CN108645119A - Dehydrogenating propane product gas cryogenic separation device and method - Google Patents
Dehydrogenating propane product gas cryogenic separation device and method Download PDFInfo
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- CN108645119A CN108645119A CN201810611992.XA CN201810611992A CN108645119A CN 108645119 A CN108645119 A CN 108645119A CN 201810611992 A CN201810611992 A CN 201810611992A CN 108645119 A CN108645119 A CN 108645119A
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- alkadienes
- product gas
- acetylene removal
- heat exchanger
- ice chest
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses dehydrogenating propane product gas cryogenic separation device and methods, including product gas compression drying system, ice chest heat exchanger, acetylene removal hydrocarbon alkadienes system, deethanization system and propylene rectification tower, product gas compression drying system is connect with ice chest heat exchanger, it is sent to ice chest heat exchanger after dehydrogenating propane product gas compression drying and carries out fractional condensaion formation condensate liquid and low temperature cold lime set, condensate liquid is sent into deethanization system after entering acetylene removal hydrocarbon alkadienes system removing alkynes and alkadienes, deethanization system can receive low temperature cold lime set and convey gas phase light component to ice chest heat exchanger, the liquid phase component of deethanization system is output to propylene rectification tower rectifying and obtains propylene product.The dehydrogenating propane product gas deep cooling process for separating of the present invention is using azeotrope compression refrigeration, wider array of refrigeration temperature levels and more refrigerant temperature ranks can be provided, reduce dynamic number of devices, a large amount of equipment investment and Operation and Maintenance expense are reduced than conventional refrigeration separating technology.
Description
Technical field
The present invention relates to petrochemical industries, more particularly to dehydrogenating propane product gas cryogenic separation device and method.
Background technology
Propylene is a kind of important basic petrochemical raw material, is occupied an important position in national economy.A few years ago, international
The method of upper traditional production propylene product mainly has oil product cracking, oil product catalytic cracking etc..Nowadays, propane is catalyzed
Dehydrogenation, methanol-to-olefins and preparing propylene from methanol also become the new important channel of production propylene, and previous, propane is mainly derived from
Associated gas, Yield comparison is low, and conditional place can produce propylene product as the raw material of light hydrocarbon cracking stove, most of
The propane in area is used as liquefied gas product due to that cannot form scale, international along with propane dehydrogenation catalyst is extremely expensive
On with dehydrogenating propane produce propylene device be phoenix feathers and unicorn horns；However, with shale gas exploitation technology be constantly progressive and it is ripe,
The yield of shale gas is increasing, and the cost for exploiting shale gas is lower and lower, to which association propane amount is increasing, leads to third
Alkane price is lower and lower, and the cost that propylene is produced by propane catalytic dehydrogenation is lower and lower, and the dress of propylene is produced with dehydrogenating propane
It sets also more and more.Realize that industrialized production dehydrogenating propane technique there are three, is had using most in the world both at home and abroad at present
Two kinds of techniques, one be UOP moving bed propane catalytic dehydrogenation process, another family is the fixed bed propane catalytic dehydrogenation of Lu Musi
Technique, and it is domestic more using UOP moving bed catalytic dehydrogenations.The either catalytic dehydrogenation of UOP moving beds or the fixation of Lu Musi
Bed propane catalytic dehydrogenation is all to use cold separation technology for product gas separation refrigeration.UOP is swollen using propylene refrigeration+two-stage
The cryogenics of swollen machine.Since dehydrogenating propane product gas constitutes feature, the method effectively recycled in hydrogen tail gas is exactly deep cooling,
Product gas is cooled to certain temperature under certain pressure, makes three component liquefaction of carbon therein and is detached.It goes into operation the country
With dehydrogenating propane product gas separating pressure 1.1MPa or so again in UOP the and Lu Musi techniques built, Lu Musi technique propylene
The cascade refrigeration technology of refrigeration+ethylene refrigeration, lowest refrigerating temperature is at -100 DEG C or so；UOP techniques adopt then use propylene refrigeration+
The cryogenics of double expansion machine, -130 DEG C of lowest refrigerating temperature, and hydrogen expander machine cost is high and refrigeration effect is bad；Expansion
Thick hydrogen after decompression goes pressure swing adsorption hydrogen production unit will also second compression again.Traditional ethylene separation technique is all to use propylene refrigeration
The cascade refrigeration method of+ethylene refrigeration, this cascade refrigeration need a propylene refrigeration unit and an ethylene refrigeration unit total
With completion.Process equipment is more, poor refrigerating efficiency, separating effect are not ideal enough.
