CN113651669A - Apparatus and process for producing propylene - Google Patents
Apparatus and process for producing propylene Download PDFInfo
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- CN113651669A CN113651669A CN202010394877.9A CN202010394877A CN113651669A CN 113651669 A CN113651669 A CN 113651669A CN 202010394877 A CN202010394877 A CN 202010394877A CN 113651669 A CN113651669 A CN 113651669A
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- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000010521 absorption reaction Methods 0.000 claims abstract description 79
- 150000001336 alkenes Chemical class 0.000 claims abstract description 67
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 53
- 238000003795 desorption Methods 0.000 claims abstract description 36
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 35
- 239000000463 material Substances 0.000 claims abstract description 33
- 239000012495 reaction gas Substances 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 32
- 238000006243 chemical reaction Methods 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 24
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 23
- 239000005977 Ethylene Substances 0.000 claims description 23
- 230000002745 absorbent Effects 0.000 claims description 20
- 239000002250 absorbent Substances 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 18
- 239000000047 product Substances 0.000 claims description 16
- 239000007795 chemical reaction product Substances 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 13
- 238000005336 cracking Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000002826 coolant Substances 0.000 claims description 2
- 238000009776 industrial production Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 16
- 239000003054 catalyst Substances 0.000 description 9
- 239000006227 byproduct Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000003507 refrigerant Substances 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 229930195733 hydrocarbon Natural products 0.000 description 5
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical compound CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- -1 propylene, ethylene Chemical group 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- QMMOXUPEWRXHJS-HWKANZROSA-N (e)-pent-2-ene Chemical compound CC\C=C\C QMMOXUPEWRXHJS-HWKANZROSA-N 0.000 description 1
- QMMOXUPEWRXHJS-HYXAFXHYSA-N (z)-pent-2-ene Chemical compound CC\C=C/C QMMOXUPEWRXHJS-HYXAFXHYSA-N 0.000 description 1
- MHNNAWXXUZQSNM-UHFFFAOYSA-N 2-methylbut-1-ene Chemical compound CCC(C)=C MHNNAWXXUZQSNM-UHFFFAOYSA-N 0.000 description 1
- YHQXBTXEYZIYOV-UHFFFAOYSA-N 3-methylbut-1-ene Chemical compound CC(C)C=C YHQXBTXEYZIYOV-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- IAQRGUVFOMOMEM-ARJAWSKDSA-N cis-but-2-ene Chemical compound C\C=C/C IAQRGUVFOMOMEM-ARJAWSKDSA-N 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- SYSQUGFVNFXIIT-UHFFFAOYSA-N n-[4-(1,3-benzoxazol-2-yl)phenyl]-4-nitrobenzenesulfonamide Chemical class C1=CC([N+](=O)[O-])=CC=C1S(=O)(=O)NC1=CC=C(C=2OC3=CC=CC=C3N=2)C=C1 SYSQUGFVNFXIIT-UHFFFAOYSA-N 0.000 description 1
- QMMOXUPEWRXHJS-UHFFFAOYSA-N pentene-2 Natural products CCC=CC QMMOXUPEWRXHJS-UHFFFAOYSA-N 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
-
- 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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/26—Fuel gas
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to an apparatus and a process for producing propylene. The apparatus of the present invention comprises: the system comprises an olefin catalytic cracking reactor, a reaction gas compressor, an absorption tower, a desorption tower, a depropanization tower and a circulating material tower; a heating furnace is arranged on an inlet pipeline of the olefin catalytic cracking reactor, and an outlet pipeline is connected to a reaction gas compressor; the outlet pipeline of the reaction gas compressor comprises two branches, one branch is communicated with the bottom of the absorption tower, and the other branch is communicated with the top of the desorption tower; the bottom of the absorption tower is communicated with the top of the desorption tower, and the top of the absorption tower is communicated with the bottom of the circulating material tower; the bottom of the desorption tower is communicated with a depropanization tower; the bottom of the depropanization tower is communicated with a circulating material tower; the top of the circulating material tower is communicated with an olefin catalytic cracking reactor. The device and the method of the invention better solve the problems that the common engineering conditions of the olefin catalytic cracking process in the prior art are harsh and are difficult to apply in refineries, and can be used in the industrial production of low-carbon olefins.
