. The invention can reduce the cold energy required to be provided by an external refrigeration cycle system, reduce the loss in the heat transfer process, and has the technical characteristics of low separation energy consumption, high economy, simple and convenient operation, high recovery rate and the like.

Description

Propane dehydrogenation product separation method and system
Technical Field
The invention belongs to the technical field of petrochemical separation, and particularly relates to a method and a system for separating a propane dehydrogenation product.
Background
The propane reserves in China are rich, and the development of shale gas in recent years further increases the yield of propane. At present, most of the propane in China is consumed in a combustion energy supply mode or even in a 'ceiling lamp' mode, so that the utilization value of the propane is greatly reduced. The conversion of propane into a product with high added value is one of key technologies for improving the utilization efficiency of propane and realizing the efficient utilization of carbon-based energy, and has wide practical prospect and great economic benefit. Among downstream products of propane, propylene is an important chemical raw material, and can be used for producing high added value products such as polypropylene, acrylonitrile, propylene oxide, ethylene propylene rubber, nylon 66, ABS resin and the like. Among them, polypropylene is widely used in people's daily life, so that propylene becomes the second largest chemical raw material next to ethylene. The propylene yield in China continuously rises from 2018 to 2020, but the propylene demand of downstream industries cannot be met, the propylene yield in China can reach 3300 ten thousand tons/year in 2022, the equivalent propylene demand can reach 3700 ten thousand tons/year, and a gap of the propylene downstream demand in China can be seen to be large in the future. The continuous rise of propylene demand and the massive propane by-product of shale gas revolution bring opportunities for the development of propane dehydrogenation technology.
At present, the domestic propane dehydrogenation devices all adopt UOP and Rums reaction processes, the separation units all adopt cryogenic separation of hydrogen and other components in reaction gas, the recovered other components are pumped to 3-3.5MPaG by a low-temperature pump, and then C2 and C3 in the reaction gas are separated by an ethane tower, steam heating is required at the bottom of the tower in the separation process, propylene refrigeration is required at the bottom of the tower, so that the energy consumption is very high. The cryogenic separation mostly adopts hydrogen expansion or cascade refrigeration, the operation is complex, and the propylene yield is very low under the condition of small load, such as the problem causes the increase of the operation cost.
The traditional expansion refrigeration process needs to liquefy and separate hydrogen from C2+ components which are easy to liquefy in raw material gas by isentropic expansion and cooling refrigeration of an expander, the liquefied C2 is boosted to 3-3.5MPaG by a hydrocarbon mixing pump and then is sent to a deethanizer through a heat exchanger for rewarming, the deethanizer adopts a high-pressure rectification mode to separate ethane, a large amount of steam is required to be consumed, the top of the deethanizer needs low-temperature precooling equipment to increase the recovery rate of propylene, the hydrogen after cryogenic separation expansion cannot meet the requirement of application due to pressure reduction, the hydrogen is used in a fuel gas mode, and resource waste is caused, and if hydrogen is required to be applied, the deethanizer needs to compress for secondary compression. In summary, it is known that the conventional expansion refrigeration process consumes a large amount of energy.
In the traditional cascade refrigeration process, a plurality of refrigeration compressors are needed to participate in circulating refrigeration (such as a propane compressor, an ethylene compressor, a methane compressor and the like), the cascade refrigeration has slightly higher recovery rate relative to an expansion refrigeration product, but the plurality of compressors are needed to be matched, the one-time investment is higher, and the recovered C2+ is possibly sent to a deethanizer by adopting a high-pressure hydrocarbon mixing pump, so that the cascade refrigeration only improves the recovery rate of the product, but the energy consumption problem is not fundamentally solved.
As those skilled in the art will appreciate, there is a need in the art for an improved low energy separation process and system for the dehydrogenation product of propane that overcomes the above disadvantages of the prior art.
Disclosure of Invention
It is an object of the present invention to provide a propane dehydrogenation product separation method and system that addresses the above-identified problems of the prior art.
In order to achieve the above object, on the one hand, the present invention adopts the following technical scheme: a process for separating a propane dehydrogenation product comprising the steps of:
step A, pressurizing and cooling a propane dehydrogenation product to obtain a first reaction gas;
step B, drying and purifying the first reaction gas to obtain a second reaction gas;
step C, introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment to respectively obtain a C3+ product and a third reaction gas;
step D, introducing the third reaction gas into a cryogenic separation system for cryogenic separation, separation and rewarming treatment to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system is provided with a heat exchange device, and the heat exchange device is used for absorbing the heat energy of third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process.