Invention content
In view of this, the purpose of the present invention is to provide a kind of process equipment simplification, good refrigeration effect, good separating effects
Dehydrogenating propane product gas cryogenic separation device and method.
According to an aspect of the invention, there is provided dehydrogenating propane product gas cryogenic separation device, including product gas compression
Drying system, ice chest heat exchanger, acetylene removal hydrocarbon alkadienes system, deethanization system and propylene rectification tower, the product gas compression are dry
Drying system is connect with ice chest heat exchanger, and ice chest heat exchanger is sent to after dehydrogenating propane product gas compression drying and carries out fractional condensaion shape
At condensate liquid and low temperature cold lime set, the ice chest heat exchanger is connect with the feed end of acetylene removal hydrocarbon alkadienes system, the acetylene removal hydrocarbon
The discharge end of alkadienes system is connect with the input terminal of deethanization system, and the condensate liquid enters the removing of acetylene removal hydrocarbon alkadienes system
Deethanization system is sent into after alkynes and alkadienes, the deethanization system is bi-directionally connected with ice chest heat exchanger to receive cryogenic condensation
Liquid simultaneously conveys gas phase light component to ice chest heat exchanger, and the output end of the deethanization system and the input terminal of propylene rectification tower connect
It connects.
In some embodiments, dehydrogenating propane product gas cryogenic separation device further includes azeotrope refrigeration system, institute
Azeotrope refrigeration system is stated to connect with ice chest heat exchanger and form refrigerating circuit.
In some embodiments, the deethanization system includes low pressure dethanizer and high pressure dethanizer.
In some embodiments, the acetylene removal hydrocarbon alkadienes system includes acetylene removal hydrocarbon alkadienes reaction feed system and takes off
Alkynes alkadienes reaction system, the ice chest heat exchanger is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction feed system, described
The discharge end of acetylene removal hydrocarbon alkadienes reaction feed system is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction system, and condensate liquid is sent into
Carry out pressurization heating to acetylene removal hydrocarbon alkadienes reaction feed system, after be re-fed into acetylene removal hydrocarbon alkadienes reaction system and carry out plus hydrogen
Reaction is by alkynes, di-olefins at propylene or propane, output end and the deethanization system of the acetylene removal hydrocarbon alkadienes reaction system
The input terminal of system connects.
In some embodiments, dehydrogenating propane product gas cryogenic separation device further includes pressure-swing absorption apparatus, the change
Pressure adsorbent equipment is connect with ice chest heat exchanger to receive the hydrogen rich off gas of ice chest heat exchanger output.
According to another aspect of the present invention, dehydrogenating propane product gas deep cooling separating method is provided, is included the following steps：
S1, dehydrogenating propane device product gas are sent into ice chest heat exchange after product gas compression drying system pressure-raising and water removal
Product gas is cooled to the condensate liquid and low temperature cold lime set of the respectively different component of different temperatures through heat exchanger heat exchange cooling by device；
S2, hydrogenation reaction is carried out after condensate liquid to be sent into the pressurization heating of acetylene removal hydrocarbon alkadienes system, removes alkynes in material
And the separation that deethanization system carries out C3 heavy constituents and methane, ethane light component is sent into after alkadienes；
Liquid phase heavy constituent in S3, deethanization system in condensate liquid is transported to propylene rectification tower and carries out rectifying, obtains propylene
Product and recycled propane.
In some embodiments, product gas is first condensed to -15 DEG C in the S1 and obtains the C3 that group is divided into 90% or more
With the condensate liquid of a small amount of C4+, then by product gas condense to -40 DEG C obtain group be divided into 0.60~0.70% H2,85% or more
The low temperature cold lime set of C3 and a small amount of methane carbon two.
In some embodiments, the acetylene removal hydrocarbon alkadienes system includes acetylene removal hydrocarbon alkadienes reaction feed system and takes off
Alkynes alkadienes reaction system, the acetylene removal hydrocarbon alkadienes reaction feed system will be sent to acetylene removal hydrocarbon after condensate liquid pressurization heating
Alkadienes reaction system carries out hydrogenation reaction, and the alkynes in product gas, alkadienes and hydrogen reaction is made to generate propylene or propane.
