CN115597309A - Low-energy-consumption separation method and system for propane dehydrogenation product - Google Patents
Low-energy-consumption separation method and system for propane dehydrogenation product Download PDFInfo
- Publication number
- CN115597309A CN115597309A CN202211291585.8A CN202211291585A CN115597309A CN 115597309 A CN115597309 A CN 115597309A CN 202211291585 A CN202211291585 A CN 202211291585A CN 115597309 A CN115597309 A CN 115597309A
- Authority
- CN
- China
- Prior art keywords
- reaction gas
- product
- separation
- energy
- cooling
- 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.)
- Granted
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 low-energy-consumption separation method and a low-energy-consumption separation system for a propane dehydrogenation product, wherein the separation method comprises the following steps of: 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 rough 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 treatment, 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 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 quantity required to be provided by an external refrigeration circulating system, reduces 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
Technical Field
The invention belongs to the technical field of petrochemical separation, and particularly relates to a low-energy-consumption separation method and system for a propane dehydrogenation product.
Background
China has abundant propane reserves, and in recent years, the shale gas development leads the propane yield to be further increased. At present, the propane is mostly utilized by China in a combustion energy supply mode, even consumed in a 'ceiling lamp' mode, and the utilization value of the propane is greatly reduced. The conversion of propane into products 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. In downstream products of propane, propylene is a very important chemical raw material and can be used for producing high-value-added products such as polypropylene, acrylonitrile, propylene oxide, ethylene propylene rubber, nylon 66 and ABS resin. Among them, polypropylene is widely used in daily life, so that propylene is the second largest chemical raw material second to ethylene. From 2018 to 2020, the yield of propylene in China continuously rises, but the demand of downstream industries on propylene still cannot be met, and in 2022, the yield of propylene in China can reach 3300 ten thousand tons per year, while the equivalent demand of propylene can reach 3700 ten thousand tons per year, which shows that the downstream demand of propylene in China has a large gap in the future. The increasing demand for propylene and the large amount of propane by-product of the shale gas revolution have created opportunities for the development of propane dehydrogenation technology.
At present, all domestic propane dehydrogenation devices adopt UOP and Rumes reaction processes, all separation units adopt cryogenic separation for hydrogen and other components in reaction gas, the pressure of the recovered other components is increased to 3-3.5MPaG through a cryogenic pump, then C2 and C3 in the reaction gas are separated through an ethane tower, steam is needed to heat the tower bottom in the separation process, and propylene is needed to refrigerate the tower bottom, so that the energy consumption is very high. The cryogenic separation mostly adopts hydrogen expansion or cascade refrigeration, the operation is complex, the propylene yield is very low under the condition of small load, and the operation cost is increased due to the problems.
The traditional expansion refrigeration process needs to carry out isentropic expansion cooling refrigeration on non-condensable gas (hydrogen) in raw material gas through an expansion machine to enable easy-to-liquefy C2+ composition in the raw material gas to liquefy and separate the hydrogen, the liquefied C2 is boosted to 3-3.5MPaG through a mixed hydrocarbon pump and then sent to a deethanizer through a heat exchanger in a rewarming way, the deethanizer adopts a high-pressure rectification mode to separate ethane, a large amount of steam is consumed, low-temperature precooling equipment is additionally needed to increase the recovery rate of propylene at the top of the deethanizer, the hydrogen after cryogenic separation and expansion cannot meet the application due to pressure reduction, the hydrogen is mostly used in a fuel gas mode to cause resource waste, and secondary compression is needed if the hydrogen is needed to be applied. The reasons are combined to know that the traditional expansion refrigeration process consumes a large amount of energy.
The traditional cascade refrigeration process needs a plurality of refrigeration compressors to participate in circulating refrigeration (such as a propane compressor, an ethylene compressor, a methane compressor and the like), the recovery rate of refrigeration is slightly higher relative to that of an expansion refrigeration product, but the multiple compressors are needed to be matched, the one-time investment is higher, and the recovered C2+ is probably sent to a deethanizer by a high-pressure mixed hydrocarbon pump, so that the recovery rate of the product is only improved by the cascade refrigeration, and the energy consumption problem is not fundamentally solved.