As an alternative design structure of the above technical solution, in step a, pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas includes: introducing a propane dehydrogenation product into a compression cooling system, performing pressurization treatment, and then, introducing the product into a circulating water cooler for cooling treatment to obtain first reaction gas.
As an optional design structure of the above technical solution, in step B, performing a drying and purifying treatment on the first reaction gas to obtain a second reaction gas includes: introducing the first reaction gas into a drying and purifying system, and removing water and trace mercury in the first reaction gas to obtain a second reaction gas.
As an optional design structure of the above technical solution, in step C, introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment, to obtain a c3+ product and a third reaction gas respectively includes: introducing the second reaction gas into a precooler of a precooling coarse separation system for precooling treatment, so that most of C3+ products in the second reaction gas are liquefied, wherein the precooling treatment adopts fresh propane to provide cold energy of a temperature zone of-17 ℃ to 20 ℃ for precooling the second reaction gas after the pressure of the fresh propane is reduced through a propane throttle valve; introducing the pre-cooled second reaction gas into a heavy hydrocarbon separator, purifying the liquid phase separated by the heavy hydrocarbon separator by a coarse separation tower, and obtaining a high-purity C3+ product; the gas phase separated by the heavy hydrocarbon separator and the crude separation tower is third reaction gas.
As an optional design structure of the above technical solution, in step D, introducing the third reaction gas into the cryogenic separation system to perform cryogenic, separation and rewarming processes, to obtain a hydrogen-rich product, a C2/C1 product, and a C3 product, respectively, includes: the third reaction gas is cooled by a heat exchange device and then is introduced into a first-stage separator of a cryogenic separation system, a liquid phase separated by the first-stage separator enters a light component removal tower, a gas phase separated by the first-stage separator is cooled by the heat exchange device and then enters a second-stage separator, a hydrogen-rich product is obtained after the gas phase separated by the second-stage separator is rewuped by the heat exchange device, the liquid phase separated by the second-stage separator enters the light component removal tower, a separation product of a tower top separator of the light component removal tower is rewuped by the heat exchange device and then a C2/C1 product is obtained, and a separation product of a reboiler of the light component removal tower is rewuped by the heat exchange device and then a C3 product is obtained.
As an optional design structure of the above technical scheme, the heat exchange device comprises a primary heat exchanger and a secondary heat exchanger, the primary heat exchanger is connected with a refrigeration cycle system, the secondary heat exchanger is connected with the refrigeration cycle system, the refrigeration cycle system is connected with a refrigerant supplementing system, and the refrigerant of the refrigerant supplementing system is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion; wherein the heat of the light ends column reboiler is provided by fresh propane; the heat of the reboiler of the crude separation column is provided by a refrigeration cycle system.
On the other hand, the invention adopts the following technical scheme: a propane dehydrogenation product separation system comprising:
the compression cooling system is used for pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas;
the drying and purifying system is used for drying and purifying the first reaction gas to obtain a second reaction gas;
the pre-cooling coarse separation system is used for pre-cooling and separating the second reaction gas to obtain a C3+ product and a third reaction gas respectively;
the cryogenic separation system is used for carrying out cryogenic, separation and rewarming treatment on the third reaction gas to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system is provided with a heat exchange device which is used for absorbing the heat energy of the third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process.
As an optional design structure of the above technical scheme, the heat exchange device further comprises a refrigeration cycle system, and the heat exchange device is connected with the refrigeration cycle system; the heat exchange device comprises a primary heat exchanger and a secondary heat exchanger, and the primary heat exchanger and the secondary heat exchanger are both connected with the refrigeration cycle system.
As an optional design structure of the technical scheme, the refrigeration cycle system comprises a compressor, an output pipeline and a backflow pipeline, wherein the input end of the output pipeline is connected with the compressor, the input end of the output pipeline penetrates through the heat exchange device to be connected with a throttle valve, the output end of the backflow pipeline is connected with the compressor, and the input end of the backflow pipeline penetrates through the heat exchange device to be connected with the throttle valve.
As an optional design structure of the technical scheme, the pre-cooling coarse separation system comprises a pre-cooler, a heavy hydrocarbon separator, a coarse separation tower reboiler and a propane throttle valve, wherein the pre-cooler is used for pre-cooling second reaction gas, fresh propane is used for pre-cooling the second reaction gas after being decompressed through the propane throttle valve to provide cold energy in a temperature zone of-17 ℃ to 20 ℃, the heavy hydrocarbon separator is used for separating the pre-cooled second reaction gas, and a liquid phase separated by the heavy hydrocarbon separator is purified through the coarse separation tower to obtain a high-purity C3+ product; the gas phase separated by the heavy hydrocarbon separator and the crude separation tower is third reaction gas.