In some embodiments, the deethanization system includes low pressure dethanizer and high pressure dethanizer, described de-
The light components such as C3 and methane, ethane are divided into high pressure dethanizer after the cooling of alkynes alkadienes reaction system outlet material
From the C3 of high pressure dethanizer tower reactor is sent into propylene rectification tower, and the high pressure deethanizer overhead contains carbon three and methane, ethane
Tail gas is sent into low pressure dethanizer after decrease temperature and pressure.
In some embodiments, the low temperature cold lime set enters low pressure dethanizer, the low pressure dethanizer tower reactor
Material enters propylene rectification tower after heating, and the carbon two and light component of the low pressure deethanizer overhead return to ice chest heat exchanger and answers
Temperature is recycled.
The beneficial effects of the invention are as follows：Dehydrogenating propane product gas deep cooling process for separating proposed by the present invention uses azeotrope
Compression refrigeration, it is possible to provide wider array of refrigeration temperature levels and more refrigerant temperature ranks, adjustment cryogen proportioning can meet third
The refrigeration requirement of alkane dehydrogenation product gas component fluctuation and different separating technologies.Dehydrogenating propane product gas is in multiple temperature level cryogens
Under be condensed into different temperatures different component liquid so that the heat transfer temperature difference in heat exchanger between hot-fluid and cold flow is relatively low always,
Reduce the operation energy consumption of device；And a refrigeration compressor is only needed, reduce dynamic number of devices, is detached than conventional refrigeration
Technique reduces a large amount of equipment investment and Operation and Maintenance expense.
Description of the drawings
Fig. 1 is the process flow chart of the dehydrogenating propane product gas cryogenic separation device of an embodiment of the present invention；
Fig. 2 is the structural schematic diagram of the ice chest heat exchanger of dehydrogenating propane product gas cryogenic separation device shown in Fig. 1.
Specific implementation mode
Invention is described in further detail below in conjunction with the accompanying drawings.
Embodiment 1
Fig. 1 and Fig. 2 schematically shows a kind of dehydrogenating propane product gas deep cooling point of embodiment according to the present invention
From device.
Referring to Figures 1 and 2, dehydrogenating propane product gas cryogenic separation device includes that product gas compression drying system 1, ice chest change
Hot device 2, acetylene removal hydrocarbon alkadienes system 3, azeotrope refrigeration system 4, deethanization system 5, propylene rectification tower 6 and pressure-variable adsorption dress
Set 7.Product gas compression drying system 1 is connect with ice chest heat exchanger 2, and dehydrogenating propane product gas is through product gas compression drying system 1
It is sent to ice chest heat exchanger 2 after compression drying and carries out fractional condensaion formation condensate liquid and low temperature cold lime set.Ice chest heat exchanger 2 with it is de-
The feed end of alkynes alkadienes system 3 connects, and the discharge end of acetylene removal hydrocarbon alkadienes system 3 connects with the input terminal of deethanization system 5
It connects.Condensate liquid enters acetylene removal hydrocarbon alkadienes system 3 and removes deethanization system 5 of being sent into after alkynes and alkadienes, deethanization system 5 with
Ice chest heat exchanger 2 is bi-directionally connected, and deethanization system 5 receives the low temperature cold lime set and acetylene removal hydrocarbon alkadienes of 2 output of ice chest heat exchanger
The material of the output of system 3 simultaneously carries out gas-liquid separation.It is multiple that the gas phase light component that deethanization system 5 is isolated returns to ice chest heat exchanger 2
It can be used as the fuel of fuel gas system after temperature.The output end of deethanization system 5 is connect with the input terminal of propylene rectification tower 6, takes off second
The liquid phase component of 5 output of methane series system is sent to propylene rectification tower 6 and carries out rectifying.Pressure-swing absorption apparatus 7 is connect with ice chest heat exchanger 2
To receive the hydrogen rich off gas of the output of ice chest heat exchanger 2.
