CN116262217A - Heterogeneous hydrocarbon conversion device and conversion method thereof - Google Patents

Heterogeneous hydrocarbon conversion device and conversion method thereof Download PDF

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Publication number
CN116262217A
CN116262217A CN202111518314.7A CN202111518314A CN116262217A CN 116262217 A CN116262217 A CN 116262217A CN 202111518314 A CN202111518314 A CN 202111518314A CN 116262217 A CN116262217 A CN 116262217A
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liquid phase
reactor
inlet
gas
unit
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丁辉
黄声骏
张大治
邹明明
焦雨桐
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Dalian Institute of Chemical Physics of CAS
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Dalian Institute of Chemical Physics of CAS
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2767—Changing the number of side-chains
    • C07C5/277—Catalytic processes
    • C07C5/2775—Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
    • C07C2529/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing iron group metals, noble metals or copper
    • C07C2529/44—Noble metals

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The application discloses a conversion device and a conversion method of an isomerism hydrocarbon, wherein the process flow adopts the sequential cyclic operation of reaction, step cooling separation and rectification, and the isomerism hydrocarbon conversion device is a cyclic reaction device and comprises a reaction unit, a cooling separation unit and a rectification unit which are connected in sequence; the reaction unit comprises a reactor; the cooling separation unit is a two-stage gas-liquid phase separation unit and comprises a first-stage gas-liquid phase separation device and a second-stage gas-liquid phase separation device which are sequentially connected; the rectification unit comprises a rectification tower. The method can be used for continuous production of 2-butene from heterogeneous hydrocarbon, avoids the method of separating isobutene by adding an etherification unit in the traditional process, has simple flow, is easy to operate and reduces the production cost.

