CN115340436A - Separation device and separation method for olefin catalytic cracking - Google Patents
Separation device and separation method for olefin catalytic cracking Download PDFInfo
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- CN115340436A CN115340436A CN202110528868.9A CN202110528868A CN115340436A CN 115340436 A CN115340436 A CN 115340436A CN 202110528868 A CN202110528868 A CN 202110528868A CN 115340436 A CN115340436 A CN 115340436A
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- 238000000926 separation method Methods 0.000 title claims abstract description 126
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 86
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 64
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 425
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 388
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 86
- 239000012535 impurity Substances 0.000 claims abstract description 79
- 230000003197 catalytic effect Effects 0.000 claims abstract description 53
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000005977 Ethylene Substances 0.000 claims abstract description 50
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 50
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 50
- 239000006227 byproduct Substances 0.000 claims abstract description 33
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229920000642 polymer Polymers 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- 238000005984 hydrogenation reaction Methods 0.000 claims description 39
- 238000007872 degassing Methods 0.000 claims description 34
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 24
- 150000001993 dienes Chemical class 0.000 claims description 17
- 230000002745 absorbent Effects 0.000 claims description 15
- 239000002250 absorbent Substances 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 14
- 238000004064 recycling Methods 0.000 claims description 13
- 239000001294 propane Substances 0.000 claims description 12
- 238000004891 communication Methods 0.000 claims description 9
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims description 8
- 239000011261 inert gas Substances 0.000 claims description 8
- MWWATHDPGQKSAR-UHFFFAOYSA-N propyne Chemical group CC#C MWWATHDPGQKSAR-UHFFFAOYSA-N 0.000 claims description 5
- IYABWNGZIDDRAK-UHFFFAOYSA-N allene Chemical compound C=C=C IYABWNGZIDDRAK-UHFFFAOYSA-N 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 3
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- 238000000034 method Methods 0.000 description 10
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- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
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- 238000005194 fractionation Methods 0.000 description 3
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- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
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- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
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- 238000005504 petroleum refining Methods 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
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- 150000001361 allenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- IAQRGUVFOMOMEM-ARJAWSKDSA-N cis-but-2-ene Chemical compound C\C=C/C IAQRGUVFOMOMEM-ARJAWSKDSA-N 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
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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
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—Ethylene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The application provides a separation device and a separation method for olefin catalytic cracking, and belongs to the technical field of petrochemical industry and coal chemical industry. The device comprises: the device comprises an olefin catalytic cracker, a separation unit, a depropanization unit, an impurity removal unit, an ethane removal unit and a rectification unit; the olefin catalytic cracker, the separation unit, the depropanization unit, the impurity removal unit, the deethanization unit and the rectification unit are communicated in sequence; the olefin catalytic cracker is used for carrying out catalytic cracking reaction on the catalytic cracking byproducts to obtain reaction products; the separation unit, the depropanization unit, the impurity removal unit and the deethanization unit are respectively used for sequentially removing a carbon four-carbon five component, a carbon four component and inert impurities in a reaction product to obtain a carbon two component and a carbon three component; and the rectifying unit is used for rectifying the carbon two component and the carbon three component respectively to obtain polymer grade ethylene and polymer grade propylene. The device can obtain polymer-grade ethylene and polymer-grade propylene with high purity and high utilization rate, and can improve the utilization rate of catalytic cracking byproducts.
Description
Technical Field
The application relates to the technical field of petrochemical industry and coal chemical industry, in particular to a separation device and a separation method for olefin catalytic cracking.
Background
In the petroleum refining process, catalytic cracking is one of the main processes of petroleum refining; during catalytic cracking, more olefin byproducts are produced. And the olefin byproducts can be used for producing ethylene and propylene, so the olefin byproducts can be recycled by a byproduct separation device.
In the related art, the byproduct separation device comprises a fractionation unit, an absorption unit and a gas separation unit which are sequentially connected, and the olefin byproduct is fractionated, absorbed and subjected to gas separation treatment sequentially through the fractionation unit, the absorption unit and the gas separation unit.
The olefin by-product is subjected to fractionation, absorption and gas separation treatment to obtain a crude component; the crude component has lower purity and poorer quality, so that the utilization rate of the catalytic cracking by-product is low.
Disclosure of Invention
The embodiment of the application provides a separation device and a separation method for olefin catalytic cracking, which can improve the utilization rate of catalytic cracking byproducts. The technical scheme is as follows:
in one aspect, there is provided a separation apparatus for catalytic cracking of olefins, the apparatus comprising: the device comprises an olefin catalytic cracker, a separation unit, a depropanization unit, an impurity removal unit, an ethane removal unit and a rectification unit;
a feed inlet is formed in one side of the olefin catalytic cracker and used for inputting catalytic cracking byproducts;
the discharge hole of the olefin catalytic cracker is communicated with the feed hole of the separation unit, the discharge hole of the separation unit is communicated with the feed hole of the propane removal unit, the discharge hole of the propane removal unit is communicated with the feed hole of the impurity removal unit, the discharge hole of the impurity removal unit is communicated with the feed hole of the ethane removal unit, and the discharge hole of the ethane removal unit is communicated with the feed hole of the rectification unit;
the olefin catalytic cracker is used for carrying out catalytic cracking reaction on the catalytic cracking byproducts to obtain reaction products, and the reaction products are input into the separation unit;
the separation unit is used for receiving the reaction product, separating a first carbon component from a carbon four-carbon five-component in the reaction product, and inputting the first carbon component into the depropanization unit;
the depropanization unit is used for receiving the first carbon component, removing four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component into the impurity removal unit;
the impurity removing unit is used for receiving the second carbon component, removing inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the ethane removing unit;
the deethanization unit is used for receiving the third carbon component, separating a carbon two component and a carbon three component in the third carbon component, and respectively inputting the carbon two component and the carbon three component into the rectification unit;
the rectification unit is used for receiving the carbon two-component and the carbon three-component, and rectifying the carbon two-component and the carbon three-component respectively to obtain polymer-grade ethylene and polymer-grade propylene.