Ice chest heat exchanger 2 may include first-class heat exchanger 21, secondary heat exchanger 22, level-one gas-liquid separator 23 and two level gas
Liquid/gas separator 24.The output end of product gas compression drying system 1 is connect with the input terminal of level-one gas-liquid separator 23, product air pressure
The product gas that contracting drying system 1 exports is sent to the progress of level-one gas-liquid separator 23 after first-class heat exchanger 21 condenses to -15 DEG C
Gas-liquid separation.The liquid phase material that level-one gas-liquid separator 23 is isolated is the condensate liquid that group is divided into 90% or more C3 and a small amount of C4+,
The liquid phase output of level-one gas-liquid separator 23 connect with acetylene removal hydrocarbon alkadienes system 3 and condensate liquid can be transported to acetylene removal hydrocarbon two
Alkene system 3.The gas phase outlet of level-one gas-liquid separator 23 is connect with the input terminal of two level gas-liquid separator 24, level-one gas-liquid
The gaseous phase materials that separator 23 exports are sent into two level gas-liquid separator 24 after secondary heat exchanger 22 condenses to -40 DEG C and carry out gas-liquid
Separation.The liquid phase that two level gas-liquid separator 24 is isolated is that group is divided into 0.60~0.70% H2,85% or more C3 and a small amount of
Methane, gas phase are then hydrogen rich off gas.24 liquid phase output of two level gas-liquid separator is connect with deethanization system 5, two level gas-liquid point
It is connect with pressure-swing absorption apparatus 7 from 24 gas phase outlet of device.
Azeotrope refrigeration system 4 connect with ice chest heat exchanger 2 and forms refrigerating circuit.Azeotrope refrigeration system 4 is adopted
It is the refrigeration cryogen mixed by the components different proportion such as methane, ethylene, propane, isopentane, nitrogen with azeotrope, it can
To provide 5 DEG C of colds to subzero 190 DEG C of temperature ranges.Patent concrete component of the present invention be methane 10~15%, ethylene 40~
45%, propane 12~25%, isopentane 10~18% and nitrogen 5~8%.
Azeotrope refrigeration system 4 is made of a refrigeration compressor set, cryogen compensator and throttle valve.
Acetylene removal hydrocarbon alkadienes system 3 includes acetylene removal hydrocarbon alkadienes reaction feed system 31 and acetylene removal hydrocarbon alkadienes reaction system
32.Ice chest heat exchanger 2 is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction feed system 31, acetylene removal hydrocarbon alkadienes reaction feed system
The discharge end of system 31 is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction system 32.Condensate liquid is sent to acetylene removal hydrocarbon diene hydrocarbon reaction
Feed system 31 carries out pressurization heating, after be re-fed into acetylene removal hydrocarbon alkadienes reaction system 32 and carry out hydrogenation reaction by alkynes, two
Alkene is converted to propylene or propane, and the output end of acetylene removal hydrocarbon alkadienes reaction system 32 is connect with the input terminal of deethanization system 5.
Deethanization system 5 includes low pressure dethanizer 51 and high pressure dethanizer 52.Low pressure dethanizer 51 and acetylene removal hydrocarbon
The connection of alkadienes reaction system 32 is to receive the gaseous phase materials of the output of acetylene removal hydrocarbon alkadienes reaction system 32.High pressure dethanizer 52
It is connect with acetylene removal hydrocarbon alkadienes reaction system 32 to receive the liquid phase material of the output of acetylene removal hydrocarbon alkadienes reaction system 32.Low pressure is de-
The output end of ethane tower 51 and the output end of high pressure dethanizer 52 connect with the input terminal of propylene rectification tower 6 and to propylene essence
It evaporates tower 6 and conveys liquid phase material.The feed end of low pressure dethanizer 51 is connect with 24 liquid phase output of two level gas-liquid separator to connect
Receive low temperature cold lime set.High pressure dethanizer 52 is connect with low pressure dethanizer 51, and what 52 tower top of high pressure dethanizer generated contains
The tail gas of a large amount of C3 is transported to low pressure dethanizer 51.
Embodiment 2
Dehydrogenating propane product gas deep cooling separating method, includes the following steps：
S1, dehydrogenating propane device product gas are sent into ice chest after 1 pressure-raising of product gas compression drying system and water removal and are changed
Product gas is cooled to the condensate liquid and low temperature cold lime set of the respectively different component of different temperatures through heat exchanger heat exchange cooling by hot device 2；
Product gas is first condensed to -15 DEG C by the first-class heat exchanger 21 of ice chest heat exchanger 2, is then sent through level-one gas-liquid separator 23
It carrying out gas-liquid separation and obtains the condensate liquid that group is divided into 90% or more C3 and a small amount of C4+, gas phase condenses to through secondary heat exchanger 22-
Be sent to two level gas-liquid separator 24 after 40 DEG C and carry out gas-liquid separation, obtain group be divided into 0.60~0.70% H2,85% or more
The low temperature cold lime set of C3 and a small amount of methane and the hydrogen rich off gas containing a large amount of H2.