As an optional design structure of the technical scheme, the cryogenic separation system comprises a first-stage separator, a second-stage separator, a light-removal tower reboiler and a light-removal tower top separator, wherein the first-stage separator is used for separating second reaction gas cooled by the first-stage heat exchanger, a liquid phase separated by the first-stage separator enters the light-removal tower, a gas phase separated by the first-stage separator enters the second-stage separator after being cooled by the second-stage heat exchanger, a hydrogen-rich product is obtained after the gas phase separated by the second-stage separator is subjected to rewarming by a heat exchange device, a liquid phase separated by the second-stage separator enters the light-removal tower, a C2/C1 product is obtained after the separation product of the light-removal tower top separator is subjected to rewarming by the heat exchange device, and a C3 product is obtained after the separation product of the light-removal tower reboiler is subjected to rewarming by the heat exchange device.
As an optional design structure of the above technical solution, the refrigeration cycle system is connected with a refrigerant supplementing system, and the refrigerant of the refrigerant supplementing system is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion.
The beneficial effects of the invention are as follows:
the invention provides a separation method and a separation system for propane dehydrogenation products, wherein a heat exchange device can absorb heat energy of third reaction gas in a cryogenic treatment process and release the heat energy in a rewarming treatment process, so that the cold energy required to be provided by an external refrigeration circulation system is reduced, a plurality of compressors are not required to be arranged, a deethanizer is directly integrated into the cryogenic separation system, the loss in the heat transfer process is reduced, ethane can be independently used as a product, and the whole process does not need steam heating, so that the separation method has the technical characteristics of low separation energy consumption, high economy, simplicity and convenience in operation, high recovery rate and the like.
Drawings
FIG. 1 is a flow chart of the operation of a process for separating a propane dehydrogenation product in one embodiment of the present invention;
fig. 2 is a flow chart of the operation of the pre-chill coarse separation system and the cryogenic separation system in one embodiment of the invention.
In the figure: 1-a compression cooling system; 2-a drying and purifying system; 3-pre-cooling the coarse separation system; 4-a cryogenic separation system; 5-a refrigeration cycle; 6-a refrigerant replenishment system; 301-precooler; 302-heavy hydrocarbon separator; 303-a crude separation column; 304-a crude separation column reboiler; 305-propane throttle valve; 401-primary heat exchanger; 402-a secondary heat exchanger; 403-first stage separator; 404-a secondary separator; 405-a light ends column reboiler; 406-a light ends removal column; 407-a light ends column overhead separator; 408-a throttle valve; 501-compressor.
Detailed Description
Examples
As shown in fig. 1 and 2, the present embodiment provides a propane dehydrogenation product separation system mainly including a compression cooling system 1, a drying and purifying system 2, a pre-cooling coarse separation system 3, a cryogenic separation system 4, a refrigeration cycle system 5, and a refrigerant replenishment system 6.
The air compression cooling system 1 is connected with the drying and purifying system 2, the drying and purifying system 2 is connected with the pre-cooling coarse separation system, the pre-cooling coarse separation system is connected with the cryogenic separation system 4, the refrigerating system is connected with the pre-cooling coarse separation system and the cryogenic separation system 4, the fresh propane is connected with the cryogenic separation system 4 and the pre-cooling coarse separation system, and the refrigerant supplementing system 6 is used for providing required refrigerant for the refrigerating circulation system 5.
The compression cooling system 1 is used for pressurizing and cooling the propane dehydrogenation product to obtain first reaction gas. The raw material gas from the boundary region is pressurized to 1MPaG-1.5MpaG by a reaction gas compressor of the compression cooling system 1. The reaction gas compressor can adopt a centrifugal compressor and a reciprocating compressor, and is provided with a corresponding auxiliary equipment separator water cooler and the like. The pressurized first reaction gas enters a circulating water cooler for cooling, and the cooled first reaction gas enters a drying and purifying system 2.
The drying and purifying system 2 is used for drying and purifying the first reaction gas to obtain a second reaction gas. The drying and purifying system 2 is used for removing the moisture in the first reaction gas by using a fixed bed drying agent, the drying and purifying system 2 is in a heating regeneration mode, the regeneration mode can be an isobaric regeneration mode or an open regeneration mode, and the drying and purifying system 2 can be used for removing the moisture, trace mercury and other components in the first reaction gas.
The pre-cooling coarse separation system 3 is used for pre-cooling and separating the second reaction gas to obtain a C3+ product and a third reaction gas respectively. The pre-cooling coarse separation system 3 comprises a pre-cooler 301, a heavy hydrocarbon separator 302, a coarse separation tower 303, a coarse separation tower reboiler 304 and a propane throttle valve 305, wherein the pre-cooler 301 is used for pre-cooling the second reaction gas, fresh propane is used for pre-cooling the second reaction gas after being depressurized through the propane throttle valve 305 to provide cold energy in a temperature zone of-17 ℃ to 20 ℃, the heavy hydrocarbon separator 302 is used for separating the pre-cooled second reaction gas, and a liquid phase separated by the heavy hydrocarbon separator 302 is purified by the coarse separation tower 303 to obtain a high-purity C3+ product; the gas phase separated from the heavy hydrocarbon separator 302 and the crude separation column 303 is the third reaction gas.