Description
Technical Field
The invention relates to a device and a method for producing propylene, in particular to a device and a method for producing propylene by catalytic cracking olefin, which are particularly suitable for application of an olefin catalytic cracking process in refinery enterprises.
Technical Field
Ethylene plants, catalytic cracking plants and methanol-to-olefins plants produce a large amount of by-products of carbon-four-carbon-five hydrocarbons, of which more than 60% are olefins. The catalytic cracking production of low-carbon olefins such as ethylene and propylene by using the byproduct hydrocarbons as raw materials is an effective way for improving the device benefit. The olefin catalytic cracking technology consists of an olefin catalytic cracking reaction technology and a product separation technology. The core of the reaction technology is the development of a catalyst and a reactor, and the core of the separation technology is a separation process which is designed according to the distribution characteristics of the olefin cracking products and has reasonable flow and economic feasibility.
The olefin catalytic cracking technology which is industrially applied at home at present comprises OCC technology of China Shanghai petrochemical industry research institute of petrochemical industry and OCP technology of UOP company. The OCC technology of China Shanghai petrochemical research institute adopts an innovative full crystallization technology to prepare the ZSM-5 molecular sieve catalyst, so that the processing capacity of the catalyst is greatly improved, and the mass airspeed is as high as 15-30 hr-1. OCC technology converts the C-pentacene into ethylene and propylene with high selectivity, and only produces a small amount of residual C-pentacene and naphtha as by-products. Because the byproduct C4+ component of the methanol-to-olefin (MTO) device contains high-content C4 and C5 olefins and is very suitable for being used as a raw material for catalytic cracking of olefins, the current industrialized catalytic cracking device for olefins adopts the byproduct C4+ of MTO, and the maximization of the diene yield of MTO is realized.
The olefin catalytic cracking device integrated with MTO has the main characteristic that after the olefin catalytic cracking product is primarily separated, the mixture flow containing ethylene and propylene can be separated by depending on an olefin separation system of MTO, so that the investment cost and the operation cost of the device are greatly reduced, and in the primary separation of the olefin catalytic cracking product, a cooling medium of a rectifying tower, such as a propylene refrigerant, can also depend on the olefin separation system of MTO. The patent CN101092323B patent describes a typical flow of a carbon-containing olefin catalytic cracking device. In the process, a liquid phase raw material carbon-containing olefin mixture is gasified and preheated by heat exchange with a cracking product, and then is heated by a heating furnace to reach the reaction temperature; the cracked product is partially condensed after heat exchange of the raw material carbon-containing olefin mixture, and a part of fraction above C5 is separated; compressing the rest cracking products to 0.3-1.1 MPa, then separating in a depropanizing tower, and further separating fractions below C3 obtained from the tower top by an ethylene device to obtain propylene and ethylene; and (3) feeding the fraction above C4 at the bottom of the tower into a debutanizer, and recycling 30-90 wt% of the fraction C4 separated from the top of the tower into the reactor for cracking again. Because the pressure at the outlet of the compressor is low, the pressure at the top of the depropanizer is far lower than 40 ℃, the depropanizer cannot be cooled by circulating cooling water, and the fraction below C3 obtained at the top of the depropanizer needs to be separated by a separation system of an ethylene device.
Along with the wide popularization of ethanol gasoline in provinces and cities of China, the upgrading requirement of national six-gasoline simultaneously reduces the olefin content in the gasoline, and refineries generally have dual requirements of gasoline yield reduction and olefin. The olefin catalytic cracking technology can effectively convert olefin components in light gasoline of a refinery into high value-added products such as ethylene and propylene and the like, and simultaneously reduce the yield and the olefin content of the gasoline, thereby achieving multiple purposes. However, a refinery usually has only a gas separation device for separating propylene, ethylene is usually discharged to a fuel system as refinery dry gas, and the refinery does not have the capability of separating ethylene, so that an ethylene separation device needs to be newly built to separate ethylene from a fraction below C3, the investment is large, the requirement of ethylene separation on a public work is high, and the refinery usually does not have a refrigerant with high quality. Therefore, the application of the existing olefin catalytic cracking process in a refinery has certain difficulties.