There is a need in the art for improvements in the art to provide a low energy separation process and system for propane dehydrogenation products that overcomes the above disadvantages of the prior art.
Disclosure of Invention
The invention aims to provide a low-energy-consumption separation method and a low-energy-consumption separation system for propane dehydrogenation products, which are used for solving the problems in the prior art.
In order to achieve the above object, in one aspect, the present invention adopts the following technical solutions: a low-energy-consumption separation method for propane dehydrogenation products comprises the following steps:
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 rough 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 treatment, 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 heat energy of 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 solution, in step a, pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas includes: introducing the propane dehydrogenation product into a compression cooling system, firstly carrying out pressurization treatment, and then entering a circulating water cooler for cooling treatment to obtain a first reaction gas.
As an optional design structure of the above technical solution, in the step B, the drying and purifying the first reaction gas to obtain the second reaction gas includes: and introducing the first reaction gas into a drying and purifying system, and removing moisture 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 rough separation system for pre-cooling and separation treatment, and obtaining a C3+ product and a third reaction gas respectively includes: introducing the second reaction gas into a precooler of a precooling rough 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 in a-17-20 ℃ temperature zone after the pressure of the fresh propane is reduced by a propane throttle valve to precool the second reaction gas; introducing the precooled second reaction gas into a heavy hydrocarbon separator, purifying a liquid phase separated by the heavy hydrocarbon separator through a coarse separation tower, and obtaining a high-purity C3+ product; the gas phase separated by the heavy hydrocarbon separator and the coarse separation tower is the third reaction gas.
As an optional design structure of the above technical solution, in step D, introducing the third reaction gas into a cryogenic separation system to perform cryogenic treatment, separation, and rewarming treatment, and obtaining a hydrogen-rich product, a C2/C1 product, and a C3 product, respectively, includes: and cooling the third reaction gas by a heat exchange device, introducing the third reaction gas into a first-stage separator of a cryogenic separation system, introducing a liquid phase separated by the first-stage separator into a light component removal tower, cooling a gas phase separated by the first-stage separator by the heat exchange device, introducing the gas phase separated by the second-stage separator into a second-stage separator, reheating the gas phase separated by the second-stage separator by the heat exchange device to obtain a hydrogen-rich product, introducing a liquid phase separated by the second-stage separator into the light component removal tower, reheating a separated product separated by a tower top separator of the light component removal tower by the heat exchange device to obtain a C2/C1 product, and reheating a separated product of a reboiler of the light component removal tower by the heat exchange device to obtain a C3 product.
As an optional design structure of the above technical solution, the heat exchange device includes a primary heat exchanger and a secondary heat exchanger, the primary heat exchanger is connected to a refrigeration cycle system, the secondary heat exchanger is connected to the refrigeration cycle system, the refrigeration cycle system is connected to a refrigerant supplement system, and a refrigerant of the refrigerant supplement system is formed by mixing at least 3 of isopentane, propane, ethylene, and methane in a ratio; wherein the heat of the reboiler of the light component removal tower 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 low energy 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 respectively obtain a C3+ product and a third reaction gas;
the cryogenic separation system is used for carrying out cryogenic treatment, 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, and the heat exchange device 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 solution, the heat exchanger further comprises a refrigeration cycle system, and the heat exchanger 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 above technical solution, the refrigeration cycle system includes a compressor, an output pipeline and a return pipeline, an input end of the output pipeline is connected to the compressor, an input end of the output pipeline passes through the heat exchanging device and is connected to a throttle valve, an output end of the return pipeline is connected to the compressor, and an input end of the return pipeline passes through the heat exchanging device and is connected to the throttle valve.
As an optional design structure of the above 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 the second reaction gas, the pre-cooling treatment adopts fresh propane to provide cold energy for pre-cooling the second reaction gas in a-17-20 ℃ temperature region after being subjected to pressure reduction through the propane throttle valve, 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 coarse separation tower is the third reaction gas.