S2, hydrogenation reaction is carried out after condensate liquid to be sent into the 3 pressurization heating of acetylene removal hydrocarbon alkadienes system, removes alkynes in material
And the separation of high pressure dethanizer 52 progress the C3 heavy constituents and methane, ethane light component of deethanization system 5 is sent into after alkadienes.
Acetylene removal hydrocarbon alkadienes system 3 includes acetylene removal hydrocarbon alkadienes reaction feed system 31 and acetylene removal hydrocarbon alkadienes reaction system
32.Condensate liquid is forced into 3.5MPa and is warming up to after 45 DEG C or so by acetylene removal hydrocarbon alkadienes reaction feed system 31 is sent to acetylene removal hydrocarbon
Alkadienes reaction system 32 carries out hydrogenation reaction, and the alkynes in product gas, alkadienes and hydrogen reaction is made to generate propylene or propane.
The liquid phase component being condensed out in S3, deethanization system 5 is transported to propylene rectification tower 6 and carries out rectifying, makees in catalyst
Under, alkynes, alkadienes and hydrogen reaction generate propylene or propane.Obtain propylene product and recycled propane.Recycled propane from
The tower reactor of propylene rectification tower 6 produces, and the raw material after vaporization refrigeration as dehydrogenating propane enters heating system under low pressure.
Deethanization system 5 includes low pressure dethanizer 51 and high pressure dethanizer 52, acetylene removal hydrocarbon alkadienes reaction system 32
The light components such as C3 and methane, ethane are detached into high pressure dethanizer 52 after outlet material cooling, high pressure dethanizer
The C3 of 52 tower reactors is sent into propylene rectification tower 6, and the part carbon three and methane of high pressure deethanizer overhead, ethane tail gas are through decrease temperature and pressure
It is sent into low pressure dethanizer 51 afterwards.
Pressure in high pressure dethanizer 52 is 1.8~2.5MPa, in high pressure dethanizer 52, the liquid phase in condensate liquid
Since gravity flows to bottom of tower, light component methane ethane in condensate liquid etc. is gasificated into gas and is flowed out from dethanizer heavy constituent, from
And realize the separation of the light components such as C3 and methane, ethane.The mixing carbon 3 material of 52 tower reactor of high pressure dethanizer leans on pressure itself
Into propylene rectification tower 6, gaseous component is sent into charging of the low pressure dethanizer 51 as low pressure dethanizer 51.Two level gas-liquid point
It is also fed into the charging in low pressure dethanizer 51 as low pressure dethanizer 51 from the low temperature cold lime set that device 24 is isolated.Low pressure
The mixing carbon 3 material of 51 tower reactor of dethanizer is pumped up out, then enters propylene rectification tower 6 after heating.Low pressure dethanizer 51
The carbon two and light component of tower top can burn after returning to ice chest heat exchanger rewarming to room temperature into fuel gas system.
Mixing carbon three into propylene rectification tower 6 is separated into propylene product and recycled propane in propylene rectification tower 6, and third
Alkene product is produced from the overhead extraction of propylene rectification tower 6, recycled propane from the tower reactor of propylene rectification tower 6, under low pressure vaporization system
Raw material after cold as dehydrogenating propane enters heating system.
The low temperature hydrogen rich off gas obtained after S4, deep cooling is sent to 7 hydrogen making of pressure-swing absorption apparatus after re-heat.
The invention discloses a kind of dehydrogenating propane product gas deep cooling process for separating.For the boiling of dehydrogenating propane product gas component
Point is different, is detached by the way of cryogenic rectification in different warm areas, and substitutes former cascade refrigeration using azeotrope refrigeration.
New separating technology system includes unstripped gas compression and drying system, acetylene removal dialkene removal reactor, main heat exchanger, dethanizer
System, propylene rectification tower, refrigeration system and pressure-variable adsorption carry hydrogen system.Refrigeration system is freezed using azeotrope, using not
Same cryogen combines and carries out condensation step by step, evaporation obtains different temperatures grade cold, reaches feed gas composition gradually cooling and liquefaction
Detach purpose.The process is easy to operate, reduces dynamic number of devices, investment and maintenance cost reduce, with former process
Operation energy consumption compared to device reduces by 10%, has good energy-saving effect and economic benefit.
Above-described is only some embodiments of the present invention.For those of ordinary skill in the art, not
Under the premise of being detached from the invention design, various modifications and improvements can be made, these belong to the protection domain of invention.
Claims (10)
1. dehydrogenating propane product gas cryogenic separation device, it is characterised in that:It is changed including product gas compression drying system (1), ice chest
Hot device (2), acetylene removal hydrocarbon and alkadienes system (3), deethanization system (5) and propylene rectification tower (6), the product gas compression drying
System (1) is connect with ice chest heat exchanger (2), and ice chest heat exchanger (2) is sent to after dehydrogenating propane product gas compression drying and is divided
Grade condensation forms condensate liquid and low temperature cold lime set, and the ice chest heat exchanger (2) and the feed end of acetylene removal hydrocarbon alkadienes system (3) connect
It connects, the discharge end of the acetylene removal hydrocarbon alkadienes system (3) is connect with the input terminal of deethanization system (5), and the condensate liquid enters
Acetylene removal hydrocarbon alkadienes system (3) removes deethanization system (5) of being sent into after alkynes and alkadienes, the deethanization system (5) with it is cold
Case heat exchanger (2) is bi-directionally connected to receive low temperature cold lime set and convey gas phase light component, the deethanization to ice chest heat exchanger (2)
The output end of system (5) is connect with the input terminal of propylene rectification tower (6).
2. dehydrogenating propane product gas cryogenic separation device according to claim 1, it is characterised in that:It further include azeotrope
Refrigeration system (4), the azeotrope refrigeration system (4) connect with ice chest heat exchanger (2) and form refrigerating circuit.
3. dehydrogenating propane product gas cryogenic separation device according to claim 2, it is characterised in that:The deethanization system
(5) include low pressure dethanizer (51) and high pressure dethanizer (52).
4. dehydrogenating propane product gas cryogenic separation device according to claim 1, it is characterised in that:The acetylene removal hydrocarbon diene
Hydrocarbon system (3) includes acetylene removal hydrocarbon alkadienes reaction feed system (31) and acetylene removal hydrocarbon alkadienes reaction system (32), the ice chest
Heat exchanger (2) is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction feed system (31), the acetylene removal hydrocarbon alkadienes reaction feed
The discharge end of system (31) is connect with the feed end of acetylene removal hydrocarbon alkadienes reaction system (32), and condensate liquid is sent into acetylene removal hydrocarbon alkadienes
Reaction feed system (31) carries out pressurization heating, after be re-fed into acetylene removal hydrocarbon alkadienes reaction system (32) carry out hydrogenation reaction will
Alkynes, di-olefins are at propylene or propane, output end and the deethanization system of the acetylene removal hydrocarbon alkadienes reaction system (32)
(5) input terminal connection.
5. according to Claims 1 to 4 any one of them dehydrogenating propane product gas cryogenic separation device, it is characterised in that:Also wrap
Pressure-swing absorption apparatus (7) is included, the pressure-swing absorption apparatus (7) connect defeated to receive ice chest heat exchanger (2) with ice chest heat exchanger (2)
The hydrogen rich off gas gone out.
6. dehydrogenating propane product gas deep cooling separating method, which is characterized in that include the following steps：
S1, dehydrogenating propane device product gas are sent into ice chest heat exchange after product gas compression drying system (1) pressure-raising and water removal
Product gas is cooled to the condensate liquid and low temperature cold lime set of the respectively different component of different temperatures through heat exchanger heat exchange cooling by device (2)；
S2, condensate liquid be sent into acetylene removal hydrocarbon alkadienes system (3) pressurize and carry out hydrogenation reaction after heating, remove in material alkynes and
The separation that deethanization system (5) carries out C3 heavy constituents and methane, ethane light component is sent into after alkadienes；
Liquid phase heavy constituent in S3, deethanization system (5) in condensate liquid is transported to propylene rectification tower (6) and carries out rectifying, obtains third
Alkene product and recycled propane.
7. dehydrogenating propane product gas deep cooling separating method according to claim 6, which is characterized in that first will production in the S1
Product gas condenses to -15 DEG C and obtains the condensate liquid that group is divided into 90% or more C3 and a small amount of C4+, then product gas is condensed to -40 DEG C
Obtain the low temperature cold lime set that group is divided into 0.60~0.70% H2,85% or more C3 and a small amount of methane.