In conclusion, the existing olefin catalytic cracking process technology has the problems that the newly-built olefin separation device is large in investment, the product separation condition is harsh, and the like, and is difficult to apply in refineries. The invention aims to solve the problems.
Disclosure of Invention
The invention aims to solve the technical problem that the application of the technology in a refinery is limited by large investment of a newly-built olefin separation device, harsh product separation conditions, high public engineering requirements and the like in the existing olefin catalytic cracking process technology. The invention provides a novel device and a novel method for producing propylene by catalytic cracking of olefin. The device and the method have the advantages of easy application to refineries, capability of depending on the existing public engineering conditions, investment saving and the like, and are particularly suitable for application of the olefin catalytic cracking process in refineries.
In order to solve the above problems, an aspect of the present invention provides an apparatus for producing propylene by catalytic cracking of olefins, comprising: the system comprises an olefin catalytic cracking reactor, a reaction gas compressor, an absorption tower, a desorption tower, a depropanization tower and a circulating material tower; a heating furnace is arranged on an inlet pipeline of the olefin catalytic cracking reactor, and an outlet pipeline is connected to a reaction gas compressor; the outlet pipeline of the reaction gas compressor comprises two branches, one branch is communicated with the bottom of the absorption tower, and the other branch is communicated with the top of the desorption tower; the bottom of the absorption tower is communicated with the top of the desorption tower, and the top of the absorption tower is communicated with the bottom of the circulating material tower; the bottom of the desorption tower is communicated with a depropanization tower; the bottom of the depropanization tower is communicated with a circulating material tower; the top of the circulating material tower is communicated with an olefin catalytic cracking reactor.
In a specific embodiment of the invention, an inlet pipeline of the olefin catalytic cracking reactor is firstly provided with a feeding and discharging heat exchanger for recovering heat of reaction products, and then the reaction products enter a heating furnace to be heated to the reaction temperature.
In another embodiment of the present invention, the absorption tower is provided with three interstage coolers for removing heat released during absorption and improving the absorption effect of the tower.
It will be understood by those skilled in the art that the meaning of "the bottom of the absorption column and the top of the desorption column are in communication" includes the absorption liquid passing from the bottom of the absorption column through a line to the top of the desorption column and the desorption gas passing from the top of the desorption column through a line to the bottom of the absorption column.
In the present invention, the line for "the other line communicating with the top of the desorption tower" at the outlet of the reaction gas compressor and the line for "the bottom of the absorption tower communicating with the top of the desorption tower" include both the case where both the two lines are directly connected to the top of the desorption tower and the case where both the two lines are combined and then connected to the desorption tower, and preferably, the case where both the two lines are combined and then connected to the top of the desorption tower.
In another aspect, the present invention provides a method for producing propylene by catalytic cracking of olefins, comprising: the olefin catalytic cracking reaction raw material and the circulating material are converged, heated to the reaction temperature by a heating furnace, and then enter an olefin catalytic cracking reactor for cracking reaction to obtain a reaction product; pressurizing the reaction product by a reaction gas compressor to obtain compressed gas and compressed condensate; the compressed gas enters the bottom of the absorption tower, absorption tail gas rich in ethylene is obtained from the top of the absorption tower, and absorption liquid is obtained from the bottom of the absorption tower; absorption liquid and compressed condensate enter from the upper part of the desorption tower, desorption gas returns to the absorption tower from the top of the absorption tower through a pipeline, and the bottom liquid of the desorption tower enters a depropanizing tower; separating out crude propylene from the top of the depropanizing tower, and feeding the depropanizing tower bottom liquid into a circulating material tower; and separating out four carbon components from the top of the circulating material tower, wherein at least part of the four carbon components is used as circulating material flow, and at least part of the bottom liquid of the circulating material tower is used as an absorbent to enter the upper part of the absorption tower.
In the above technical scheme, the absorbent comprises five or more components of carbon of the olefin catalytic cracking product.