As an optional design structure of the technical scheme, the cryogenic separation system comprises a primary separator, a secondary separator, a light component removal tower reboiler and a light component removal tower top separator, wherein the primary separator is used for separating second reaction gas cooled by a primary heat exchanger, a liquid phase separated by the primary separator enters the light component removal tower, a gas phase separated by the primary separator enters the secondary separator after being cooled by the secondary heat exchanger, a gas phase separated by the secondary separator is reheated by a heat exchange device to obtain a hydrogen-rich product, a liquid phase separated by the secondary separator enters the light component removal tower, a separated product of the light component removal tower top separator is reheated by the heat exchange device to obtain a C2/C1 product, and a separated product of the light component removal tower reboiler is reheated by the heat exchange device to obtain a C3 product.
As an optional design structure of the above technical solution, the refrigeration cycle system is connected with a refrigerant supplement system, and a refrigerant of the refrigerant supplement 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 low-energy-consumption separation method and a low-energy-consumption separation system for propane dehydrogenation products, wherein a heat exchange device can absorb the heat energy of a third reaction gas in the cryogenic treatment process and release the heat energy in the rewarming treatment process, the cold quantity 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, the whole process does not need steam heating, and the low-energy-consumption separation method and the low-energy-consumption separation system have 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 work flow diagram of a process for low energy separation of propane dehydrogenation product in one embodiment of the present invention;
FIG. 2 is a flow diagram of the operation of a pre-chilling coarse separation system and a cryogenic separation system in one embodiment of the present invention.
In the figure: 1-a compression cooling system; 2-a drying and purifying system; 3-precooling a coarse separation system; 4-a cryogenic separation system; 5-a refrigeration cycle system; 6-a refrigerant make-up system; 301-a precooler; 302-a heavy hydrocarbon separator; 303-a crude separation column; 304-crude separation column reboiler; 305-propane throttling valve; 401-primary heat exchanger; 402-a secondary heat exchanger; 403-first stage separator; 404-a secondary separator; 405-a lightness-removing column reboiler; 406-a light ends removal column; 407-a light component removal tower top separator; 408-a throttle valve; 501-compressor.
Detailed Description
Examples
As shown in fig. 1 and fig. 2, the present embodiment provides a low energy consumption separation system for propane dehydrogenation products, which mainly includes a compression cooling system 1, a drying and purification system 2, a pre-cooling coarse separation system 3, a cryogenic separation system 4, a refrigeration cycle system 5, and a refrigerant supplement 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 rough separation system, the pre-cooling rough separation system is connected with the cryogenic separation system 4, the refrigerating system is connected with the pre-cooling rough separation system and the cryogenic separation system 4, the fresh propane is connected with the cryogenic separation system 4 and the pre-cooling rough separation system, and the refrigerant supplementing system 6 is used for providing a 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 a first reaction gas. The raw material gas from the battery limits 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 accessory equipment, a 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 selects a fixed bed drying agent to remove moisture in the first reaction gas, the drying and purifying system 2 is a heating and regenerating mode, the regenerating mode can select an isobaric regenerating mode and an open regenerating mode, and the drying and purifying system 2 can remove 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 respectively obtain a C3+ product and a third reaction gas. The precooling and coarse separating system 3 comprises a precooler 301, a heavy hydrocarbon separator 302, a coarse separating tower 303, a coarse separating tower reboiler 304 and a propane throttle valve 305, wherein the precooler 301 is used for precooling the second reaction gas, fresh propane is adopted for precooling treatment through the propane throttle valve 305 to provide cold energy precooling second reaction gas in a temperature range of-17 ℃ to 20 ℃, the heavy hydrocarbon separator 302 is used for separating the precooled second reaction gas, and a liquid phase separated by the heavy hydrocarbon separator 302 is purified through the coarse separating tower 303 to obtain a high-purity C3+ product; the gas phase separated by the heavy hydrocarbon separator 302 and the crude separation tower 303 is the third reaction gas.