The cryogenic separation system 4 is used for carrying out cryogenic, separation and rewarming treatment on the third reaction gas to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system 4 is provided with a heat exchange device which is used for absorbing the heat energy of the third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process. The heat exchange device is connected with the refrigeration cycle system 5.
The heat exchange device comprises a primary heat exchanger 401 and a secondary heat exchanger 402, and the primary heat exchanger 401 and the secondary heat exchanger 402 are connected with the refrigeration cycle system 5. The refrigeration cycle system 5 comprises a compressor 501, an output pipeline and a return pipeline, wherein the input end of the output pipeline is connected with the compressor 501, the input end of the output pipeline passes through the heat exchange device and is connected with the throttle valve 408, the output end of the return pipeline is connected with the compressor 501, and the input end of the return pipeline passes through the heat exchange device and is connected with the throttle valve 408. The refrigeration cycle system 5 is connected with a refrigerant supplementing system 6, and the refrigerant of the refrigerant supplementing system 6 is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion. The compressor 501 of the refrigeration cycle 5 may be a centrifugal compressor, a reciprocating compressor, and a screw compressor. Compressor 501 discharge pressure may be operated between 1.8MPaG and 3.5 MPaG. The refrigeration cycle system 5 is connected with the pre-cooling coarse separation system 3 and the cryogenic separation system 4, and forms a cycle.
The cryogenic separation system 4 comprises a first-stage separator 403, a second-stage separator 404, a light-off tower 406, a reboiler 405 of the light-off tower and a separator 407 at the top of the light-off tower, wherein the first-stage separator 403 is used for separating the second reaction gas cooled by the first-stage heat exchanger 401, the liquid phase separated by the first-stage separator 403 enters the light-off tower 406, the gas phase separated by the first-stage separator 403 is cooled by the second-stage heat exchanger 402 and enters the second-stage separator 404, the gas phase separated by the second-stage separator 404 is rewarmed by a heat exchange device to obtain a hydrogen-rich product, the liquid phase separated by the second-stage separator 404 enters the light-off tower 406, the separated product of the separator 407 at the top of the light-off tower is rewarmed by the heat exchange device to obtain a C2/C1 product, and the separated product of the reboiler 405 is rewarmed by the heat exchange device to obtain a C3 product.
The heat exchange device can absorb the heat energy of the third reaction gas in the cryogenic treatment process and release the heat energy in the rewarming treatment process, reduces the cold energy required to be provided by the external refrigeration cycle system 5, does not need to arrange a plurality of compressors 501, directly integrates the deethanizer into the cryogenic separation system 4, reduces the loss in the heat transfer process, can independently serve as a product, does not need steam heating in the whole process, and has the technical characteristics of low separation energy consumption, high economy, simplicity and convenience in operation, high recovery rate and the like.
The embodiment also provides a separation method of the propane dehydrogenation product, which is applied to the separation system, and comprises the following steps:
step A, pressurizing and cooling a propane dehydrogenation product to obtain a first reaction gas, wherein the first reaction gas specifically comprises the following components: introducing a propane dehydrogenation product into the compression cooling system 1, performing pressurization treatment, and then, introducing the pressurized product into a circulating water cooler for cooling treatment to obtain first reaction gas.
Step B, drying and purifying the first reaction gas to obtain a second reaction gas, which specifically comprises the following steps: the first reaction gas is introduced into a drying and purifying system 2, and the moisture and trace mercury in the first reaction gas are removed to obtain a second reaction gas.
Step C, introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment to respectively obtain a C3+ product and a third reaction gas, wherein the method specifically comprises the following steps: introducing the second reaction gas into a precooler 301 of a precooling coarse separation system for precooling treatment, so that most of C3+ products in the second reaction gas are liquefied, wherein the precooling treatment adopts fresh propane to provide cold energy of a temperature zone of-17 ℃ to 20 ℃ for precooling after being depressurized by a propane throttle valve 305; introducing the pre-cooled second reaction gas into a heavy hydrocarbon separator 302, purifying the liquid phase separated by the heavy hydrocarbon separator 302 by a coarse separation tower 303, and obtaining a high-purity C3+ product; the gas phase separated from the heavy hydrocarbon separator 302 and the crude separation column 303 is the third reaction gas.
Step D, introducing the third reaction gas into a cryogenic separation system 4 for cryogenic separation, separation and rewarming treatment to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system 4 is provided with a heat exchange device for absorbing the thermal energy of the third reactant gas during the cryogenic treatment and releasing the thermal energy during the re-warming treatment.