In the technical scheme, the absorbent is cooled to 40-42 ℃ by a refrigerant and then enters the absorption tower.
In the technical scheme, the operating pressure of the absorption tower is 1.0-1.5 MPAG.
In the technical scheme, the number of theoretical plates of the absorption tower is 20-40.
In the above technical scheme, the olefin catalytic cracking feedstock comprises at least one of a carbon tetramonoolefin and a carbon pentamonoolefin. The carbon tetramonoolefin includes isobutylene, 1-butene, cis-2-butene and trans-2-butene, and the carbon pentamonoolefin has a large number of isomers including 1-pentene, 2-methyl-1-butene, 2-methyl-2-butene, 3-methyl-1-butene, cis-2-pentene and trans-2-pentene.
The olefin catalytic cracking reactor is arranged in a fixed bed reactor, the reaction temperature is 500-600 ℃, and the reaction pressure is 0.01-0.5 MPaG.
By adopting the method, olefin cracking raw materials such as carbon tetraolefin and carbon pentaolefin are subjected to cracking reaction in an olefin catalytic cracking reactor and are cracked into reaction products containing ethylene, propylene and other low-carbon hydrocarbons at the reaction temperature of 500-600 ℃ and the reaction pressure of 0.01-0.5 MPaG. The reaction product is cooled, compressed and then sent to an absorption tower. The reaction product of the gas phase is in countercurrent contact with the absorbent in the absorption tower, propylene in the reaction product is absorbed by the absorbent, flows out of the tower kettle of the absorption tower and enters the desorption tower, and components such as methane, ethylene, ethane and the like which are not absorbed by the absorbent are discharged from the top of the absorption tower. The absorption tower bottoms enter from the top of the desorption tower, and a small amount of ethylene absorbed by the absorbent is removed in the desorption tower so as to ensure the impurity content index of the final propylene product. The bottom liquid of the desorption tower is then sent to a depropanizer, crude propylene products containing propylene and propane are obtained at the tower top, and carbon four and heavier components flow out of the tower bottom and are sent to a circulating material tower. The top of the circulating material tower is provided with four carbon components, and the bottom of the circulating material tower is provided with five carbon components and heavier components. And the four carbon components at the tower top are returned to the reaction unit as circulating materials, and the rest are discharged as liquefied gas products. Most of the carbon five and heavier components in the tower bottom are used as absorbent and enter the upper part of the absorption tower, and the rest is discharged as a crude gasoline byproduct.
By adopting the method, the absorbent of the absorption tower comes from the reaction product of the olefin catalytic cracking reaction, and the reaction product is a mixed hydrocarbon material containing heavy components such as benzene, toluene, xylene and the like after the four components of carbon are separated by the circulating material tower. The use of the heavier component as the absorbent has the advantages that the loss of the absorbent in absorbing the tail gas at the top of the absorption tower is small, the absorption capacity of the absorbent for ethylene is weak, and the load of the desorption tower can be reduced. The absorption process has better effect at lower temperature, therefore, the absorbent is cooled by circulating cooling water before entering the absorption tower.
By adopting the method, the pressure of the outlet of the compressor of the olefin cracking device is controlled to be 1.0-1.5 MPaG, and the pressure can be achieved by adopting two-stage compression. The outlet pressure of the compressor in the prior art is usually above 1.5MPaG, so that the depropanizer is convenient to separate carbon three and lighter components, and therefore three-stage compression is generally needed to meet the pressure requirement of gas separation. In addition, in the prior art, the top of the depropanizer generally needs to adopt chilled water or propylene refrigerant, and refinery enterprises generally cannot meet the requirement of the public engineering. By adopting the device and the method, the refinery enterprises with the circulating cooling water and the low-pressure steam can meet the public engineering requirements of the whole cracking device, the operating condition requirements of the device are reduced, and the popularization and the application of the technology in the refinery enterprises are facilitated.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
In FIG. 1, 1 is an olefin-containing feedstock; 2 is a recycle stream; 3 absorbing tail gas; 4 is crude propylene; 5 is liquefied gas; 6 is crude gasoline; a is a raw material vaporizer; b is a charging and discharging heat exchanger; c is a heating furnace; d is an olefin catalytic cracking reactor; e is a compressor; f is an absorption tower; g is a desorption tower; h is a depropanizer; i is a debutanizer.