The cryogenic separation system 4 is used for carrying out cryogenic separation, 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 both 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 penetrates through the heat exchange device and is connected with a throttle valve 408, the output end of the return pipeline is connected with the compressor 501, and the input end of the return pipeline penetrates through the heat exchange device and is connected with the throttle valve 408. The refrigeration cycle system 5 is connected with a refrigerant supplement system 6, and the refrigerant of the refrigerant supplement 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. The compressor 501 discharge pressure may be operated between 1.8MPaG and 3.5 MPaG. The refrigeration cycle system 5 is connected with the precooling coarse separation system 3 and the cryogenic separation system 4, and forms a cycle.
The cryogenic separation system 4 comprises a primary separator 403, a secondary separator 404, a light component removal tower 406, a light component removal tower reboiler 405 and a light component removal tower top separator 407, wherein the primary separator 403 is used for separating the second reaction gas cooled by the primary heat exchanger 401, the liquid phase separated by the primary separator 403 enters the light component removal tower 406, the gas phase separated by the primary separator 403 is cooled by the secondary heat exchanger 402 and then enters the secondary separator 404, the gas phase separated by the secondary separator 404 is reheated by a heat exchange device to obtain a hydrogen-rich product, the liquid phase separated by the secondary separator 404 enters the light component removal tower 406, the separated product of the light component removal tower top separator 407 is reheated by the heat exchange device to obtain a C2/C1 product, and the separated product of the light component removal tower reboiler 405 is reheated 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, the cold quantity required to be provided by the external refrigeration circulating system 5 is reduced, a plurality of compressors 501 are not required to be arranged, the deethanizer is directly integrated into the cryogenic separation system 4, the loss in the heat transfer process is reduced, ethane can be independently used as a product, the whole process does not need steam heating, and the heat exchange device 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 low-energy-consumption separation method of a propane dehydrogenation product, which is applied to the separation system, and the separation method comprises the following steps:
step A, pressurizing and cooling the propane dehydrogenation product to obtain a first reaction gas, which specifically comprises the following steps: introducing the propane dehydrogenation product into a compression cooling system 1, carrying out pressurization treatment, and then entering a circulating water cooler for cooling treatment to obtain a first reaction gas.
And step B, drying and purifying the first reaction gas to obtain a second reaction gas, which specifically comprises the following steps: and introducing the first reaction gas into a drying and purifying system 2, and removing moisture and trace mercury in the first reaction gas to obtain a second reaction gas.
Step C, introducing the second reaction gas into a pre-cooling rough 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 rough 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 for precooling the second reaction gas in a temperature zone of-17-20 ℃ after the pressure of the fresh propane is reduced through a propane throttle valve 305; introducing the pre-cooled second reaction gas into a heavy hydrocarbon separator 302, purifying a liquid phase separated by the heavy hydrocarbon separator 302 through a coarse separation tower 303, and obtaining a high-purity C3+ product; the gas phase separated by the heavy hydrocarbon separator 302 and the crude separation tower 303 is the third reaction gas.
Step D, introducing the third reaction gas into a cryogenic separation system 4 for cryogenic treatment, 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 heat energy of the third reaction gas in the cryogenic treatment process and releasing the heat energy in the rewarming treatment process.
Specifically, 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 supplement system 6, and a refrigerant of the refrigerant supplement 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 a cryogenic separation system 4 for cryogenic treatment, separation and rewarming treatment to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product, and the method comprises the following steps: and (3) cooling the third reaction gas by a heat exchange device, introducing the cooled third reaction gas into a primary separator 403 of a cryogenic separation system 4, introducing a liquid phase separated by the primary separator 403 into a light component removal tower 406, cooling a gas phase separated by the primary separator 403 by a primary heat exchanger 401, then introducing the cooled gas phase into a secondary separator 404, reheating the gas phase separated by the secondary separator 404 by the heat exchange device to obtain a hydrogen-rich product, introducing a liquid phase separated by the secondary separator 404 into the light component removal tower 406, reheating the separated product of the light component removal tower top separator 407 by a secondary heat exchanger 402 to obtain a C2/C1 product, and reheating the separated product of a reboiler 405 of the light component removal tower by the heat exchange device to obtain a C3 product. Wherein the heat of the lightness-removing column reboiler 405 is provided by fresh propane.