Specifically, the heat exchange device comprises a primary heat exchanger 401 and a secondary heat exchanger 402, wherein the primary heat exchanger 401 is connected with a refrigeration cycle system 5, the secondary heat exchanger 402 is connected with the refrigeration cycle system 5, the refrigeration cycle system 5 is connected with a refrigerant supplementing system 6, and the refrigerant of the refrigerant supplementing system 6 is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion.
Wherein, introducing the third reaction gas into the cryogenic separation system 4 for cryogenic, separation and rewarming treatment to obtain a hydrogen-rich product, a C2/C1 product and a C3 product respectively comprises: the third reaction gas is cooled by a heat exchange device and then is introduced into a first-stage separator 403 of a cryogenic separation system 4, a liquid phase separated by the first-stage separator 403 enters a light component removal tower 406, a gas phase separated by the first-stage separator 403 is cooled by a first-stage heat exchanger 401 and then enters a second-stage separator 404, a hydrogen-rich product is obtained after the gas phase separated by the second-stage separator 404 is subjected to rewarming by the heat exchange device, the liquid phase separated by the second-stage separator 404 enters the light component removal tower 406, a separation product of a tower top separator 407 is subjected to rewarming by the second-stage heat exchanger 402 to obtain a C2/C1 product, and a separation product of a light component removal tower reboiler 405 is subjected to rewarming by the heat exchange device to obtain a C3 product. Wherein the heat of the light ends column reboiler 405 is provided by fresh propane.
The invention provides a separation method and a separation system for propane dehydrogenation products, wherein propane dehydrogenation raw gas is pressurized by a compression cooling system 1, the pressurized gas enters a circulating water cooler for cooling, the cooled gas enters a drying and purifying system 2 for removing moisture, trace mercury and the like in the gas, the dried and purified gas enters a pre-cooling coarse separation system 3, the pre-cooling coarse separation system mainly recovers cold energy released when fresh propane is depressurized, so that the gas after drying and purification is pre-cooled, most of C3+ products in the gas are liquefied, the pre-cooled gas enters a heavy hydrocarbon separator 302, and liquid phase components separated by the heavy hydrocarbon separator 302 enter a coarse separation tower 303 for purification and obtain high-purity C3+ products. The heat of the reboiler 304 of the crude separation tower is provided by the refrigeration cycle system 5, the gas phase at the top of the crude separation tower 303 and the gas phase at the top of the heavy hydrocarbon separator 302 enter the cryogenic separation system 4, the gas phase from the top of the crude separation tower 303 and the gas phase at the top of the heavy hydrocarbon separator 302 are continuously cooled through the first-stage heat exchanger 401, cooled gas enters the first-stage separator 403 of the cryogenic separation system 4, the liquid phase component separated by the first-stage separator 403 enters the light component removing tower 406, the gas phase separated by the first-stage separator 403 enters the second-stage heat exchanger 402 to be continuously cooled, cooled gas enters the second-stage separator 404, the gas phase separated by the second-stage separator 404 is subjected to re-heating through the second-stage heat exchanger 402 and the first-stage heat exchanger 401 to obtain hydrogen-rich gas, the hydrogen-rich gas is sent out of the boundary region to be continuously used, the liquid phase separated by the second-stage separator 404 is returned to the light component removing tower 406, the top separator 407 mainly generates light components such as ethane, such as main and a small amount of C1 products and hydrogen, and the like, and the gas is continuously used after being re-heated by the first-stage heat exchanger 401. The separation product of the light ends column reboiler 405 is mainly a C3 product, and the C3 product is sent out of the boundary region for further separation after being rewarmed by the primary heat exchanger 401, and the heat of the light ends column reboiler 405 is provided by fresh feed propane. The refrigerating capacity of the whole cryogenic separation system 4 is provided by the refrigeration cycle system 5, the core of the refrigeration cycle system 5 is composed of a mixed refrigerant compressor 501, the refrigerant is formed by mixing isopentane, propane, ethylene, methane and the like according to a certain proportion, the mixed refrigerant is compressed by the compressor 501, then is cooled by circulating water, passes through the crude separation tower 303 and provides heat required by separation for the refrigerant, the gas-liquid phase separated by the crude separation tower 303 enters the primary heat exchanger 401 and the secondary heat exchanger 402 respectively, is depressurized by a throttle valve 408, then is re-warmed and mixed by the secondary heat exchanger 402 and the primary heat exchanger 401, and returns to the compressor 501 again, and the whole refrigeration cycle is completed repeatedly.
In the description of the present invention, the specific features, structures, etc. described in the examples are included in at least one embodiment, and those skilled in the art may combine features of different embodiments without contradiction. The scope of the present invention is not limited to the above-described specific embodiments, and embodiments which can be suggested to those skilled in the art without inventive effort according to the basic technical concept of the present invention are all within the scope of the present invention.