Description

Heterogeneous hydrocarbon conversion device and conversion method thereof
Technical Field
The application relates to a conversion device and a conversion method of heterogeneous hydrocarbon, and belongs to the technical field of chemical industry.
Background
Isobutene is one of typical carbon four side products in petroleum refining industry, is mainly used for oil modulation and methyl tert-butyl ether (MTBE) synthesis, and is limited in market demand for producing chemical products such as butyl rubber, methacrylonitrile, antioxidants and the like. Meanwhile, as the emerging industries such as ethanol biofuel and the like rise, ethanol gasoline starts to be popularized, and oxygenated compounds such as MTBE and the like cannot be continuously used as gasoline additive components, the market demand of isobutene further shrink, and development of a novel production process of isobutene downstream derivatives becomes a problem to be solved urgently.
Chinese patent CN112441865 discloses a process for preparing n-butene from isobutene. The method adopts two-step hydrogen-free reaction, isobutene is normal-structured into butene-1 intermediate products, and then butene-1 is isomerized into butene-2.
Chinese patent CN112441866 discloses a process for preparing n-butene from isobutene. The method introduces an etherification reaction and separation device to refine isobutene in the carbon four raw materials, and then produces normal butene products through hydrogen-free isomerization.
Chinese patent CN108997075 discloses an isobutene isomerization method, which uses hydrotalcite roasting product as carrier to load platinum group metal to synthesize isomerism catalyst, realizing target product selectivity of 99.87%, and maximum yield of 47.28%.
The invention explores the preparation of normal butene from isobutene, the main content is catalyst development, and carrier gas separation and recycling are not considered in the process design.
Disclosure of Invention
The invention provides an isomerism hydrocarbon conversion device and a conversion method thereof, wherein the device realizes carrier gas separation and recovery through secondary condensation separation, and realizes separation of a non-condensable gas-raw material-product system through a fractional condensation rectification method, thereby simplifying the production flow and reducing the production cost.
In one aspect of the present application, there is provided an heterogeneous hydrocarbon conversion apparatus, the heterogeneous hydrocarbon conversion apparatus being a cyclic reaction apparatus;
the heterogeneous hydrocarbon conversion device comprises a reaction unit, a cooling separation unit and a rectification unit which are connected in sequence;
the reaction unit comprises a reactor, wherein the reactor comprises a reactor inlet and a reaction product outlet;
the cooling separation unit is a two-stage gas-liquid phase separation unit and comprises a first-stage gas-liquid phase separation device and a second-stage gas-liquid phase separation device which are sequentially connected;
the first-stage gas-liquid phase separation device is provided with a first inlet, a gas phase outlet I and a liquid phase outlet I; the second-stage gas-liquid phase separation device is provided with a second inlet, a gas phase outlet II and a liquid phase outlet II;
the reaction product outlet is communicated with the first inlet through a pipeline, and the gas phase outlet I is communicated with the second inlet through a pipeline; the gas phase outlet II is communicated with the reactor inlet pipeline;
the rectifying unit comprises a rectifying tower, the rectifying tower comprises a rectifying unit inlet I and a rectifying unit inlet II, and a rectifying unit liquid phase outlet I is positioned at the bottom of the rectifying tower;
and the liquid phase outlet I and the liquid phase outlet II are respectively communicated with the pipeline of the inlet I and the pipeline of the inlet II of the rectifying unit.
Optionally, the rectifying tower further comprises a rectifying unit liquid phase outlet II and a rectifying unit gas phase outlet, and the rectifying unit liquid phase outlet II is communicated with the reactor inlet pipeline.
Optionally, the heterogeneous hydrocarbon conversion apparatus further includes a feedstock supply end I, a feedstock supply end II;
the reaction unit also comprises a preheater I and a preheater II;
the raw material supply end I, the preheater I and the reactor inlet are sequentially communicated through a pipeline;
the raw material supply end II, the preheater II and the inlet of the reactor are sequentially communicated through a pipeline.
Optionally, a cooling device I is arranged on a pipeline for communicating the reaction product outlet with the first inlet;
and a cooling device II is arranged on a pipeline for communicating the gas phase outlet I with the second inlet.
Optionally, a pressurizing device is arranged on a pipeline for communicating the gas phase outlet II with the inlet of the reactor.
Optionally, the theoretical plate number of the rectifying tower is 30-110;
optionally, the upper limit of the theoretical plate number of the rectifying tower can be independently selected from 45 blocks, 65 blocks, 85 blocks, 100 blocks and 110 blocks; the lower limit may be independently selected from 30 blocks, 45 blocks, 65 blocks, 85 blocks, 100 blocks.