In one possible implementation, the separation unit comprises a heat exchanger, a first air press, and a separation column;
the feed inlet and the discharge outlet of the heat exchanger are respectively communicated with the discharge outlet of the olefin catalytic cracker and the feed inlet of the first air compressor, the discharge outlet of the first air compressor is communicated with the feed inlet of the separation tower, and the discharge outlet of the separation tower is communicated with the depropanization unit;
the heat exchanger is used for receiving the reaction product, cooling the reaction product to 35-45 ℃ and inputting the cooled reaction product into the first air compressor;
the first air compressor is used for receiving the cooled reaction product, boosting the pressure of the reaction product to 0.2-0.5Mpa, and inputting the reaction product into the separation tower;
the separation tower is used for receiving the reaction product after cooling and boosting, separating a first carbon component from a carbon four-carbon five-component in the reaction product, and inputting the first carbon component into the depropanization unit.
In one possible implementation, the depropanization unit comprises a second gas compressor and a depropanizer;
the feed inlet and the discharge outlet of the second air compressor are respectively communicated with the discharge outlet of the separation unit and the feed inlet of the depropanizing tower, and the discharge outlet of the depropanizing tower is communicated with the feed inlet of the impurity removal unit;
the second air compressor is used for receiving the first carbon component, boosting the pressure of the first carbon component to 1.8-4.0Mpa, and inputting the first carbon component into the depropanizing tower;
the depropanizer is used for receiving the first carbon component after pressure boosting, removing four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component into the impurity removing unit.
In a possible implementation manner, the apparatus further includes a first selective hydrogenation reactor, and the separation unit and the depropanization unit are respectively communicated with the olefin catalytic cracker through the first selective hydrogenation reactor;
and the first selective hydrogenation reactor is used for receiving the carbon four-carbon five component separated by the separation unit and the carbon four component separated by the depropanization unit, reducing the content of diene in the carbon four-carbon five component and the carbon four component, and inputting the reduced content of diene into the olefin catalytic cracker for reprocessing.
In one possible implementation, the impurity removal unit includes a dehydration column and a degassing column;
the feed inlet and the discharge outlet of the dehydration tower are respectively communicated with the discharge outlet of the propane removal unit and the feed inlet of the degassing tower, and the discharge outlet of the degassing tower is communicated with the feed inlet of the ethane removal unit;
the dehydration tower is used for receiving the second carbon component, dehydrating the second carbon component and inputting the dehydrated second carbon component into the degassing tower;
the degassing tower is used for receiving the dehydrated second carbon component, removing inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the deethanizing unit.
In one possible implementation, the lower part of the degassing column is provided with a reboiler;
and the reboiler is used for heating the inert impurities to vaporize the inert impurities in the second component into inert gases and then remove the inert gases.
In a possible realization, the upper part of the degassing tower is provided with an intermediate circulation cooler;
and the intermediate circulation cooler is used for cooling the absorbent in the degassing tower, so that the cooled absorbent absorbs the carbon two components in the second carbon component to obtain the third carbon component.
In one possible implementation, the rectification unit comprises an ethylene rectification column and a propylene rectification column;
the discharge holes of the deethanization unit comprise a first discharge hole and a second discharge hole, the feed inlet of the ethylene rectifying tower is communicated with the first discharge hole of the deethanization unit, and the feed inlet of the propylene rectifying tower is communicated with the second discharge hole of the deethanization unit;
the ethylene rectifying tower is used for receiving the carbon two-component and rectifying the carbon two-component to obtain polymer-grade ethylene;
and the propylene rectifying tower is used for receiving the carbon three components and rectifying the carbon three components to obtain polymer-grade propylene.
In a possible implementation manner, the apparatus further includes a second selective hydrogenation reactor and a third selective hydrogenation reactor, and the ethylene rectification column and the propylene rectification column are respectively communicated with the deethanizing unit through the second selective hydrogenation reactor and the third selective hydrogenation reactor;
the second selective hydrogenation reactor is used for receiving the carbon two components, reducing the acetylene content in the carbon two components and inputting the reduced acetylene content into the ethylene rectifying tower;
and the third selective hydrogenation reactor is used for receiving the carbon three-component, reducing the contents of methylacetylene and propadiene in the carbon three-component and inputting the reduced contents into the propylene rectifying tower.
In another aspect, there is provided a separation method for catalytic cracking of olefins, applied to the separation device, the method including:
carrying out catalytic cracking reaction on the catalytic cracking byproducts through the olefin catalytic cracker to obtain reaction products, and inputting the reaction products into the separation unit;
receiving, by the separation unit, the reaction product, separating a first carbon component from a carbon four carbon five component in the reaction product, and inputting the first carbon component to the depropanization unit;
receiving the first carbon component through the depropanizing unit, removing four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component into the depropanizing unit;
receiving the second carbon component through the impurity removal unit, removing inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the ethane removal unit;
receiving the third carbon component through the deethanizing unit, separating a carbon two component and a carbon three component in the third carbon component, and respectively inputting the carbon two component and the carbon three component into the rectifying unit;
and receiving the carbon two-component and the carbon three-component through the rectification unit, and rectifying the carbon two-component and the carbon three-component respectively to obtain polymer-grade ethylene and polymer-grade propylene.
The technical scheme provided by the embodiment of the application has the beneficial effects that at least:
the embodiment of the application provides a separation device for olefin catalytic cracking, the device enables catalytic cracking byproducts to obtain reaction products through an olefin catalytic cracker through a separation unit, a depropanization unit, an impurity removal unit, an ethane removal unit and a rectification unit which are connected in sequence, and can remove carbon four-carbon five-component, carbon four-component and inert impurities in the reaction products sequentially through the separation unit, the depropanization unit, the impurity removal unit and the ethane removal unit to obtain carbon two-component and carbon three-component, and the carbon two-component and the carbon three-component can be rectified through the rectification unit to obtain polymer grade ethylene and polymer grade propylene. Therefore, the polymer-grade ethylene and the polymer-grade propylene obtained by the device have high purity, good quality and high utilization rate, and further can improve the utilization rate of catalytic cracking byproducts.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a block diagram of a separation apparatus for catalytic cracking of olefins according to an embodiment of the present disclosure;
FIG. 2 is a block diagram of a separation apparatus for catalytic cracking of olefins according to an embodiment of the present disclosure;
FIG. 3 is a flow chart of a separation method for catalytic cracking of olefins according to an embodiment of the present application.
The reference numerals in the figures denote:
a 10-olefin catalytic cracker;
20-a separation unit;
201-a heat exchanger;
202-a first air compressor;
203-a separation column;
a 30-depropanization unit;
301-a second air compressor;
302-depropanizer;
40-impurity removal unit;
401-a dehydration column;
402-a degasser column;
a 50-deethanization unit;
501-a deethanizer;
60-a rectification unit;
601-an ethylene rectification column;
602-a propylene rectification column;
70-a first selective hydrogenation reactor;
80-a second selective hydrogenation reactor;
90-third selective hydrogenation reactor.