The process is briefly described as follows: the liquid phase olefin-containing raw material 1 is vaporized by a raw material vaporizer A and then is converged with a circulating material flow 2, and after heat exchange between a feeding heat exchanger B and a discharging heat exchanger B and a high-temperature reaction product, the temperature is raised to a proper cracking reaction temperature by a heating furnace and then the mixture enters an olefin catalytic cracking reactor D; after heat exchange is carried out on the reaction product by a feeding and discharging heat exchanger B, pressurization is carried out by a compressor E; the gas phase at the outlet of the compressor enters from the bottom of the absorption tower F, the absorption tail gas 3 is discharged from the top of the absorption tower, and the absorption liquid flows out from the bottom of the absorption tower; the absorption liquid and the condensate of the compressor enter a desorption tower G together, the desorption gas returns to the absorption tower, and the residue of the desorption tower enters a depropanizing tower H; separating out crude propylene 4 from the top of the depropanizing tower, and feeding the depropanizing tower bottom liquid into a debutanizing tower I; and separating four carbon components from the top of the debutanizer, wherein gas phase is extracted as a circulating material flow 2, liquid phase is extracted as a byproduct of liquefied gas 5, part of the debutanizer kettle liquid is discharged as a byproduct of crude gasoline 6, and part of the debutanizer kettle liquid is used as an absorbent and enters the top of the absorption tower.
The present invention will be further illustrated by the following examples, but is not limited to these examples.
Detailed Description
[ example 1 ]
According to the flow shown in figure 1, a carbon four raw material containing 75% of butene by mass is adopted, the flow rate is 9 tons/hour, a fixed bed is adopted in an olefin catalytic cracking reactor, the catalyst is a full-crystalline composite molecular sieve catalyst, the reaction temperature is 560 ℃, and the reaction pressure is 0.08 MPaG. The reactor compressor is two-stage compression, the first stage outlet pressure is 0.30MPaG, and the second stage outlet pressure is 1.10 MPaG. The operating pressure of the absorption tower is 1.0MPaG, the theoretical plate number of the absorption tower is 40, and interstage circulating water coolers are arranged on the 10 th and 25 th tower plates from top to bottom of the absorption tower. The dosage of the absorbent of the absorption tower is 16000 kg/h, the total yield of the ethylene and the propylene of the device is 60 percent (mass fraction), and the energy consumption of the device is 1158 kg standard oil/h.
[ example 2 ]
According to the flow shown in the figure 1, a mixed raw material of four carbon and five carbon, which contains 40 mass percent of butene and 35 mass percent of pentene, is adopted, and the flow rate is 12 tons/hour. The hydrocarbon catalytic cracking reactor adopts a fixed bed, the catalyst is a full-crystalline composite molecular sieve catalyst, the reaction temperature is 560 ℃, and the reaction pressure is 0.10 MPaG. The reactor compressor is two-stage compression, the first stage outlet pressure is 0.35MPaG, and the second stage outlet pressure is 1.40 MPaG. The operating pressure of the absorption tower is 1.30MPaG, the theoretical plate number of the absorption tower is 40, the 5 th tray from top to bottom of the absorption tower is provided with a circulating water cooler, and the 35 th tray from top to bottom of the absorption tower is provided with a circulating water cooler. The dosage of the absorbent in the absorption tower is 12000 kg/h, the total yield of the ethylene and the propylene in the device is 62.1 percent (mass fraction), and the energy consumption of the device is 1538 kg standard oil/h.