Optionally, the reflux ratio of the rectifying tower is 5-50.
In another aspect of the present application, there is provided a conversion method of heterogeneous hydrocarbons, the conversion method comprising: introducing a raw material containing hydrogen and isobutene into a reaction device containing a catalyst through a reactor inlet, and reacting to obtain a product containing 2-butene;
wherein the reaction device is selected from the heterogeneous hydrocarbon conversion device.
Optionally, the method specifically comprises the following steps:
(1) Raw materials containing hydrogen and isobutene enter a reactor to perform catalytic reaction through an inlet of the reactor to obtain a reaction product;
wherein a catalyst is arranged in the reactor;
(2) The reaction product is separated into a gas phase I and a liquid phase I through a first-stage gas-liquid phase separation device; the gas phase I enters a second-stage gas-liquid phase separation device through a gas phase outlet I to be subjected to secondary cooling separation, and a gas phase II and a liquid phase II are separated;
the gas phase II enters the reactor through a gas phase outlet II;
the liquid phase I enters the rectifying tower through a liquid phase outlet II;
the liquid phase II enters the rectifying tower through a liquid phase outlet II;
(3) The liquid phase I and the liquid phase II are rectified by a rectifying tower to separate a product containing 2-butene, a liquid phase raw material and a gas phase III;
the gas phase III is discharged through a gas phase outlet of the rectification unit, a product containing 2-butene is discharged through a liquid phase outlet I of the rectification unit, and a liquid phase raw material enters the reactor through a liquid phase outlet II of the rectification unit.
Optionally, the gas phase II is a mixed gas containing hydrogen
Optionally, the cooling temperature of the first-stage gas-liquid phase separation device is 42-65 ℃;
alternatively, the upper limit of the cooling temperature of the first stage gas-liquid phase separation device can be independently selected from 45 ℃, 50 ℃, 55 ℃, 60 ℃ and 65 ℃; the lower limit can be independently selected from 42 ℃, 45 ℃, 50 ℃, 55 ℃, 60 ℃.
Optionally, the cooling temperature of the second-stage gas-liquid phase separation device is-60 to-10 ℃;
alternatively, the upper cooling temperature limit of the second stage gas-liquid phase separation device can be independently selected from-50 ℃, -40 ℃, -30 ℃, -20 ℃, -10 ℃; the lower limit can be independently selected from-60 ℃, -50 ℃, -40 ℃, -30 ℃, -20 ℃.
Optionally, the operating pressure of the rectifying tower is 0.1-3.0 MPa;
alternatively, the upper limit of the operating pressure of the rectifying tower can be independently selected from 0.5MPa, 1MPa, 1.5MPa, 2MPa, 2.5MPa and 3MPa; the lower limit can be independently selected from 0.1MPa, 0.5MPa, 1MPa, 1.5MPa, 2MPa, 2.5MPa.
Optionally, the temperature of the top of the rectifying tower is-40-42 ℃;
alternatively, the upper temperature limit of the top of the rectifying tower can be independently selected from-30 ℃, -20 ℃, -10 ℃, 0 ℃, 10 ℃, 20 ℃, 30 ℃ and 42 ℃; the lower limit can be independently selected from-40 ℃, -30 ℃, -20 ℃, -10 ℃, 0 ℃, 10 ℃, 20 ℃ and 30 ℃.
Optionally, the catalytic reaction temperature is 450 ℃ to 600 ℃.
Alternatively, the upper catalytic reaction temperature limit may be independently selected from 500 ℃, 550 ℃, 600 ℃; the lower limit can be independently selected from 450 ℃, 500 ℃, 550 ℃;
optionally, the liquid phase raw material is preheated by a preheater II and then enters a reactor;
the gas phase II enters a reactor after being preheated by a preheater I;
the raw materials containing hydrogen and isobutene are preheated by a preheater I and a preheater II respectively and then enter a reactor;
optionally, the gas phase II enters the reactor after being pressurized by the pressurizing device.
Optionally, the liquid-phase raw material is an isobutene raw material with a mole fraction of more than or equal to 90%;
optionally, the 2-butene-containing product has a mass content of 2-butene of > 85%.
As a specific embodiment, the heterogeneous hydrocarbon conversion apparatus includes the following components:
a hydrogen preheater 1, a raw material preheater 2, a normal reactor 3, a condenser 4, a cooling separation tank 5 (namely, a first-stage gas-liquid phase separation device), a deep cooler 6, a deep cooling separation tank 7 (namely, a second-stage gas-liquid phase separation device), a circulating hydrogen compressor 8 and a separation tower 9.
As a specific embodiment, the method for converting the heterogeneous hydrocarbon comprises the following steps:
s001, heating hydrogen and isobutene raw materials in a hydrogen preheater 1 and a raw material preheater 2 respectively to a reaction temperature, and then feeding the heated hydrogen and isobutene raw materials into a normal reactor 3;
s002, the reaction raw materials are subjected to catalytic reaction in a normal reaction vessel 3 to obtain a normal reaction product;
s003, cooling and phase-separating the normal reaction product by a condenser 4, and then realizing gas-liquid phase separation in a cooling and separating tank 5;
s004, realizing secondary phase separation in a cryogenic separation tank 7 after the gas phase separated by the cooling separation tank 5 is subjected to cryogenic treatment by a cryogenic refrigerator 6, and recycling the gas phase after being pressurized by a circulating hydrogen compressor 8;
and S005, conveying liquid phases at the bottoms of the cooling separation tank 5 and the cryogenic separation tank 7 into a separation tower 9, carrying out mass transfer separation, discharging non-condensable gas at the top of the tower, separating out unreacted raw materials, recycling, and obtaining a 2-butene product at the bottom of the tower.
The beneficial effects that this application can produce include:
the method can continuously prepare the 2-butene product by taking isobutene as a raw material, avoids multi-unit combined operation, reduces the production cost and simplifies the operation flow.
Drawings
FIG. 1 is a schematic diagram of an heterogeneous hydrocarbon conversion apparatus of the present application.
Wherein:
1. a hydrogen preheater; 2. a raw material preheater; 3. a normal reactor; 3-1, reactor inlet; 3-2, reaction product outlet; 4. a condenser; 5. cooling the separation tank; 5-1, a first inlet; 5-2, a gas phase outlet I;5-3, a liquid phase outlet I; 6. a chiller; 7. a cryogenic separation tank; 7-1, a second inlet; 7-2, a liquid phase outlet II;7-3, a gas phase outlet II; 8. a recycle hydrogen compressor; 9. a rectifying tower; 9-1, inlet I of rectifying unit; 9-2, inlet II of the rectifying unit; 9-3, a liquid phase outlet I of the rectifying unit; 9-4, a liquid phase outlet II of the rectifying unit; 9-5, a gas phase outlet of the rectifying unit.
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, both the starting materials and the catalysts in the examples of the present application were purchased commercially.
Example 1
An implementation method of the present application, an heterogeneous hydrocarbon conversion apparatus is shown in fig. 1, including:
the hydrogen preheater 1 and the raw material preheater 2 are respectively connected with a reactor inlet 3-1 of a normal reactor 3, and a reaction product outlet 3-2 of the normal reactor 3 is connected with a first inlet 5-1 of a cooling separation tank 5 (a first-stage gas-liquid phase separation device) through a condenser 4; the gas phase outlet I5-2 of the cooling separation tank 5 is connected with the second inlet 7-1 of the cryogenic separation tank 7 (second-stage gas-liquid phase separation device) through the cryogenic refrigerator 6; the gas phase outlet II of the cryogenic separation tank 7 is connected with the hydrogen preheater 1 through a circulating hydrogen compressor 8; the liquid phase outlet I5-3 of the cooling separation tank 5 and the liquid phase outlet II7-3 of the cryogenic separation tank 7 are respectively connected with the rectifying unit inlet I9-1 and the rectifying unit inlet II9-2 of the rectifying tower 9; the rectification unit liquid phase outlet II9-4 of the rectification tower 9 is connected with the raw material preheater 2, and the rectification tower 9 is also provided with the rectification unit liquid phase outlet II9-4; and 9-5 parts of gas phase outlet of the rectification unit.
Example 2
The method comprises the steps of mixing circulating hydrogen and fresh hydrogen, heating the mixture to 560 ℃ in a hydrogen preheater 1, mixing circulating isobutene and fresh isobutene, heating the mixture to 560 ℃ in a raw material preheater 2, mixing the mixture with the heated hydrogen, sending the mixture to a normal reactor 3 through a reactor inlet 3-1 to generate normal reaction products, wherein the reaction adopts a ZSM-5 molecular sieve catalyst loaded with Pt metal, the molar ratio of the hydrogen to the isobutene is 0.5:1, and the reaction pressure is 2.4MPa. The normal reaction product is cooled to 42 ℃ through a reaction product outlet 3-2 and is separated into gas-liquid two phases in a condenser 4, gas-liquid phase separation is realized in a cooling separation tank 5, the separated gas phase I is subjected to deep cooling to-30 ℃ through a deep cooler 6 and then is separated again, secondary phase separation is realized in a deep cooling separation tank 7, the molar fraction of hydrogen in the gas phase II is 98.48%, and the gas phase II is pressurized to 3MPa through a circulating hydrogen compressor 8 and then is recycled. The liquid phase I and the liquid phase II at the bottoms of the cooling separation tank 5 and the cryogenic separation tank 7 are sent into a rectifying tower 9, the operating pressure of the rectifying tower 9 is 0.7MPa, the tower top temperature is 42 ℃, and 65 theoretical plates are arranged. The top of the rectifying tower 9 is provided with a dephlegmator, a small amount of gas phase III is separated to be non-condensable waste gas containing hydrogen, the liquid phase obtained from the top of the rectifying tower is a circulating isobutene raw material with the mol fraction of 90%, and the bottom of the rectifying tower is provided with a 2-butene product with the mass fraction of more than 85%.
The foregoing description is only a few examples of the present application and is not intended to limit the present application in any way, and although the present application is disclosed in the preferred examples, it is not intended to limit the present application, and any person skilled in the art may make some changes or modifications to the disclosed technology without departing from the scope of the technical solution of the present application, and the technical solution is equivalent to the equivalent embodiments.