Detailed Description
To make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below with reference to the accompanying drawings.
The terms "first," "second," "third," and "fourth," etc. in the description and claims of this application and in the accompanying drawings are used for distinguishing between different objects and not for describing a particular order. Furthermore, the terms "include" and "have," as well as any variations thereof, are intended to cover a non-exclusive inclusion. For example, a process, method, system, article, or apparatus that comprises a list of steps or elements is not limited to only those steps or elements listed, but may alternatively include other steps or elements not listed, or inherent to such process, method, article, or apparatus.
The embodiment of this application provides a separator of olefin catalytic cracking, and referring to fig. 1, the device includes: the system comprises an olefin catalytic cracker 10, a separation unit 20, a depropanization unit 30, an impurity removal unit 40, an deethanization unit 50 and a rectification unit 60.
One side of the olefin catalytic cracker 10 is provided with a feed inlet for the input of catalytic cracking byproducts.
The discharge hole of the olefin catalytic cracker 10 is communicated with the feed hole of the separation unit 20, the discharge hole of the separation unit 20 is communicated with the feed hole of the depropanization unit 30, the discharge hole of the depropanization unit 30 is communicated with the feed hole of the impurity removal unit 40, the discharge hole of the impurity removal unit 40 is communicated with the feed hole of the deethanization unit 50, and the discharge hole of the deethanization unit 50 is communicated with the feed hole of the rectification unit 60.
The olefin catalytic cracker 10 is used for performing a catalytic cracking reaction on the catalytic cracking byproducts to obtain a reaction product, and inputting the reaction product into the separation unit 20.
The separation unit 20 is configured to receive the reaction product, separate a first carbon component from a four-carbon five-carbon component in the reaction product, and input the first carbon component to the depropanization unit 30.
And a depropanizing unit 30 for receiving the first carbon component, depropanizing the four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component to the impurity removing unit 40.
And the impurity removal unit 40 is used for receiving the second carbon component, removing the inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the ethane removal unit 50.
And the deethanizing unit 50 is used for receiving the third carbon component, separating the carbon two component and the carbon three component in the third carbon component, and respectively inputting the carbon two component and the carbon three component into the rectifying unit 60.
And the rectifying unit 60 is used for receiving the carbon two component and the carbon three component, and rectifying the carbon two component and the carbon three component respectively to obtain polymer-grade ethylene and polymer-grade propylene.
The embodiment of the application provides a separation device for catalytic cracking of olefin, and the device comprises a separation unit 20, a depropanization unit 30, an impurity removal unit 40, an deethanization unit 50 and a rectification unit 60 which are sequentially connected, so that after a catalytic cracking byproduct obtains a reaction product through an olefin catalytic cracker 10, the catalytic cracking byproduct can sequentially pass through the separation unit 20, the depropanization unit 30, the impurity removal unit 40 and the deethanization unit 50 to sequentially remove a carbon four-carbon five component, a carbon four component and an inert impurity in the reaction product, so as to obtain a carbon two component and a carbon three component, and the carbon two component and the carbon three component can be rectified through the rectification unit 60, so that polymerization-grade ethylene and polymerization-grade propylene are obtained. Therefore, the polymer-grade ethylene and the polymer-grade propylene obtained by the device have high purity, good quality and high utilization rate, and further can improve the utilization rate of catalytic cracking byproducts.
Referring to fig. 2, the apparatus further comprises a first selective hydrogenation reactor 70, and the separation unit 10 and the depropanization unit 30 are respectively communicated with the olefin catalytic cracker 10 through the first selective hydrogenation reactor 70.
The first selective hydrogenation reactor 70 is configured to receive the four-carbon five-component carbon separated by the separation unit 10 and the four-component carbon separated by the depropanizing unit 30, reduce the content of diolefins in the four-carbon five-component carbon and the four-component carbon, and input the reduced diolefins into the olefin catalytic cracker 10 for recycling.
Wherein, the four carbon five components and the four carbon components are input into the olefin catalytic cracker 10 for recycle, thereby effectively improving the utilization rate of the four carbon five components and the four carbon components.
In the embodiment of the present application, the content of the diolefin in the four-carbon five-component and the content of the diolefin in the four-carbon component can be effectively reduced through the first selective hydrogenation reactor 70, and then the catalytic efficiency of the catalyst can be improved.
With continued reference to fig. 1, a feed inlet is provided at one side of the olefin catalytic cracker 10 for inputting catalytic cracking byproducts, and a discharge outlet of the olefin catalytic cracker 10 is communicated with a feed inlet of the separation unit 20. The olefin catalytic cracker 10 is used for carrying out catalytic cracking reaction on the catalytic cracking byproducts to obtain reaction products, and the reaction products are input into the separation unit 20.
Wherein, the catalytic cracking by-products comprise olefin fractions with four to eight carbons, namely C4-C8 olefin fractions, and the C4-C8 olefin fractions are subjected to catalytic cracking reaction in a gas phase state at a high temperature under the catalytic action of a catalyst in an olefin catalytic cracker 10 to obtain reaction products.
The reaction product includes a plurality of impurities such as sulfur, chlorine, ammonia, arsenic, mercury, and the like, and the impurities can be removed by selecting a proper way according to the actual analysis and test result of the reaction product and the quality requirements of the polymerization-grade ethylene and the polymerization-grade propylene products, and the removal way is not limited in the embodiment of the application.
With continued reference to fig. 1, the feed inlet and the discharge outlet of the separation unit 20 are respectively communicated with the discharge outlet of the olefin catalytic cracker 10 and the feed inlet of the depropanization unit 30. A separation unit 20 for receiving the reaction product, separating a first carbon component from a carbon four-carbon five component in the reaction product, and inputting the first carbon component to a depropanization unit 30.
Referring to fig. 2, the separation unit 20 includes a heat exchanger 201, a first air press 202, and a separation column 203. The feed inlet and the discharge outlet of the heat exchanger 201 are respectively communicated with the discharge outlet of the olefin catalytic cracker 10 and the feed inlet of the first air compressor 202, the discharge outlet of the first air compressor 202 is communicated with the feed inlet of the separation tower 203, and the discharge outlet of the separation tower 203 is communicated with the depropanization unit 30.