Claims (10)

1. A process for separating a propane dehydrogenation product comprising the steps of:
step A, pressurizing and cooling a propane dehydrogenation product to obtain a first reaction gas;
step B, drying and purifying the first reaction gas to obtain a second reaction gas;
step C, introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment to respectively obtain a C3+ product and a third reaction gas;
step D, introducing the third reaction gas into a cryogenic separation system (4) for cryogenic, separation and rewarming treatment to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system (4) is provided with a heat exchange device, and the heat exchange device is used for absorbing the heat energy of third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process.
2. The process for separating a propane dehydrogenation product according to claim 1, wherein in the step a, the pressurizing and cooling treatment of the propane dehydrogenation product to obtain the first reaction gas comprises: introducing a propane dehydrogenation product into a compression cooling system (1), performing pressurization treatment, and then introducing the product into a circulating water cooler for cooling treatment to obtain a first reaction gas;
in the step B, the first reaction gas is subjected to drying and purifying treatment, and the second reaction gas is obtained by the following steps: introducing the first reaction gas into a drying and purifying system (2) to remove water and trace mercury in the first reaction gas and obtain a second reaction gas.
3. The method for separating a propane dehydrogenation product according to claim 1, wherein in the step C, introducing the second reaction gas into a pre-cooling coarse separation system for pre-cooling and separation treatment to obtain a c3+ product and a third reaction gas, respectively, comprises: introducing the second reaction gas into a precooler (301) of a precooling coarse separation system for precooling treatment, so that most of C3+ products in the second reaction gas are liquefied, wherein fresh propane is adopted for precooling the second reaction gas through cooling capacity of a temperature zone of-17 ℃ to 20 ℃ after decompression of a propane throttle valve (305); introducing the pre-cooled second reaction gas into a heavy hydrocarbon separator (302), and purifying the liquid phase separated by the heavy hydrocarbon separator (302) through a coarse separation tower (303) to obtain a high-purity C3+ product; the gas phase separated from the heavy hydrocarbon separator (302) and the crude separation column (303) is the third reaction gas.
4. A process for separating a propane dehydrogenation product according to claim 3, wherein in step D, introducing a third reactant gas into a cryogenic separation system (4) for cryogenic, separation and rewarming treatments to obtain a hydrogen-rich product, a C2/C1 product and a C3 product, respectively, comprises: the third reaction gas is cooled by a heat exchange device and then is introduced into a first-stage separator (403) of a cryogenic separation system (4), a liquid phase separated by the first-stage separator (403) enters a light component removing tower (406), a gas phase separated by the first-stage separator (403) is cooled by the heat exchange device and then enters a second-stage separator (404), a hydrogen-rich product is obtained after the gas phase separated by the second-stage separator (404) is rewarmed by the heat exchange device, the liquid phase separated by the second-stage separator (404) enters the light component removing tower (406), a C2/C1 product is obtained after the separation product of a light component removing tower top separator (407) is rewarmed by the heat exchange device, and a C3 product is obtained after the separation product of a light component removing tower reboiler (405) is rewarmed by the heat exchange device.
5. The propane dehydrogenation product separation method according to claim 4, characterized in that the heat exchange device comprises a primary heat exchanger (401) and a secondary heat exchanger (402), the primary heat exchanger (401) is connected with a refrigeration cycle system (5), the secondary heat exchanger (402) is connected with the refrigeration cycle system (5), the refrigeration cycle system (5) is connected with a refrigerant supplementing system (6), and a refrigerant of the refrigerant supplementing system (6) is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion; wherein the heat of the light ends column reboiler (405) is provided by fresh propane; the heat of the crude separation tower reboiler (304) is provided by the refrigeration cycle system (5).