The invention provides a low-energy-consumption separation method and a low-energy-consumption separation system for propane dehydrogenation products, wherein propane dehydrogenation feed gas is pressurized by a compression cooling system 1, pressurized gas enters a circulating water cooler for cooling, cooled gas enters a drying and purifying system 2 for removing water, trace mercury and the like in the gas, the gas after drying and purifying enters a precooling coarse separation system 3, and the precooling coarse separation system mainly recovers cold energy released during pressure reduction of fresh propane, so that precools the gas after drying and purifying and most of C3+ products in the gas are liquefied, the gas after precooling 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 a reboiler 304 of the crude separation tower is provided by a 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 a cryogenic separation system 4, the gas phase from the top of the crude separation tower 303 and the heavy hydrocarbon separator 302 firstly passes through a first-stage heat exchanger 401 to be continuously cooled, the cooled gas enters a first-stage separator 403 of the cryogenic separation system 4, the liquid phase component separated by the first-stage separator 403 enters a lightness-removing tower 406, the gas phase separated by the first-stage separator 403 enters a second-stage heat exchanger 402 to be continuously cooled, the cooled gas enters a second-stage separator 404, the gas phase separated by the second-stage separator 404 is reheated by 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 a boundary area to be continuously used, the liquid phase separated by the second-stage separator 404 returns to enter the lightness-removing tower 406, the separator 407 at the top of the lightness-removing tower mainly produces light components of which mainly comprise ethane as a small amount of C1 products and hydrogen, and the like, and the light components are sent out of the boundary area to be continuously used after being reheated by the first-stage heat exchanger 401. The separated products of the reboiler 405 of the light component removal tower are mainly C3 products, the C3 products are sent out of a battery limit zone for further separation after being reheated by the first-stage heat exchanger 401, and the heat of the reboiler 405 of the light component removal tower is provided by fresh feed propane. The refrigeration capacity of the whole cryogenic separation system 4 is provided by a 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 a rough separation tower 303 and provides heat required by separation for the rough separation tower 303, gas and liquid phases separated by the rough separation tower 303 respectively enter a first-stage heat exchanger 401 and a second-stage heat exchanger 402, are decompressed by a throttle valve 408, then are subjected to temperature recovery mixing by the second-stage heat exchanger 402 and the first-stage heat exchanger 401 and then return to the compressor 501 again, and the whole refrigeration cycle is completed repeatedly.
In the description of the present invention, specific features, structures, etc. described in the embodiments are included in at least one embodiment, and those skilled in the art may combine features of different embodiments without contradiction. The protection scope of the present invention is not limited to the above-mentioned embodiments, and those embodiments that can be imagined by those skilled in the art without creative efforts based on the basic technical concept of the present invention belong to the protection scope of the present invention.
Claims (10)
1. A low-energy-consumption separation method for propane dehydrogenation products is characterized by comprising the following steps:
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 rough 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 treatment, separation and rewarming treatment to respectively obtain a hydrogen-rich product, a C2/C1 product and a C3 product; wherein, cryogenic separation system (4) is equipped with heat transfer device, heat transfer device is arranged in absorbing the heat energy of third reaction gas among the cryogenic treatment process and releases this heat energy in the rewarming processing process.
2. The low-energy-consumption separation method for the propane dehydrogenation product according to claim 1, wherein in the step A, the pressurizing and cooling treatment is carried out on the propane dehydrogenation product to obtain the first reaction gas, and the step A comprises the following steps: introducing the propane dehydrogenation product into a compression cooling system (1), carrying out pressurization treatment, and then entering a circulating water cooler for cooling treatment to obtain a first reaction gas;
in step B, drying and purifying the first reaction gas to obtain a second reaction gas, comprising: and introducing the first reaction gas into a drying and purifying system (2), and removing moisture and trace mercury in the first reaction gas to obtain a second reaction gas.