The heat exchanger 201 is used for receiving the reaction product, cooling the reaction product to 35-45 ℃, and inputting the reaction product into the first air compressor 202. For example, the temperature of the reaction product can be 35 ℃, 36 ℃, 37 ℃, 38 ℃, 39 ℃, 40 ℃, 41 ℃, 42 ℃, 43 ℃, 44 ℃, 45 ℃ and so on.
And the first air compressor 202 is used for receiving the reaction product after temperature reduction, boosting the pressure of the reaction product to 0.2-0.5Mpa, and inputting the reaction product into the separation tower 203. For example, the pressure of the reaction product may be 0.2MPa, 0.3MPa, 0.4MPa, 0.5MPa or the like.
The separation tower 203 is configured to receive the reaction product after temperature reduction and pressure increase, separate a first carbon component from a carbon four-carbon five-component in the reaction product, and input the first carbon component to the depropanization unit 30.
Among them, the separation column 203 is a light-heavy separation column 203.
Wherein the reaction product also comprises carbon six components and heavier components separated by the separation tower 203. The bottom of the separation tower 203 is provided with a booster pump, and the carbon six components and heavier components are boosted by the booster pump and then output from the bottom of the separation tower 203 to be recycled as gasoline blending components.
Wherein the first carbon component is output from the top of the separation column 203 and is input to the depropanization unit 30. The first carbon component comprises a carbon third component, a carbon second component, inert impurities and an incompletely separated carbon fourth component, and the content of the carbon fourth component is 0-5%.
Wherein, the carbon four-carbon five-component is output from the middle part of the separation tower 203; the carbon four-carbon five component comprises a carbon four component and a carbon five component, and the carbon four component and the carbon five component comprise monoolefine and dialkene.
Wherein the carbon two component comprises hydrocarbons with two carbon numbers; such as ethylene and ethane, and the like. By analogy, the carbon three component comprises hydrocarbons with three carbon numbers, the carbon four component comprises hydrocarbons with four carbon numbers, the carbon five component comprises hydrocarbons with five carbon numbers, the carbon six component comprises hydrocarbons with six carbon numbers, and the heavier component comprises hydrocarbons with more than six carbon numbers.
With continued reference to fig. 2, the separation column 203 is in communication with the olefin catalytic cracker 10 via the first selective hydrogenation reactor 70. And the first selective hydrogenation reactor 70 is used for receiving the four-carbon five-component separated by the separation tower 203, reducing the content of the diene in the four-carbon five-component, and inputting the reduced diene into the olefin catalytic cracker 10 for recycling.
Wherein, the carbon four-carbon five-component is separated from the middle part of the separation tower 203 in a gas phase state, thereby avoiding the need of heating and vaporizing the carbon four-carbon five-component when inputting into the olefin catalytic cracker 10.
In another possible implementation manner, if the content of the diolefin in the four-carbon five-component is low, the separation tower 203 is directly communicated with the olefin catalytic cracker 10, and the four-carbon five-component is input into the olefin catalytic cracker 10 for recycling.
In the embodiment of the application, the carbon four-carbon five-component in the reaction product is separated by the separation tower 203 and input into the olefin catalytic cracker 10 for remixing, so that the utilization rate of the carbon four-carbon five-component is effectively improved.
With continued reference to fig. 1, the inlet and outlet of the depropanizing unit 30 are in communication with the outlet of the separation unit 20 and the inlet of the impurity removal unit 40, respectively. And a depropanizing unit 30 for receiving the first carbon component, depropanizing the four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component to the impurity removing unit 40.
With continued reference to fig. 2, the depropanization unit 30 comprises a second gas compressor 301 and a depropanizer 302. The feed inlet and the discharge outlet of the second pneumatic press 301 are respectively communicated with the discharge outlet of the separation unit 20 and the feed inlet of the depropanizer 302, and the discharge outlet of the depropanizer 302 is communicated with the feed inlet of the impurity removal unit 40.
Wherein, the feed inlet of the second pneumatic press 301 is communicated with the discharge outlet of the separation tower 203.
And the second pneumatic press 301 is used for receiving the first carbon component, boosting the pressure of the first carbon component to 1.8-4.0Mpa, and inputting the first carbon component into the depropanizer 302. For example, the pressure of the first carbon component may be 1.8MPa, 2.0MPa, 2.2MPa, 2.5MPa, 2.7MPa, 3.0MPa, 3.3MPa, 3.5MPa, 3.7MPa, 3.9MPa, 4.0MPa, or the like.
The depropanizer 302 is configured to receive the first carbon component after pressure boosting, depropanize the four carbon components in the first carbon component to obtain a second carbon component, and input the second carbon component to the impurity removal unit 40.
Wherein the second carbon component is output from the top of the depropanizer 302 and input to the depropanizer unit 40. The second carbon component comprises a carbon three component, a carbon two component and inert impurities.
Wherein, the carbon four components are removed from the bottom of the depropanizer 302, and the carbon four components comprise monoolefin and diolefin. One part of the four carbon components is taken as a product and sent out of the device, and the other part is input into an olefin catalytic cracker 10 for recycling.
In the embodiment of the application, the four carbon components in the second carbon component are separated by the depropanizer 302 and input into the olefin catalytic cracker 10 for reprocessing, so that the utilization rate of the four carbon components is effectively improved.
With continued reference to fig. 2, the depropanizer 302 is in communication with the olefin catalytic cracker 10 via the first selective hydrogenation reactor 70. The first selective hydrogenation reactor 70 is configured to receive the four carbon components removed from the depropanizer 302, reduce the content of diolefins in the four carbon components, and input the reduced four carbon components to the olefin catalytic cracker 10 for recycling.
In another possible implementation, if the content of diolefin in the carbon four components is low, the depropanizer 302 is directly communicated with the olefin catalytic cracker 10, and the carbon four components are input into the olefin catalytic cracker 10 for recycling.
With continued reference to fig. 1, the feed and discharge ports of the impurity removal unit 40 communicate with the discharge port of the depropanizing unit 30 and the feed port of the deethanizing unit 50, respectively. And the impurity removal unit 40 is used for receiving the second carbon component, removing the inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the ethane removal unit 50.
With continued reference to fig. 2, the de-impurity unit 40 includes a dehydration column 401 and a degasser column 402. The feed inlet and the discharge outlet of the dehydration tower 401 are respectively communicated with the discharge outlet of the depropanization unit 30 and the feed inlet of the degassing tower 402, and the discharge outlet of the degassing tower 402 is communicated with the feed inlet of the deethanization unit 50.