6. A propane dehydrogenation product separation system, comprising:
the compression cooling system (1) is used for pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas;
the drying and purifying system (2) is used for drying and purifying the first reaction gas to obtain a second reaction gas;
the pre-cooling coarse separation system (3) is used for pre-cooling and separating the second reaction gas to obtain a C3+ product and a third reaction gas respectively;
the cryogenic separation system (4) is used for carrying out cryogenic separation and rewarming treatment on the third reaction gas to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; the cryogenic separation system (4) is provided with a heat exchange device which is used for absorbing the heat energy of the third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process.
7. The propane dehydrogenation product separation system according to claim 6, further comprising a refrigeration cycle system (5), the heat exchange device being connected to the refrigeration cycle system (5); the heat exchange device comprises a primary heat exchanger (401) and a secondary heat exchanger (402), and the primary heat exchanger (401) and the secondary heat exchanger (402) are connected with a refrigeration cycle system (5); the refrigeration cycle system (5) comprises a compressor (501), an output pipeline and a backflow pipeline, wherein the input end of the output pipeline is connected with the compressor (501), the input end of the output pipeline penetrates through the heat exchange device and is connected with a throttle valve (408), the output end of the backflow pipeline is connected with the compressor (501), and the input end of the backflow pipeline penetrates through the heat exchange device and is connected with the throttle valve (408).
8. The propane dehydrogenation product separation system according to claim 7, wherein the pre-cooling coarse separation system (3) comprises a pre-cooler (301), a heavy hydrocarbon separator (302), a coarse separation column (303), a coarse separation column reboiler (304) and a propane throttle valve (305), wherein the pre-cooler (301) is used for pre-cooling the second reaction gas, the pre-cooling process uses fresh propane to provide cold energy in a temperature range of-17 ℃ to 20 ℃ after being decompressed by the propane throttle valve (305), the heavy hydrocarbon separator (302) is used for separating the pre-cooled second reaction gas, and a liquid phase separated by the heavy hydrocarbon separator (302) is purified by the coarse separation column (303) to obtain a high-purity C3+ product; the gas phase separated from the heavy hydrocarbon separator (302) and the crude separation column (303) is the third reaction gas.
9. The propane dehydrogenation product separation system according to claim 8, wherein the cryogenic separation system (4) comprises a first-stage separator (403), a second-stage separator (404), a light component removal tower (406), a light component removal tower reboiler (405) and a light component removal tower top separator (407), the first-stage separator (403) is used for separating a second reaction gas cooled by the first-stage heat exchanger (401), a liquid phase separated by the first-stage separator (403) enters the light component removal tower (406), a gas phase separated by the first-stage separator (403) enters the second-stage separator (404) after being cooled by the second-stage heat exchanger (402), a hydrogen-rich product is obtained after the gas phase separated by the second-stage separator (404) is subjected to heat exchange device reheating, a separated product of the light component removal tower top separator (407) is subjected to heat exchange device reheating to obtain a C2/C1 product, and a separated product of the light component removal tower (405) is subjected to heat exchange device reheating to obtain a C3 product.
10. Propane dehydrogenation product separation system according to claim 9, characterized in that the refrigeration cycle system (5) is connected with a refrigerant replenishment system (6), the refrigerant of the refrigerant replenishment system (6) being composed of isopentane, propane, ethylene and methane, at least 3 of which are mixed in proportion.
CN202211291585.8A 2022-10-19 2022-10-19 Propane dehydrogenation product separation method and system Active CN115597309B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202211291585.8A CN115597309B (en) 2022-10-19 2022-10-19 Propane dehydrogenation product separation method and system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202211291585.8A CN115597309B (en) 2022-10-19 2022-10-19 Propane dehydrogenation product separation method and system