3. The low-energy-consumption separation method for propane dehydrogenation products according to claim 1, wherein in the step C, introducing the second reaction gas into a pre-cooling rough separation system for pre-cooling and separation treatment, and obtaining a C3+ product and a third reaction gas respectively comprises: introducing the second reaction gas into a precooler (301) of a precooling rough 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 for precooling the second reaction gas in a temperature zone of-17-20 ℃ after the pressure of the fresh propane is reduced by a propane throttle valve (305); introducing the pre-cooled second reaction gas into a heavy hydrocarbon separator (302), purifying a 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 by the heavy hydrocarbon separator (302) and the crude separation tower (303) is third reaction gas.
4. The low-energy-consumption separation method for the propane dehydrogenation product according to claim 3, wherein in the step D, the third reaction gas is introduced into a cryogenic separation system (4) to be subjected to cryogenic treatment, separation and rewarming treatment, and the hydrogen-rich product, the C2/C1 product and the C3 product are obtained respectively by the following steps: and (2) cooling the third reaction gas by a heat exchange device, introducing the cooled third reaction gas into a first-stage separator (403) of a cryogenic separation system (4), allowing a liquid phase separated by the first-stage separator (403) to enter a lightness-removing tower (406), cooling a gas phase separated by the first-stage separator (403) by the heat exchange device, allowing the cooled gas phase to enter a second-stage separator (404), allowing the gas phase separated by the second-stage separator (404) to be reheated by the heat exchange device to obtain a hydrogen-rich product, allowing a liquid phase separated by the second-stage separator (404) to enter the lightness-removing tower (406), allowing a separated product of a top separator (407) of the lightness-removing tower to be reheated by the heat exchange device to obtain a C2/C1 product, and allowing a separated product of a reboiler (405) of the lightness-removing tower to be reheated by the heat exchange device to obtain a C3 product.
5. The low-energy-consumption separation method for the propane dehydrogenation product, 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 supplement system (6), and the refrigerant of the refrigerant supplement system (6) is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion; wherein the heat of the reboiler (405) of the light component removal column is provided by fresh propane; the heat of the reboiler (304) of the crude separation column is provided by a refrigeration cycle system (5).
6. A propane dehydrogenation product low energy consumption separation system is characterized by 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 respectively obtain a C3+ product and a third reaction gas;
the cryogenic separation system (4) is used for carrying out cryogenic treatment, 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, and the heat exchange device 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 low energy consumption separation system according to claim 6, further comprising a refrigeration cycle system (5), wherein 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 both 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 penetrates through the heat exchange device to be connected with a throttle valve (408), the output end of the return pipeline is connected with the compressor (501), and the input end of the return pipeline penetrates through the heat exchange device to be connected with the throttle valve (408).
8. The low-energy-consumption separation system for the propane dehydrogenation product, according to claim 7, wherein the precooling and coarse separation system (3) comprises a precooler (301), a heavy hydrocarbon separator (302), a coarse separation tower (303), a coarse separation tower reboiler (304) and a propane throttle valve (305), the precooler (301) is used for precooling the second reaction gas, the precooling treatment adopts fresh propane to precool the second reaction gas by cooling energy in a temperature range of-17 ℃ to 20 ℃ after the pressure of the propane throttle valve (305) is reduced, the heavy hydrocarbon separator (302) is used for separating the precooled second reaction gas, 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 by the heavy hydrocarbon separator (302) and the crude separation tower (303) is third reaction gas.
9. The propane dehydrogenation product low-energy-consumption 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 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 component removal tower (406), the 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), the gas phase separated by the second-stage separator (404) is reheated by the heat exchange device to obtain a hydrogen-rich product, the liquid phase separated by the second-stage separator (404) enters the light component removal tower (406), the separated product separated by the light component removal tower top separator (407) is reheated by the heat exchange device to obtain a C2/C1 product, and the separated product by the light component removal tower reboiler (405) is reheated by the heat exchange device to obtain a C3 product.