Wherein, the feed inlet of the dehydrating tower 401 is communicated with the discharge outlet of the depropanizing tower 302. The degasser 402 can be a light ends removal column.
And a dehydrating tower 401 for receiving the second carbon component, dehydrating the second carbon component, and inputting the dehydrated second carbon component into a degassing tower 402. A degassing tower 402 for receiving the dehydrated second carbon component, degassing the inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component to the deethanizing unit 50.
The inert impurities comprise methane, hydrogen, nitrogen and the like, and the state of the inert impurities comprises a gas state and a liquid state. The inert impurities are removed from the top of the degasser 402 and sent to a fuel gas pipe network as dry gas for recycling.
Wherein the third carbon component comprises a carbon two component and a carbon three component, and the carbon two component and the carbon three component are extracted from the bottom of the degassing tower 402.
Wherein, the lower part of the degassing tower 402 is provided with a reboiler. And the reboiler is used for heating the inert impurities to vaporize the inert impurities in the second component into inert gas and remove the inert gases.
In the embodiment of the application, the inert impurities are vaporized into the inert gas by arranging the reboiler, so that the inert impurities can be conveniently output from the top of the degassing tower 402, the methane content in the third carbon component at the bottom of the degassing tower 402 is reduced, and the mole fraction of the methane in the third carbon component is ensured to be lower than 1 percent so as to ensure the purity of the third carbon component.
Wherein an intermediate circulation cooler is provided at the upper part of the degassing tower 402. And an intermediate circulation cooler for cooling the absorbent in the degassing tower 402, so that the cooled absorbent absorbs the carbon two components in the second carbon component to obtain a third carbon component.
Wherein the intermediate circulation cooler is disposed at an upper portion of the outside of the degassing tower 402, and the absorbent and the second carbon component are mixed, withdrawn from the top of the degassing tower 402, cooled by the intermediate circulation cooler, and returned to the degassing tower 402 to absorb the carbon dioxide component of the second carbon component at a low temperature.
Wherein, the absorbent is three components of carbon, and the temperature that the absorbent gets into in degasser 402 is higher than-40 ℃, in this application embodiment, through setting up the intercooler, can reduce the temperature of absorbent, and then can improve the absorption efficiency of absorbent to the two carbon components.
With continued reference to fig. 1, the feed and discharge of deethanizer unit 50 are in communication with the discharge of impurity removal unit 40 and the feed of rectification unit 60, respectively. And the deethanizing unit 50 is used for receiving the third carbon component, separating the carbon two component and the carbon three component in the third carbon component, and respectively inputting the carbon two component and the carbon three component into the rectifying unit 60.
With continued reference to fig. 2, deethanizer unit 50 includes deethanizer 501, with the feed and discharge of deethanizer 501 communicating with the discharge of degasser 402 and the feed of rectification unit 60, respectively. The deethanizer 501 is configured to receive a third carbon component, separate a carbon three component from the carbon two component in the third carbon component, and input the carbon two component and the carbon three component to the rectification unit 60, respectively.
With continued reference to fig. 1, the feed inlet of the rectification unit 60 is in communication with the discharge outlet of the deethanizer unit 50. And the rectification unit 60 is used for receiving the carbon two component and the carbon three component and respectively rectifying the carbon two component and the carbon three component to obtain polymer grade ethylene and polymer grade propylene.
With continued reference to fig. 2, the rectification unit 60 includes an ethylene rectification column 601 and a propylene rectification column 602. The discharge ports of the deethanization unit 50 comprise a first discharge port and a second discharge port, the feed port of the ethylene rectifying tower 601 is communicated with the first discharge port of the deethanization unit 50, and the feed port of the propylene rectifying tower 602 is communicated with the second discharge port of the deethanization unit 50.
Wherein, the second discharge gate of first discharge gate is located the top of the tower and the bottom of the tower of deethanizer 501 respectively, and the first discharge gate at the top of the tower is used for importing the carbon two-component into ethylene rectifying column 601, and the second discharge gate at the bottom of the tower is used for importing the carbon three-component into propylene rectifying column 602.
The ethylene rectifying tower 601 is used for receiving the carbon two components and rectifying the carbon two components to obtain polymer-grade ethylene.
Wherein, after the carbon dioxide component is rectified, ethane and polymer-grade ethylene are obtained, and the ethane and the polymer-grade ethylene are respectively output from a tower bottom discharge port and a tower top discharge port of the ethylene rectifying tower 601.
And the propylene rectifying tower 602 is used for receiving the carbon three components and rectifying the carbon three components to obtain polymer-grade propylene.
After the three carbon components are rectified, propane and polymer-grade propylene are obtained, and the propane and the polymer-grade propylene are respectively output from a tower bottom discharge port and a tower top discharge port of the propylene rectifying tower 602.
With continued reference to fig. 2, the apparatus further comprises a second selective hydrogenation reactor 80 and a third selective hydrogenation reactor 90, the ethylene rectification column 601 and the propylene rectification column 602 being in communication with the deethanizer unit 50 through the second selective hydrogenation reactor 80 and the third selective hydrogenation reactor 90, respectively.
The second selective hydrogenation reactor 80 is used for receiving the carbon two components, reducing the acetylene content in the carbon two components and inputting the reduced acetylene content into the ethylene rectifying tower 601; and the third selective hydrogenation reactor 90 is configured to receive the carbon three components, reduce the contents of methylacetylene and propadiene in the carbon three components, and input the reduced contents into the propylene rectification tower 602.
Wherein the ethylene rectifying tower 601 is communicated with the deethanizer 501 through the second selective hydrogenation reactor 80. The propylene rectification column 602 is in communication with the deethanizer 501 via the third selective hydrogenation reactor 90.
In another possible implementation, the ethylene rectification column 601 is in direct communication with the deethanizer 501 if the acetylene content in the carbon dioxide component is low.
In another possible implementation, if the content of methylacetylene and propadiene in the carbon tri-component is low, the propylene rectification column 602 is directly communicated with the deethanizer 501.
The yield of the polymer-grade ethylene and the polymer-grade propylene obtained by the device provided by the embodiment of the application is more than 98%, and the high-efficiency separation of olefin catalytic cracking byproducts is realized.
Wherein, a discharge port at the bottom of the propylene rectifying tower 602 is communicated with a feed port of the degassing tower 402, and is used for inputting a part of propane as an absorbent into the degassing tower 402 for recycling.
The embodiment of the application provides a separation device for olefin catalytic cracking, the device enables catalytic cracking byproducts to obtain reaction products through an olefin catalytic cracker 10 through a separation unit 20, a depropanization unit 30, an impurity removal unit 40, an ethane removal unit 50 and a rectification unit 60 which are connected in sequence, and then sequentially removes carbon four-carbon five components, carbon four components and inert impurities in the reaction products through the separation unit 20, the depropanization unit 30, the impurity removal unit 40 and the ethane removal unit 50 to obtain carbon two components and carbon three components, and can carry out rectification treatment on the carbon two components and the carbon three components through the rectification unit 60 to obtain polymer grade ethylene and polymer grade propylene. Therefore, the polymer-grade ethylene and the polymer-grade propylene obtained by the device have high purity, good quality and high utilization rate, and further can improve the utilization rate of catalytic cracking byproducts.
The embodiment of the application provides a separation method for catalytic cracking of olefin, and referring to fig. 3, the method comprises the following steps:
step 301: the catalytic cracking reaction is performed on the catalytic cracking byproducts by the olefin catalytic cracker 10 to obtain reaction products, and the reaction products are input into the separation unit 20.
The reaction product includes a plurality of components, and for example, in a separation experiment of a certain reaction product, the reaction product includes a plurality of components such as hydrogen, nitrogen, methane, and the like, see table 1, where table 1 includes mass fractions and mass flow rates of the components of the reaction product.
TABLE 1
| Components | Mass fraction% | Mass flow rate kg/h |
| Hydrogen gas | 0.349 | 82.633 |
| Nitrogen gas | 0.162 | 38.271 |
| Methane | 1.299 | 307.76 |
| Ethylene | 15.049 | 3564.8 |
| Ethane (III) | 1.617 | 383.12 |
| Acetylene | 0.002 | 0.3635 |
| Propylene polymer | 81.083 | 19207 |
| Propane | 0.216 | 51.191 |
| Methylacetylene | 0.011 | 2.527 |
| Allene | 0.003 | 0.6493 |
| Cyclopropane | 0.031 | 7.432 |
| Isobutane | 0.002 | 0.5652 |
| Isobutene | 0.076 | 18.082 |
| 1-butene | 0.031 | 7.3944 |
| 1, 3-butadiene | 0.004 | 0.9514 |
| N-butane | 0.022 | 5.1237 |
| Cis-2-butene | 0.007 | 1.6443 |
| Trans-2-butene | 0.003 | 0.6025 |
| C five + C | 0.033 | 7.8897 |
| Is totaled | 100.00 | 23688 |
Step 302: the reaction product is received by separation unit 20, the first carbon component of the reaction product is separated from the four-carbon five-carbon component, and the first carbon component is input to depropanization unit 30.
Wherein, the reaction product is received by a heat exchanger 201, cooled to 35-45 ℃ and then input into a first air compressor 202. The cooled reaction product is received by the first air compressor 202, and the pressure of the reaction product is raised to 0.2-0.5Mpa, and then the reaction product is input into the separation tower 203.
Continuing with the example of the separation experiment of the reaction product, the reaction product is received by the heat exchanger 201, cooled to 35-45 ℃, and then input into the first air compressor 202. The cooled reaction product is received by the first air compressor 202, and the pressure of the reaction product is raised to 0.45Mpa, and then the reaction product is fed into the separation tower 203.
The cooled and pressurized reaction product is received by the separation tower 203, the first carbon component and the carbon four-carbon five-component in the reaction product are separated, and the first carbon component is input to the depropanization unit 30.
The four-carbon five-component separated by the separation tower 203 is received by the first selective hydrogenation reactor 204, and the diolefin content in the four-carbon five-component is reduced and then the reduced diolefin content is input into the olefin catalytic cracker 10 for recycling.
The carbon six-component and heavier components are output from the bottom of the separation tower 203 through a booster pump in the separation tower 203 and are recycled as gasoline blending components.
Step 303: the first carbon component is received by the depropanizing unit 30, the four carbon components in the first carbon component are depropanized to obtain a second carbon component, and the second carbon component is inputted to the depropanizing unit 40.
Wherein, the first carbon component is received by the second pneumatic press 301, and the first carbon component is input into the depropanizer 302 after being pressurized to 2.0Mpa-4.0 Mpa.
Taking the separation experiment of a certain reaction product as an example, the first carbon component is received by the second gas compressor 301, and the first carbon component is pressurized to 2.6Mpa and then is input into the depropanizer 302.
The first carbon component after the pressure increase is received by the depropanizer 302, the four carbon components in the first carbon component are removed to obtain the second carbon component, and the second carbon component is input to the impurity removing unit 40.
The carbon four components removed from the depropanizer 302 are received by the second selective hydrogenation reactor 303, and the diolefins content in the carbon four components is reduced and then input into the olefin catalytic cracker 10 for recycling.
Step 304: the second carbon fraction is received by the impurity removal unit 40, inert impurities in the second carbon fraction are removed to obtain a third carbon fraction, and the third carbon fraction is input to the deethanizer unit 50.
Wherein the second carbon component is received by the dehydrating tower 401, dehydrated and then input to the degassing tower 402.
The dehydrated second carbon component is received by the degasser 402, the inert impurities in the second carbon component are removed to yield a third carbon component, and the third carbon component is input to the deethanizer unit 50.
Wherein, the inert impurities are heated by a reboiler, so that the inert impurities in the second component are vaporized into inert gas and then removed, and the inert impurities are used as dry gas and conveyed to a fuel gas pipe network for recycling, and meanwhile, the mole fraction of methane in the third carbon component is ensured to be lower than 1%.
Wherein the absorbent in the degassing tower 402 is cooled to-40 ℃ by an intermediate circulation cooler, so that the cooled absorbent absorbs the carbon two component in the second carbon component to obtain a third carbon component.
Step 305: the third carbon component is received through the deethanizing unit 50, the carbon two component and the carbon three component in the third carbon component are separated, and the carbon two component and the carbon three component are respectively input to the rectifying unit 60.
Wherein the third carbon component is received by the deethanizer 501, the carbon two component and the carbon three component in the third carbon component are separated, and the carbon two component and the carbon three component are respectively input to the rectification unit 60.
Step 306: the rectification unit 60 receives the carbon two component and the carbon three component, and the carbon two component and the carbon three component are respectively rectified to obtain polymer grade ethylene and polymer grade propylene.
Wherein, the ethylene rectifying tower 601 receives the carbon two components, and rectifies the carbon two components to obtain the polymer-grade ethylene. The propylene rectifying tower 602 receives the carbon three components, and the carbon three components are rectified to obtain polymer-grade propylene.
Taking the separation experiment of a certain reaction product as an example, the mass flow of the obtained polymerization-grade ethylene is 3500kg/h, and the molar concentration is 99.9%; the mass flow rate of the obtained polymerization grade propylene is 18850kg/h, and the molar concentration is 99.9%.
Wherein, a part of propane obtained from the bottom of the propylene rectifying tower 602 is output as a product, and a part of propane is input into the degassing tower 402 as an absorbent for recycling.
The embodiment of the application provides a separation method for olefin catalytic cracking, and the method comprises the steps of arranging a separation unit 20, a depropanization unit 30, an impurity removal unit 40, an ethane removal unit 50 and a rectification unit 60 which are sequentially connected, so that after a catalytic cracking byproduct obtains a reaction product through an olefin catalytic cracker 10, sequentially removing a carbon four-carbon five component, a carbon four component and an inert impurity in the reaction product through the separation unit 20, the depropanization unit 30, the impurity removal unit 40 and the ethane removal unit 50 to obtain a carbon two component and a carbon three component, and rectifying the carbon two component and the carbon three component through the rectification unit 60 to obtain polymer grade ethylene and polymer grade propylene. Thus, the polymer-grade ethylene and the polymer-grade propylene obtained by the method have high purity, good quality and high utilization rate, and further the utilization rate of catalytic cracking byproducts can be improved.
The above description is intended only to illustrate the alternative embodiments of the present application, and should not be construed as limiting the present application, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. A separation device for catalytic cracking of olefins, the device comprising: the device comprises an olefin catalytic cracker (10), a separation unit (20), a depropanization unit (30), an impurity removal unit (40), an ethane removal unit (50) and a rectification unit (60);
a feed inlet is formed in one side of the olefin catalytic cracker (10) and is used for inputting catalytic cracking byproducts;
the discharge hole of the olefin catalytic cracker (10) is communicated with the feed hole of the separation unit (20), the discharge hole of the separation unit (20) is communicated with the feed hole of the propane removal unit (30), the discharge hole of the propane removal unit (30) is communicated with the feed hole of the impurity removal unit (40), the discharge hole of the impurity removal unit (40) is communicated with the feed hole of the ethane removal unit (50), and the discharge hole of the ethane removal unit (50) is communicated with the feed hole of the rectification unit (60);
the olefin catalytic cracker (10) is used for carrying out catalytic cracking reaction on the catalytic cracking byproducts to obtain reaction products, and the reaction products are input into the separation unit (20);
the separation unit (20) is used for receiving the reaction product, separating a first carbon component from a carbon four-carbon five-component in the reaction product, and inputting the first carbon component into the depropanization unit (30);
the depropanization unit (30) is used for receiving the first carbon component, removing four carbon components in the first carbon component to obtain a second carbon component, and inputting the second carbon component into the impurity removal unit (40);
the impurity removal unit (40) is used for receiving the second carbon component, removing inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the deethanizing unit (50);
the deethanization unit (50) is used for receiving the third carbon component, separating a carbon two component and a carbon three component in the third carbon component, and respectively inputting the carbon two component and the carbon three component into the rectification unit (60);
the rectifying unit (60) is used for receiving the carbon two-component and the carbon three-component and rectifying the carbon two-component and the carbon three-component respectively to obtain polymer grade ethylene and polymer grade propylene.
2. The separation unit for the catalytic cracking of olefins according to claim 1, characterized in that the separation unit (20) comprises a heat exchanger (201), a first air compressor (202) and a separation column (203);
the feed inlet and the discharge outlet of the heat exchanger (201) are respectively communicated with the discharge outlet of the olefin catalytic cracker (10) and the feed inlet of the first air compressor (202), the discharge outlet of the first air compressor (202) is communicated with the feed inlet of the separation tower (203), and the discharge outlet of the separation tower (203) is communicated with the propane removal unit (30);
the heat exchanger (201) is used for receiving the reaction product, cooling the reaction product to 35-45 ℃ and then inputting the cooled reaction product into the first air compressor (202);
the first air compressor (202) is used for receiving the reaction product after temperature reduction, boosting the pressure of the reaction product to 0.2-0.5Mpa, and inputting the reaction product into the separation tower (203);
the separation tower (203) is used for receiving the reaction products after cooling and pressure increasing, separating a first carbon component from a carbon four-carbon five-component in the reaction products, and inputting the first carbon component into the depropanization unit (30).
3. The separation unit for catalytic cracking of olefins according to claim 1, characterized in that the depropanizing unit (30) comprises a second gas compressor (301) and a depropanizer (302);
a feeding hole and a discharging hole of the second air compressor (301) are respectively communicated with a discharging hole of the separation unit (20) and a feeding hole of the depropanizing tower (302), and a discharging hole of the depropanizing tower (302) is communicated with a feeding hole of the impurity removing unit (40);
the second gas compressor (301) is used for receiving the first carbon component, boosting the pressure of the first carbon component to 1.8-4.0Mpa, and inputting the first carbon component into the depropanizer (302);
the depropanizer (302) is configured to receive the first carbon component after pressure boosting, remove four carbon components in the first carbon component to obtain a second carbon component, and input the second carbon component to the impurity removal unit (40).
4. The separation device for catalytic cracking of olefins according to claim 1, characterized in that the device further comprises a first selective hydrogenation reactor (70), and the separation unit (10) and the depropanization unit (30) are respectively communicated with the catalytic cracking unit (10) of olefins through the first selective hydrogenation reactor (70);
the first selective hydrogenation reactor (70) is used for receiving the carbon four-carbon five component separated by the separation unit (10) and the carbon four component separated by the depropanizing unit (30), reducing the content of diene in the carbon four-carbon five component and the carbon four component, and inputting the reduced content of diene into the olefin catalytic cracker (10) for recycling.
5. The separation apparatus for catalytic cracking of olefins according to claim 1, wherein the impurity removal unit (40) comprises a dehydration column (401) and a degassing column (402);
the feed inlet and the discharge outlet of the dehydrating tower (401) are respectively communicated with the discharge outlet of the depropanizing unit (30) and the feed inlet of the degassing tower (402), and the discharge outlet of the degassing tower (402) is communicated with the feed inlet of the deethanizing unit (50);
the dehydration tower (401) is used for receiving the second carbon component, dehydrating the second carbon component and inputting the second carbon component into the degassing tower (402);
the degassing tower (402) is used for receiving the dehydrated second carbon component, removing inert impurities in the second carbon component to obtain a third carbon component, and inputting the third carbon component into the deethanizing unit (50).
6. The apparatus for separating olefin catalytic cracking according to claim 5, wherein the degasser (402) is provided with a reboiler at the lower part;
and the reboiler is used for heating the inert impurities to vaporize the inert impurities in the second component into inert gas and remove the inert gases.
7. The apparatus for the catalytic cracking of olefins according to claim 5, wherein an intermediate circulation cooler is provided at the upper part of the degassing tower (402);
the intermediate circulation cooler is used for cooling the absorbent in the degassing tower (402) so that the cooled absorbent absorbs the carbon two components in the second carbon component to obtain the third carbon component.
8. The separation unit for catalytic cracking of olefins according to claim 1, characterized in that the rectification unit (60) comprises an ethylene rectification column (601) and a propylene rectification column (602);
the discharge holes of the deethanization unit (50) comprise a first discharge hole and a second discharge hole, the feed hole of the ethylene rectifying tower (601) is communicated with the first discharge hole of the deethanization unit (50), and the feed hole of the propylene rectifying tower (602) is communicated with the second discharge hole of the deethanization unit (50);
the ethylene rectifying tower (601) is used for receiving the carbon two components and rectifying the carbon two components to obtain polymerization-grade ethylene;
and the propylene rectifying tower (602) is used for receiving the carbon three-component and rectifying the carbon three-component to obtain polymer-grade propylene.
9. The separation device for catalytic cracking of olefins according to claim 8, characterized in that it further comprises a second selective hydrogenation reactor (80) and a third selective hydrogenation reactor (90), said ethylene rectification column (601) and said propylene rectification column (602) being in communication with said deethanizing unit (50) through said second selective hydrogenation reactor (80) and said third selective hydrogenation reactor (90), respectively;
the second selective hydrogenation reactor (80) is used for receiving the carbon two components, reducing the acetylene content in the carbon two components and inputting the reduced acetylene content into the ethylene rectifying tower (601);
the third selective hydrogenation reactor (90) is used for receiving the carbon three components, reducing the contents of methylacetylene and propadiene in the carbon three components and inputting the reduced contents into the propylene rectifying tower (602).
10. A separation method for catalytic cracking of olefins, characterized in that it is applied to a separation device according to any one of claims 1 to 9, characterized in that it comprises:
carrying out catalytic cracking reaction on the catalytic cracking byproducts through the olefin catalytic cracker (10) to obtain reaction products, and inputting the reaction products into the separation unit (20);
receiving, by the separation unit (20), the reaction product, separating a first carbon component from a carbon four carbon five component in the reaction product, and inputting the first carbon component to the depropanization unit (30);
receiving, by the depropanization unit (30), the first carbon component, depropanizing the four carbon components of the first carbon component to obtain a second carbon component, and feeding the second carbon component to the depropanization unit (40);
receiving, by the de-impurity unit (40), the second carbon component, de-extracting inert impurities from the second carbon component to obtain a third carbon component, and inputting the third carbon component to the de-ethane unit (50);
receiving the third carbon component by the deethanizing unit (50), separating a carbon two component and a carbon three component in the third carbon component, and inputting the carbon two component and the carbon three component to the rectifying unit (60), respectively;
and receiving the carbon two component and the carbon three component through the rectifying unit (60), and rectifying the carbon two component and the carbon three component respectively to obtain polymer grade ethylene and polymer grade propylene.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050150817A1 (en) * | 2004-01-14 | 2005-07-14 | Kellogg Brown And Root, Inc. | Integrated catalytic cracking and steam pyrolysis process for olefins |
| US7763165B1 (en) * | 2006-12-21 | 2010-07-27 | Uop Llc | Fractionation recovery processing of FCC-produced light olefins |
| CN102070390A (en) * | 2011-01-12 | 2011-05-25 | 王伟跃 | Method for preparing propylene from refinery mixed C4 |
| CN102206128A (en) * | 2010-10-14 | 2011-10-05 | 东华工程科技股份有限公司 | Separation method for low-carbon olefin prepared from oxygen-containing compound |
| CN111320525A (en) * | 2020-03-02 | 2020-06-23 | 大连理工大学 | Non-low temperature separation process for ethylene-rich catalytic cracking gas |
| CN111320524A (en) * | 2018-12-14 | 2020-06-23 | 中国石油化工股份有限公司 | Method and device for separating ethylene and propylene from pyrolysis gas and/or dry gas |
| CN112694383A (en) * | 2019-10-22 | 2021-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking of olefin |
-
2021
- 2021-05-14 CN CN202110528868.9A patent/CN115340436A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050150817A1 (en) * | 2004-01-14 | 2005-07-14 | Kellogg Brown And Root, Inc. | Integrated catalytic cracking and steam pyrolysis process for olefins |
| US7763165B1 (en) * | 2006-12-21 | 2010-07-27 | Uop Llc | Fractionation recovery processing of FCC-produced light olefins |
| CN102206128A (en) * | 2010-10-14 | 2011-10-05 | 东华工程科技股份有限公司 | Separation method for low-carbon olefin prepared from oxygen-containing compound |
| CN102070390A (en) * | 2011-01-12 | 2011-05-25 | 王伟跃 | Method for preparing propylene from refinery mixed C4 |
| CN111320524A (en) * | 2018-12-14 | 2020-06-23 | 中国石油化工股份有限公司 | Method and device for separating ethylene and propylene from pyrolysis gas and/or dry gas |
| CN112694383A (en) * | 2019-10-22 | 2021-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking of olefin |
| CN111320525A (en) * | 2020-03-02 | 2020-06-23 | 大连理工大学 | Non-low temperature separation process for ethylene-rich catalytic cracking gas |
Non-Patent Citations (1)
| Title |
|---|
| 李立新等: "烯烃催化裂解制丙烯分离技术进展", 《化工进展》, vol. 28, no. 7, 31 December 2009 (2009-12-31), pages 1159 - 1164 * |
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