Publications (2)

Publication Number Publication Date
CN115597309A CN115597309A (en) 2023-01-13
CN115597309B true CN115597309B (en) 2023-05-16

Family

ID=84847981

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202211291585.8A Active CN115597309B (en) 2022-10-19 2022-10-19 Propane dehydrogenation product separation method and system

Country Status (1)

Country Link
CN (1) CN115597309B (en)

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102795956B (en) * 2012-08-30 2015-01-07 惠生工程（中国）有限公司 Method for separating reaction products produced during preparation of propylene by dehydrogenating propane
CN104296499B (en) * 2014-10-21 2016-03-23 杭州中泰深冷技术股份有限公司 A kind of two turbine booster expansion machine dehydrogenating propane ice chest piece-rate system and technique thereof
CN105884567A (en) * 2014-12-19 2016-08-24 朱琳 Method for extracting isobutane, isobutene and hydrogen rich gas from chemical tail gas
CN106316760A (en) * 2015-06-24 2017-01-11 中石化广州工程有限公司 Separation method for reaction product of propane dehydrogenated propylene preparation
CN208843967U (en) * 2018-06-05 2019-05-10 北京恒泰洁能科技有限公司 A kind of separation system of dehydrogenating propane product gas
CN108645119B (en) * 2018-06-14 2023-09-29 北京恒泰洁能科技有限公司 Cryogenic separation device and method for propane dehydrogenation product gas
CN212833550U (en) * 2020-05-26 2021-03-30 中国石油天然气集团有限公司 Propane dehydrogenation product separation device
CN114573415B (en) * 2020-11-30 2024-03-19 惠生工程（中国）有限公司 Separation method and device for coupled alkane catalytic dehydrogenation reaction products

Also Published As

Publication number Publication date
CN115597309A (en) 2023-01-13

Similar Documents

Publication Publication Date Title
CN109140903B (en) Air separation system and air separation method utilizing cold energy of liquefied natural gas
CN108458549B (en) System and method for extracting helium from natural gas and liquefying same
CN112028731B (en) Method for separating propylene reaction product from propane dehydrogenation
CN101625190A (en) Mixed refrigerant re-circulated liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA)
WO2019137359A1 (en) Lng cold energy utilization system and method based on argon cycle
CN101625189A (en) Cascade type liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA)
CN102071039B (en) Method for increasing light dydrocarbon recovery rate of oil-field associated gas through shallow condensing recovery
CN101285639B (en) Pre-cooled type coal bed gas nitrogen dilated and liquefied process taking advantage of variable pressure for adsorbing residual pressure
CN204508803U (en) The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide
CN115597309B (en) Propane dehydrogenation product separation method and system
CN102634395A (en) Process and system for purifying and refining coal-bed gas
US20230212768A1 (en) Device and method for producing hydrogen and byproduct oxygen by using green electricity electrolyzed water
CN114165987B (en) Liquid carbon dioxide production device and production method thereof
CN111634883B (en) Pretreatment method and system for synthesis ammonia feed gas
CN110387274B (en) Equipment and method for preparing LNG and coproducing LPG by pyrolyzing coal gas
CN209910277U (en) Unpowered cryogenic separation device
CN212669206U (en) Pretreatment system for synthesis ammonia raw material gas
CN114163291A (en) Propane dehydrogenation reaction product separation system and method
CN113663477A (en) Energy-saving device and process for strengthening low-temperature methanol washing absorption
CN112980490A (en) Associated gas light hydrocarbon recovery system for dry gas low-pressure expansion oil field and use method
CN221464140U (en) Fischer-Tropsch tail gas hydrogen separation liquefaction system
CN116592574B (en) Liquid hydrogen transport ship reliquefaction system for recovering expansion work
CN114777414B (en) Device and method for co-producing hydrogen, liquid hydrogen and liquefied natural gas by using industrial tail gas
CN116059675B (en) Method and device for desorbing carbon II from absorbent rich liquid by differential pressure type rectification
CN213778369U (en) Cryogenic separation system for separating methane from crude gas

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant