CN118126745A - Hydrocarbon conversion device and conversion method - Google Patents
Hydrocarbon conversion device and conversion method Download PDFInfo
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- CN118126745A CN118126745A CN202211531455.7A CN202211531455A CN118126745A CN 118126745 A CN118126745 A CN 118126745A CN 202211531455 A CN202211531455 A CN 202211531455A CN 118126745 A CN118126745 A CN 118126745A
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- butane
- isobutane
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 30
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 24
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 24
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 23
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims abstract description 106
- 238000000926 separation method Methods 0.000 claims abstract description 92
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 77
- 239000001282 iso-butane Substances 0.000 claims abstract description 53
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000000047 product Substances 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 239000007791 liquid phase Substances 0.000 claims abstract description 28
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 14
- 238000012545 processing Methods 0.000 claims abstract description 3
- 239000001257 hydrogen Substances 0.000 claims description 49
- 229910052739 hydrogen Inorganic materials 0.000 claims description 49
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 42
- 239000002994 raw material Substances 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 14
- 238000010992 reflux Methods 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 3
- 238000011426 transformation method Methods 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 11
- 238000006317 isomerization reaction Methods 0.000 abstract description 5
- 239000001273 butane Substances 0.000 abstract description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 abstract description 3
- 239000012535 impurity Substances 0.000 description 20
- 150000002431 hydrogen Chemical class 0.000 description 7
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- GYCMBHHDWRMZGG-UHFFFAOYSA-N Methylacrylonitrile Chemical compound CC(=C)C#N GYCMBHHDWRMZGG-UHFFFAOYSA-N 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229920005549 butyl rubber Polymers 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/13—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation with simultaneous isomerisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4205—Reflux ratio control splitter
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
- C10G2300/1092—C2-C4 olefins
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Crystallography & Structural Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The application discloses a hydrocarbon conversion device and a conversion method, wherein the hydrocarbon conversion device comprises a reaction unit and a separation processing unit which are sequentially connected; the reaction unit comprises a reactor, wherein the reactor comprises a reactor inlet I, a reactor inlet II and a reaction product outlet; the separation treatment unit comprises a gas-liquid separation tank, a separation tower, an isobutane tower and a normal butane tower; the gas-liquid separation tank comprises a gas phase outlet and a liquid phase outlet; the liquid phase outlet is connected with the separation tower, the top of the separation tower is connected with the isobutane tower, and the bottom of the separation tower is connected with the n-butane tower; and the reaction product outlet is connected with the gas-liquid separation tank. The conversion device and the conversion method disclosed by the application can be used for preparing butane products by isobutene isomerization and hydrogenation, and are continuous in process, simple in flow, high in product purity and suitable for industrial large-scale continuous operation.
Description
Technical Field
The application relates to a hydrocarbon conversion device and a hydrocarbon conversion method, and belongs to the technical field of chemical industry.
Background
The carbon tetrad is a byproduct of the production process of preparing ethylene, preparing olefin by methanol and the like by naphtha pyrolysis, is rich in carbon tetrad/olefin, and is an important chemical raw material. The method can be used as fuel for production and living, and can also be used for obtaining chemical products such as high-purity n-butane, isobutane, n-butene, isobutene and the like through a purification process, wherein the isobutene is mainly used for oil product preparation and methyl tert-butyl ether (MTBE) synthesis, the chemical products such as butyl rubber, methacrylonitrile, antioxidants and the like are produced, the market demand is limited, and the development of a novel production process of isobutene downstream derivatives becomes a problem to be solved urgently. N-butane is an important chemical product obtained by purifying byproducts in the oil refining process, and can be directly used as fuel and also used as an extraction solvent of subcritical biotechnology. With the continuous expansion of the technology for preparing ethylene by thermal cracking of n-butane and the technology for preparing maleic anhydride by n-butane in recent years, the demand for high-purity n-butane is increased, and meanwhile, the supply shortage of n-butane resources in China further promotes the n-butane market to be up-going. The market correspondence effect of the isobutene and the n-butane is known, and the method has great scientific and economic significance for researching and exploring the technology for preparing the n-butane by the normal hydrogenation of the isobutene.
Chinese application CN107285978a discloses a process for preparing n-butane from tetra-alkane, wherein the process adopts a three-tower process comprising a light component removal tower, a butane tower and a heavy component removal tower to implement raw material pretreatment and product refining, the method adopts multi-tower operation, the equipment occupation and investment are large, and meanwhile, the separation of light impurities in the reaction product is not considered, and the process operation difficulty and the raw material and catalyst requirements are high.
Chinese application CN108530254a discloses a method for preparing n-butane from a mixture of carbon four, in which the process includes hydrodesulfurizing a raw material of the mixture of carbon four, separating n-butane product and isobutane raw material by rectification, and obtaining n-butane product by normal reaction.
Chinese application CN104892339a discloses a method for preparing n-butane from isobutane, which uses 80% wt or more pure isobutane as raw material to produce n-butane through hydrogenation saturation normal structure, separates noncondensable gas through flash evaporation, and obtains n-butane product through rectification. The method does not consider the recycling of the process hydrogen, adopts two towers to separate light impurities, improves investment cost, and does not consider the separation of heavy impurities, thereby reducing the quality of the n-butane product.
In the existing research, the related information of n-butane preparation by isobutene is very rare, the problems of higher equipment cost, insufficient impurity separation and the like of the technology for preparing n-butane by the rest carbon four compounds generally exist, and the related problems are necessary to be studied deeply.
Disclosure of Invention
The application provides a hydrocarbon conversion method, which takes isobutene and hydrogen as raw materials, normal hydrogenation is carried out on isobutene, normal butane and isobutane products are obtained through separation, the process is continuous, the flow is simple, the product purity is high, and the method is suitable for industrial large-scale continuous operation.
According to an aspect of the present application, there is provided a hydrocarbon conversion apparatus including a reaction unit and a separation processing unit connected in sequence;
the reaction unit comprises a reactor, wherein the reactor comprises a reactor inlet I, a reactor inlet II and a reaction product outlet;
The separation treatment unit comprises a gas-liquid separation tank, a separation tower, an isobutane tower and a normal butane tower;
The gas-liquid separation tank comprises a gas phase outlet and a liquid phase outlet;
the liquid phase outlet is connected with the separation tower, the top of the separation tower is connected with the isobutane tower, and the bottom of the separation tower is connected with the n-butane tower;
And the reaction product outlet is connected with the gas-liquid separation tank.
Optionally, the hydrocarbon conversion apparatus further comprises a hydrogen compressor and a hydrogen preheater;
the gas phase outlet is connected with a hydrogen compressor, and the hydrogen compressor is connected with a hydrogen preheater.
Optionally, the separation column is a rectifying column.
Optionally, the reflux ratio of the separation tower is 0.1-50.
Optionally, the reflux ratio of the separation tower is selected from any value of 0.1, 1, 5, 10, 20, 30, 40 and 50 or a range value between any two points.
Optionally, the theoretical plates of the separation tower are 20-100.
Optionally, the theoretical plate number of the separation tower is selected from any value of 20 blocks, 30 blocks, 50 blocks, 70 blocks and 100 blocks or a range value between any two points.
Optionally, the isobutane column is a rectifying column.
Optionally, the reflux ratio of the isobutane tower is 5-70.
Optionally, the reflux ratio of the isobutane tower is selected from any one value or range value between any two points of 5, 10, 20, 30, 40, 50, 60 and 70.
Optionally, the number of theoretical plates of the isobutane tower is 10-80.
Optionally, the number of theoretical plates of the isobutane tower is selected from any value of 10 blocks, 20 blocks, 50 blocks, 70 blocks and 80 blocks or a range value between any two points.
Optionally, the n-butane column is a rectifying column.
Optionally, the reflux ratio of the n-butane tower is 0.1-10.
Optionally, the reflux ratio of the n-butane tower is selected from any value of 0.1, 1,2, 5, 7 and 10 or a range value between any two points.
Optionally, the theoretical plates of the n-butane tower are 10-80.
Optionally, the theoretical plate number of the n-butane tower is selected from any value of 10 blocks, 20 blocks, 30 blocks, 50 blocks and 80 blocks or a range value between any two points.
According to another aspect of the present application, there is provided a hydrocarbon conversion method comprising:
introducing isobutene raw materials and hydrogen into a conversion device, and reacting to obtain a product containing isobutane and n-butane;
The conversion device is selected from the hydrocarbon conversion devices described above.
Optionally, the method specifically comprises the following steps:
(1) Mixing an isobutene raw material through a reactor inlet I with a hydrogen raw material introduced through a reactor inlet II, and introducing the mixture into a reactor together for reaction to obtain a reaction product;
(2) Introducing the reaction product into a gas-liquid separation tank, and separating to generate a gas phase component and a liquid phase component;
The gas phase component enters a hydrogen compressor through a gas phase outlet and then is introduced into the reactor through a reactor inlet II; the liquid phase component enters the separation tower through a liquid phase outlet;
(3) The liquid phase component enters a separation tower, is rectified, the top of the separation tower is separated to obtain a product containing isobutane, and the bottom of the separation tower is separated to obtain a product containing n-butane;
(4) Introducing the isobutane-containing product into an isobutane tower for separation, and obtaining isobutane at the bottom of the isobutane tower; and (3) introducing the n-butane product into a n-butane tower for separation, and obtaining n-butane at the top of the n-butane tower.
Optionally, in the step (1), the reaction temperature is-60 ℃; the pressure of the reaction is 0.1-10 Mpa.
Alternatively, the temperature of the reaction is selected from any value of-60 ℃, -50 ℃, -20 ℃,0 ℃, 20 ℃, 60 ℃ or a range of values between any two of the above.
Alternatively, the pressure of the reaction is selected from any value of 0.1Mpa, 1Mpa, 2Mpa, 5Mpa, 8Mpa, 10Mpa or a range between any two points.
Optionally, the temperature of the top of the separation tower is-40-60 ℃; the pressure at the top of the separation tower is 0.5-5 MPa.
Optionally, the top temperature of the separation column is selected from any value of-40 ℃, -20 ℃, -10 ℃, 0 ℃, 20 ℃, 60 ℃ or a range value between any two points.
Optionally, the top pressure of the separation tower is selected from any value of 0.5Mpa, 1Mpa, 2Mpa, 3Mpa, 4Mpa and 5Mpa or a range value between any two points.
Optionally, the temperature of the top of the isobutane tower is-60 ℃; the top pressure of the isobutane tower is 0.5-5 Mpa.
Optionally, the top temperature of the isobutane tower is selected from any value of-60 ℃, -40 ℃, -20 ℃, -10 ℃, 0 ℃, 20 ℃, 60 ℃ or a range value between any two points.
Optionally, the top pressure of the isobutane tower is selected from any value of 0.5Mpa, 1Mpa, 2Mpa, 3Mpa, 4Mpa and 5Mpa or a range value between any two points.
Optionally, the temperature of the top of the n-butane tower is-30-60 ℃; the top pressure of the n-butane tower is 0.1-2 MPa.
Optionally, the top temperature of the n-butane tower is selected from any value of-30 ℃, -20 ℃, -10 ℃, 0 ℃, 10 ℃, 20 ℃ and 60 ℃ or a range value between any two points.
Optionally, the top pressure of the n-butane tower is selected from any value of 0.1Mpa, 0.5Mpa, 1Mpa, 1.5Mpa and 2Mpa or a range value between any two points.
Optionally, the isobutylene feedstock and the hydrogen feedstock are preheated by a preheater and then enter the reactor.
As a specific implementation mode, the application is realized by the following technical scheme:
A hydrocarbon conversion method, which uses isobutene and hydrogen as raw materials, comprises the following parts: the device comprises a raw material preheater, a hydrogen preheater, a reactor, a condenser, a gas-liquid separation tank, a hydrogen compressor, a condensate pump, a separation tower, a booster pump, an isobutane tower and a normal butane tower.
The isobutene raw material is heated to the reaction temperature in a raw material preheater, and meanwhile, fresh hydrogen and circulating hydrogen are mixed and then heated to the reaction temperature in a hydrogen preheater, and the mixture and isobutene are fed into a reactor together to carry out catalytic isomerization hydrogenation reaction. The isomerism hydrogenation reaction product sent out by the reactor is condensed in a condenser, gas-liquid two phases are formed at low temperature, gas-liquid separation is realized in a gas-liquid separation tank, unreacted hydrogen separated by the gas-liquid separation tank is pressurized by a hydrogen compressor and then is mixed with fresh hydrogen for recycling, and liquid phase separated by the gas-liquid separation tank is pressurized by a condensate pump and then sent to a separation tower. Separating out liquid phase isobutane, light impurities and non-condensable gas at the top of the separation tower by fractional condensation rectification, pressurizing the liquid phase at the top of the separation tower by a pressurizing pump, then delivering the liquid phase to the isobutane tower, obtaining n-butane and heavy impurities at the bottom of the separation tower, and delivering the n-butane to the n-butane tower. The liquid phase from the top of the separation tower is separated in an isobutane tower through rectification, light impurity waste gas is discharged from the top of the separation tower, an isobutane product is obtained from the bottom of the separation tower, n-butane and heavy impurity fluid are separated in an n-butane tower through rectification, an n-butane product is obtained from the top of the separation tower, and heavy impurity oil is discharged from the bottom of the separation tower.
Optionally, the reaction product at the outlet of the reactor is cooled and flashed to separate out unreacted hydrogen, and the unreacted hydrogen is pressurized by a hydrogen compressor and recycled.
Alternatively, the reaction product at the outlet of the reactor can be cooled directly by using public engineering, or can exchange heat with the reaction raw material, and the cold energy is recovered and then cooled by using public engineering.
Optionally, a high-pressure dephlegmator is used at the top of the separation column to separate non-condensable waste gases.
Alternatively, the top of the isobutane tower adopts a partial condenser, and only gaseous products are extracted as light impurity waste gas.
Optionally, the n-butane tower adopts full condensation rectification to separate out n-butane products.
Optionally, the heat exchange temperature of the condenser is-60 ℃.
Optionally, the separation pressure of the gas-liquid separation tank is 0.1-10 MPa.
The application has the beneficial effects that:
The hydrocarbon conversion device and the hydrocarbon conversion method disclosed by the application can be used for preparing butane products by isobutene isomerization and hydrogenation, and are continuous in process, concise in flow, high in product purity and suitable for industrial large-scale continuous operation.
Drawings
FIG. 1 is a schematic diagram of a hydrocarbon conversion apparatus in accordance with an embodiment of the present application.
Wherein: 1. the device comprises a raw material preheater 2, a hydrogen preheater 3, a reactor 4, a condenser 5, a gas-liquid separation tank 6, a hydrogen compressor 7, a condensate pump 8, a separation tower 9, a booster pump 10, an isobutane tower 11 and an n-butane tower.
Detailed Description
The present application is described in detail below with reference to examples, but the present application is not limited to these examples.
Unless otherwise indicated, all starting materials in the examples of the present application were purchased commercially.
Example 1
A hydrocarbon conversion apparatus, as shown in FIG. 1, comprises a raw material preheater 1, a hydrogen preheater 2, a reactor 3, a condenser 4, a gas-liquid separation tank 5, a hydrogen compressor 6, a condensate pump 7, a separation column 8, a booster pump 9, an isobutane column 10 and an n-butane column 11.
The isobutene raw material is heated to the reaction temperature in a raw material preheater 1; mixing fresh hydrogen and circulating hydrogen, heating to a reaction temperature in a hydrogen preheater 2, and sending the mixture and isobutene into a reactor 3 to perform catalytic isomerization hydrogenation reaction; the isomerism hydrogenation reaction product sent out from the reactor 3 is condensed in a condenser 4, forms gas-liquid two phases at low temperature, and realizes gas-liquid separation in a gas-liquid separation tank 5; unreacted hydrogen separated by the gas-liquid separation tank 5 is pressurized by the hydrogen compressor 6 and then mixed with fresh hydrogen for recycling; the liquid phase separated by the gas-liquid separation tank 5 is sent to a separation tower 8 after being pressurized by a condensate pump 7; separating out liquid phase isobutane, light impurities and non-condensable gas at the top of a separating tower 8 by fractional condensation and rectification, pressurizing a liquid phase at the top of the tower by a pressurizing pump 9, sending the liquid phase to an isobutane tower 10, obtaining n-butane and heavy impurities at the bottom of the tower, and sending the n-butane and heavy impurities to an n-butane tower 11; the liquid phase from the top of the separation tower 8 is separated in an isobutane tower 10 by rectification, light impurity waste gas is discharged from the top of the tower, and an isobutane product is obtained from the bottom of the tower; the normal butane and the heavy impurity fluid are separated in the normal butane tower 11 through rectification, the normal butane product is obtained at the top of the tower, and the heavy impurity oil is discharged at the bottom of the tower.
Example 2
The isobutene raw material is heated to 230 ℃ in a raw material preheater 1, meanwhile, fresh hydrogen and circulating hydrogen are mixed and then heated to 230 ℃ in a hydrogen preheater 2, and the mixture and isobutene are fed into a reactor 3 together, and catalytic isomerization hydrogenation reaction is carried out under the pressure of 2.4 MPa. The isomerism hydrogenation reaction product sent out by the reactor 3 is condensed to-30 ℃ in a condenser 4, gas-liquid two phases are formed at low temperature, gas-liquid separation is realized in a gas-liquid separation tank 5, unreacted hydrogen separated by the gas-liquid separation tank 5 is pressurized to 2.5MPa by a hydrogen compressor 6 and then returns to the inlet of a hydrogen preheater 2 to be mixed with fresh hydrogen, and the separated liquid phase is pressurized by a condensate pump 7 and then sent to a separation tower 8. The separation tower 8 adopts fractional condensation rectification, the tower top pressure is 1.4MPa, the tower top temperature is-5 ℃, the reflux ratio is 20, 80 theoretical plates are arranged, the liquid phase of isobutane, light impurities and non-condensable gas are separated from the tower top, the liquid phase is pressurized by the pressurizing pump 9 and then sent to the isobutane tower 10, the tower bottom is provided with n-butane and heavy impurities, and the n-butane tower 11 is provided with the liquid phase. The isobutane tower 10 adopts fractional condensation rectification, the tower top pressure is 2.1MPa, the tower top temperature is minus 31 ℃, the reflux ratio is 40, 40 theoretical plates are arranged, only light impurity waste gas is discharged from the tower top, and the isobutane product with the purity of 99.5 weight percent is obtained at the tower bottom. The n-butane tower 11 adopts full condensation rectification, the tower top pressure is 0.3MPa, the tower top temperature is 42 ℃, the reflux ratio is 0.5, 30 theoretical plates are arranged, the n-butane product with the purity of 99.6wt% is obtained at the tower top, and the heavy impurity oil is discharged at the tower bottom.
While the application has been described in terms of preferred embodiments, it will be understood by those skilled in the art that various changes and modifications can be made without departing from the scope of the application, and it is intended that the application is not limited to the specific embodiments disclosed.
Claims (10)
1. A hydrocarbon conversion apparatus, characterized in that the hydrocarbon conversion apparatus comprises a reaction unit and a separation processing unit connected in sequence;
the reaction unit comprises a reactor, wherein the reactor comprises a reactor inlet I, a reactor inlet II and a reaction product outlet;
The separation treatment unit comprises a gas-liquid separation tank, a separation tower, an isobutane tower and a normal butane tower;
The gas-liquid separation tank comprises a gas phase outlet and a liquid phase outlet;
the liquid phase outlet is connected with the separation tower, the top of the separation tower is connected with the isobutane tower, and the bottom of the separation tower is connected with the n-butane tower;
And the reaction product outlet is connected with the gas-liquid separation tank.
2. The hydrocarbon conversion apparatus of claim 1, further comprising a hydrogen compressor, a hydrogen preheater;
the gas phase outlet is connected with a hydrogen compressor, and the hydrogen compressor is connected with a hydrogen preheater.
3. The hydrocarbon conversion apparatus of claim 1, wherein said separation column is a rectifying column;
The reflux ratio of the separation tower is 0.1-50;
the theoretical plates of the separation tower are 20-100.
4. The hydrocarbon conversion apparatus of claim 1, wherein,
The isobutane tower is a rectifying tower;
The reflux ratio of the isobutane tower is 5-70;
The number of theoretical plates of the isobutane tower is 10-80.
5. The hydrocarbon conversion apparatus of claim 1, wherein,
The n-butane tower is a rectifying tower;
the reflux ratio of the n-butane tower is 0.1-10;
The theoretical plates of the n-butane tower are 10-80.
6. A method of converting hydrocarbons, the method comprising:
introducing isobutene raw materials and hydrogen into a conversion device, and reacting to obtain a product containing isobutane and n-butane;
the conversion device is selected from the hydrocarbon conversion device of any one of claims 1 to 5.
7. The transformation method according to claim 6, comprising the steps of:
(1) Mixing an isobutene raw material through a reactor inlet I with a hydrogen raw material introduced through a reactor inlet II, and introducing the mixture into a reactor together for reaction to obtain a reaction product;
(2) Introducing the reaction product into a gas-liquid separation tank, and separating to generate a gas phase component and a liquid phase component;
The gas phase component enters a hydrogen compressor through a gas phase outlet and then is introduced into the reactor through a reactor inlet II; the liquid phase component enters the separation tower through a liquid phase outlet;
(3) The liquid phase component enters a separation tower, is rectified, the top of the separation tower is separated to obtain a product containing isobutane, and the bottom of the separation tower is separated to obtain a product containing n-butane;
(4) Introducing the isobutane-containing product into an isobutane tower for separation, and obtaining isobutane at the bottom of the isobutane tower; and (3) introducing the n-butane product into a n-butane tower for separation, and obtaining n-butane at the top of the n-butane tower.
8. The conversion process according to claim 7, wherein in step (1), the temperature of the reaction is-60 to 60 ℃; the pressure of the reaction is 0.1-10 Mpa.
9. The conversion process according to claim 7, wherein the overhead temperature of the separation column is from-40 to 60 ℃; the pressure at the top of the separation tower is 0.5-5 MPa;
preferably, the temperature of the top of the isobutane tower is-60 ℃; the top pressure of the isobutane tower is 0.5-5 Mpa;
preferably, the temperature of the top of the n-butane tower is-30-60 ℃; the top pressure of the n-butane tower is 0.1-2 MPa.
10. The conversion process of claim 7 wherein the isobutylene feedstock and the hydrogen feedstock are preheated by a preheater before entering the reactor.
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