8. dehydrogenating propane product gas deep cooling separating method according to claim 6, which is characterized in that the acetylene removal hydrocarbon diene
Hydrocarbon system (3) includes acetylene removal hydrocarbon alkadienes reaction feed system (31) and acetylene removal hydrocarbon alkadienes reaction system (32), the acetylene removal
Hydrocarbon alkadienes reaction feed system (31) will be sent to acetylene removal hydrocarbon alkadienes reaction system (32) after condensate liquid pressurization heating and carry out
Hydrogenation reaction makes the alkynes in product gas, alkadienes and hydrogen reaction generate propylene or propane.
9. dehydrogenating propane product gas deep cooling separating method according to claim 8, which is characterized in that the deethanization system
(5) include low pressure dethanizer (51) and high pressure dethanizer (52), acetylene removal hydrocarbon alkadienes reaction system (32) outlet object
The light components such as C3 and methane, ethane are detached into high pressure dethanizer (52) after material cooling, high pressure dethanizer (52)
The C3 of tower reactor is sent into propylene rectification tower (6), and methane, the ethane tail gas of the high pressure deethanizer overhead are sent into after decrease temperature and pressure
Low pressure dethanizer (51).
10. dehydrogenating propane product gas deep cooling separating method according to claim 8, which is characterized in that the cryogenic condensation
Liquid enters low pressure dethanizer (51), and low pressure dethanizer (51) kettle material enters propylene rectification tower (6) after heating,
The carbon two and light component of low pressure dethanizer (51) tower top return to ice chest heat exchanger rewarming and are recycled.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5421167A (en) * | 1994-04-01 | 1995-06-06 | The M. W. Kellogg Company | Enhanced olefin recovery method |
| 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 |
| CN103304358A (en) * | 2013-05-29 | 2013-09-18 | 中建安装工程有限公司 | Separating method and equipment of low-carbon olefins beneficial to product recovery |
| 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 |
| WO2018048073A1 (en) * | 2016-09-09 | 2018-03-15 | 주식회사 효성 | Method for preparing ethylene in propylene preparation process using propane dehydrogenation reaction |
| WO2018052437A1 (en) * | 2016-09-16 | 2018-03-22 | Lummus Technology Inc. | Integrated propane dehydrogenation process |
| CN209310365U (en) * | 2018-06-14 | 2019-08-27 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device |
-
2018
- 2018-06-14 CN CN201810611992.XA patent/CN108645119B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5421167A (en) * | 1994-04-01 | 1995-06-06 | The M. W. Kellogg Company | Enhanced olefin recovery method |
| 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 |
| CN103304358A (en) * | 2013-05-29 | 2013-09-18 | 中建安装工程有限公司 | Separating method and equipment of low-carbon olefins beneficial to product recovery |
| 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 |
| WO2018048073A1 (en) * | 2016-09-09 | 2018-03-15 | 주식회사 효성 | Method for preparing ethylene in propylene preparation process using propane dehydrogenation reaction |
| WO2018052437A1 (en) * | 2016-09-16 | 2018-03-22 | Lummus Technology Inc. | Integrated propane dehydrogenation process |
| CN209310365U (en) * | 2018-06-14 | 2019-08-27 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device |
Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112939724A (en) * | 2019-12-11 | 2021-06-11 | 中国石油化工股份有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| CN112939724B (en) * | 2019-12-11 | 2022-09-20 | 中国石油化工股份有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| WO2021143418A1 (en) * | 2020-01-15 | 2021-07-22 | 浙江卫星能源有限公司 | Cryogenic separation process for dehydrogenation of propane into propylene |
| CN111454115A (en) * | 2020-05-15 | 2020-07-28 | 天津渤海石化有限公司 | Feeding method and device for process for preparing propylene by propane cracking dehydrogenation |
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| CN111848327A (en) * | 2020-07-08 | 2020-10-30 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111875467A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
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| 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 |
| CN114576928B (en) * | 2020-11-30 | 2024-05-10 | 惠生工程（中国）有限公司 | Overlapping refrigeration separation system and method for propane dehydrogenation reaction product |
| CN114543444A (en) * | 2022-02-28 | 2022-05-27 | 杭州中泰深冷技术股份有限公司 | Multi-refrigerant cold box separation system for propane dehydrogenation and process method |
| CN114992983A (en) * | 2022-03-21 | 2022-09-02 | 江苏卓然恒泰低温科技有限公司 | Low-temperature separation cold box for propane dehydrogenation |
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