10. The propane dehydrogenation product low energy consumption separation system according to claim 9, wherein the refrigeration cycle system (5) is connected with a refrigerant supplement system (6), and the refrigerant of the refrigerant supplement system (6) is formed by mixing at least 3 of isopentane, propane, ethylene and methane according to a proportion.
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 true CN115597309A (en) | 2023-01-13 |
| CN115597309B 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) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102795956A (en) * | 2012-08-30 | 2012-11-28 | 惠生工程（中国）有限公司 | Method for separating reaction products produced during preparation of propylene by dehydrogenating propane |
| CN104296499A (en) * | 2014-10-21 | 2015-01-21 | 杭州中泰深冷技术股份有限公司 | Double-turbine boosting expansion machine propane dehydrogenation cold box separation system and technique |
| 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 |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| 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 |
| 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 |
| CN114573415A (en) * | 2020-11-30 | 2022-06-03 | 惠生工程（中国）有限公司 | Method and device for separating coupling type alkane catalytic dehydrogenation reaction product |
-
2022
- 2022-10-19 CN CN202211291585.8A patent/CN115597309B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102795956A (en) * | 2012-08-30 | 2012-11-28 | 惠生工程（中国）有限公司 | Method for separating reaction products produced during preparation of propylene by dehydrogenating propane |
| CN104296499A (en) * | 2014-10-21 | 2015-01-21 | 杭州中泰深冷技术股份有限公司 | Double-turbine boosting expansion machine propane dehydrogenation cold box separation system and technique |
| 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 |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| 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 |
| CN114573415A (en) * | 2020-11-30 | 2022-06-03 | 惠生工程（中国）有限公司 | Method and device for separating coupling type alkane catalytic dehydrogenation reaction product |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115597309B (en) | 2023-05-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20230067883A1 (en) | Mixed refrigerant hydrogen liquefaction device and method of using same | |
| CN108458549B (en) | System and method for extracting helium from natural gas and liquefying same | |
| CN109140903B (en) | Air separation system and air separation method utilizing cold energy of liquefied natural gas | |
| CN101625190A (en) | Mixed refrigerant re-circulated liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA) | |
| CN112028731B (en) | Method for separating propylene reaction product from propane dehydrogenation | |
| CN102200370A (en) | Expansion combustible gas liquefaction device and flow | |
| CN101625189A (en) | Cascade type liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA) | |
| CN102435045A (en) | Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof | |
| CN101285639B (en) | Pre-cooled type coal bed gas nitrogen dilated and liquefied process taking advantage of variable pressure for adsorbing residual pressure | |
| WO2019137359A1 (en) | Lng cold energy utilization system and method based on argon cycle | |
| CN204508803U (en) | The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide | |
| CN202382518U (en) | Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas) | |
| CN102634395A (en) | Process and system for purifying and refining coal-bed gas | |
| CN105910387B (en) | The process unit and method of cold are reclaimed in a kind of LNG from coke-stove gas | |
| CN104495751A (en) | Method and device for preparing hydrogen and carbon monoxide by efficient synthesis gas separation | |
| CN115597309B (en) | Propane dehydrogenation product separation method and system | |
| CN109357475B (en) | System for cascade utilization LNG cold energy prepares liquid oxygen liquid nitrogen | |
| CN106500458B (en) | Pre-cooling type natural gas liquefaction process and system | |
| CN114165987B (en) | Liquid carbon dioxide production device and production method thereof | |
| CN114440551B (en) | Device and method for recycling mixed hydrocarbon of associated gas of oil field rich in nitrogen and liquefying dry gas at low temperature | |
| CN215517292U (en) | Integrated process system for producing LNG (liquefied Natural gas) and LPG (liquefied Petroleum gas) from oilfield associated gas | |
| CN214735563U (en) | System for producing light hydrocarbon and LNG (liquefied Natural gas) from oilfield associated gas | |
| CN111634883B (en) | Pretreatment method and system for synthesis ammonia feed gas | |
| CN209910277U (en) | Unpowered cryogenic separation device | |
| CN210506240U (en) | Equipment for preparing LNG (liquefied Natural gas) and co-producing LPG (liquefied Petroleum gas) by pyrolyzing coal 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 |