Claims (10)

1. An isomerised hydrocarbon conversion apparatus, characterised in that,
the heterogeneous hydrocarbon conversion device is a circulating reaction device;
the heterogeneous hydrocarbon conversion device comprises a reaction unit, a cooling separation unit and a rectification unit which are connected in sequence;
the reaction unit comprises a reactor, wherein the reactor comprises a reactor inlet and a reaction product outlet;
the cooling separation unit is a two-stage gas-liquid phase separation unit and comprises a first-stage gas-liquid phase separation device and a second-stage gas-liquid phase separation device which are sequentially connected;
the first-stage gas-liquid phase separation device is provided with a first inlet, a gas phase outlet I and a liquid phase outlet I; the second-stage gas-liquid phase separation device is provided with a second inlet, a gas phase outlet II and a liquid phase outlet II;
the reaction product outlet is communicated with the first inlet through a pipeline, and the gas phase outlet I is communicated with the second inlet through a pipeline; the gas phase outlet II is communicated with the reactor inlet pipeline;
the rectifying unit comprises a rectifying tower, the rectifying tower comprises a rectifying unit inlet I and a rectifying unit inlet II, and a rectifying unit liquid phase outlet I is positioned at the bottom of the rectifying tower;
and the liquid phase outlet I and the liquid phase outlet II are respectively communicated with the pipeline of the inlet I and the pipeline of the inlet II of the rectifying unit.
2. The heterogeneous hydrocarbon conversion apparatus of claim 1, wherein,
the rectifying tower also comprises a rectifying unit liquid phase outlet II and a rectifying unit gas phase outlet, and the rectifying unit liquid phase outlet II is communicated with the reactor inlet pipeline.
3. The heterogeneous hydrocarbon conversion apparatus of claim 1, wherein,
the heterogeneous hydrocarbon conversion device also comprises a raw material supply end I and a raw material supply end II;
the reaction unit also comprises a preheater I and a preheater II;
the raw material supply end I, the preheater I and the reactor inlet are sequentially communicated through a pipeline;
the raw material supply end II, the preheater II and the inlet of the reactor are sequentially communicated through a pipeline.
4. The heterogeneous hydrocarbon conversion apparatus of claim 1, wherein,
a cooling device I is arranged on a pipeline for communicating the reaction product outlet with the first inlet;
and a cooling device II is arranged on a pipeline for communicating the gas phase outlet I with the second inlet.
5. The heterogeneous hydrocarbon conversion apparatus of claim 1, wherein,
and a pressurizing device is arranged on a pipeline for communicating the gas phase outlet II with the reactor inlet.
6. The heterogeneous hydrocarbon conversion apparatus of claim 1, wherein,
the theoretical plate number of the rectifying tower is 30-110;
the reflux ratio of the rectifying tower is 5-50.
7. A process for converting an isomeric hydrocarbon, said process comprising: introducing a raw material containing hydrogen and isobutene into a reaction device provided with a catalyst through a reactor inlet, and reacting to obtain a product containing 2-butene;
wherein the reaction device is selected from the heterogeneous hydrocarbon conversion apparatus of any one of claims 1 to 6.
8. The transformation method according to claim 7, comprising the steps of:
(1) Raw materials containing hydrogen and isobutene enter a reactor to perform catalytic reaction through an inlet of the reactor to obtain a reaction product;
wherein a catalyst is arranged in the reactor;
(2) The reaction product is separated into a gas phase I and a liquid phase I through a first-stage gas-liquid phase separation device; the gas phase I enters a second-stage gas-liquid phase separation device through a gas phase outlet I to be subjected to secondary cooling separation, and a gas phase II and a liquid phase II are separated;
the gas phase II enters the reactor through a gas phase outlet II;
the liquid phase I enters the rectifying tower through a liquid phase outlet II;
the liquid phase II enters the rectifying tower through a liquid phase outlet II;
(3) The liquid phase I and the liquid phase II are rectified by a rectifying tower to separate a product containing 2-butene, a liquid phase raw material and a gas phase III;
the gas phase III is discharged through a gas phase outlet of the rectification unit, a product containing 2-butene is discharged through a liquid phase outlet I of the rectification unit, and a liquid phase raw material enters the reactor through a liquid phase outlet II of the rectification unit.
9. The method of claim 8, wherein the method comprises the steps of,
the gas phase II is a mixed gas containing hydrogen;
the cooling temperature of the first-stage gas-liquid phase separation device is 42-65 ℃;
the cooling temperature of the second-stage gas-liquid phase separation device is-60 to-10 ℃;
the operating pressure of the rectifying tower is 0.1-3.0 MPa;
the temperature of the top of the rectifying tower is-40-42 ℃;
the catalytic reaction temperature is 450-600 ℃.
10. The method of claim 8, wherein the method comprises the steps of,
the liquid phase raw material enters a reactor after being preheated by a preheater II;
the gas phase II enters a reactor after being preheated by a preheater I;
the raw materials containing hydrogen and isobutene are preheated by a preheater I and a preheater II respectively and then enter a reactor;
preferably, the gas phase II enters the reactor after being pressurized by the pressurizing device;
preferably, the liquid-phase raw material is an isobutene raw material with a mole fraction of more than or equal to 90%;
the mass content of the 2-butene in the product containing the 2-butene is more than 85 percent.
CN202111518314.7A 2021-12-13 2021-12-13 Heterogeneous hydrocarbon conversion device and conversion method thereof Pending CN116262217A (en)

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Application Number Priority Date Filing Date Title
CN202111518314.7A CN116262217A (en) 2021-12-13 2021-12-13 Heterogeneous hydrocarbon conversion device and conversion method thereof

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Application Number Priority Date Filing Date Title
CN202111518314.7A CN116262217A (en) 2021-12-13 2021-12-13 Heterogeneous hydrocarbon conversion device and conversion method thereof

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CN116262217A true CN116262217A (en) 2023-06-16

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