[ example 3 ]
According to the flow shown in the figure 1, a carbon five raw material containing 77 percent of amylene by mass is adopted, and the flow rate is 9 tons/hour. The olefin catalytic cracking reactor adopts a fixed bed, the catalyst is a full-crystalline composite molecular sieve catalyst, the reaction temperature is 550 ℃, and the reaction pressure is 0.10 MPaG. The reactor compressor is two-stage compression, the first stage outlet pressure is 0.35MPaG, and the second stage outlet pressure is 1.40 MPaG. The operating pressure of the absorption tower is 1.30MPaG, the theoretical plate number of the absorption tower is 40, a circulating water cooler is arranged on the 5 th tray from top to bottom of the absorption tower, a circulating water cooler is arranged on the 30 th tray from top to bottom of the absorption tower, and the dosage of the absorbent in the absorption tower is 8768 kg/h. The total yield of ethylene and propylene in the device is 61.3 percent (mass fraction), and the energy consumption of the device is 851 kg standard oil/h.
[ COMPARATIVE EXAMPLE ]
The separation system employed rectification separation according to the feed conditions, olefin catalytic cracking reaction conditions, and compressor operating conditions described in example 1. The material flow from the outlet of the compressor firstly enters a depropanizing tower, the operation temperature at the top of the depropanizing tower is 18 ℃, and the material flow can be cooled by adopting chilled water. And (3) obtaining components of carbon three and below at the top of the depropanizing tower, pressurizing the components of carbon three and below to 2.6MPaG by a three-section compressor, and then separating ethylene-rich gas and a crude propylene product in the deethanizing tower, wherein the operation temperature at the top of the deethanizing tower is-27 ℃, and the process requirements can be met only by adopting a propylene refrigerant or an ethylene refrigerant. The bottom liquid of the depropanizing tower is carbon four and heavier components, and the circulating material flow, the liquefied gas and the crude gasoline are separated through the debutanizing tower. The total yield of ethylene and propylene in the device is 60 percent (mass fraction), and the energy consumption of the device is 1387 kilograms of standard oil/hour.
Claims (10)
1. An apparatus for producing propylene, characterized in that the apparatus comprises: the system comprises an olefin catalytic cracking reactor, a reaction gas compressor, an absorption tower, a desorption tower, a depropanization tower and a circulating material tower; a heating furnace is arranged on an inlet pipeline of the olefin catalytic cracking reactor, and an outlet pipeline is connected to a reaction gas compressor; the outlet pipeline of the reaction gas compressor comprises two branches, one branch is communicated with the bottom of the absorption tower, and the other branch is communicated with the top of the desorption tower; the bottom of the absorption tower is communicated with the top of the desorption tower, and the top of the absorption tower is communicated with the bottom of the circulating material tower; the bottom of the desorption tower is communicated with a depropanization tower; the bottom of the depropanization tower is communicated with a circulating material tower; the top of the circulating material tower is communicated with an olefin catalytic cracking reactor.
2. The apparatus for producing propylene according to claim 1, wherein said olefin catalytic cracking reactor is in the form of a fixed bed reactor.
3. The apparatus for producing propylene according to claim 1 or 2, wherein the inlet line of the olefin catalytic cracking reactor is further provided with a feed and discharge heat exchanger.
4. The apparatus for producing propylene according to claim 1 or 2, characterized in that the absorption column is provided with an interstage cooler.
5. A process for producing propylene, characterized in that the process comprises: the olefin catalytic cracking reaction raw material and the circulating material are converged, heated to the reaction temperature by a heating furnace, and then enter an olefin catalytic cracking reactor for cracking reaction to obtain a reaction product; pressurizing the reaction product by a reaction gas compressor to obtain compressed gas and compressed condensate; the compressed gas enters the bottom of the absorption tower, absorption tail gas rich in ethylene is obtained from the top of the absorption tower, and absorption liquid is obtained from the bottom of the absorption tower; absorption liquid and compressed condensate enter from the upper part of the desorption tower, desorption gas returns to the absorption tower from the top of the absorption tower through a pipeline, and the bottom liquid of the desorption tower enters a depropanizing tower; separating out crude propylene from the top of the depropanizing tower, and feeding the depropanizing tower bottom liquid into a circulating material tower; and separating out four carbon components from the top of the circulating material tower, wherein at least part of the four carbon components is used as circulating material flow, and at least part of the bottom liquid of the circulating material tower is used as an absorbent to enter the upper part of the absorption tower.
6. The process for producing propylene according to claim 5, wherein the absorbent contains five or more carbon components of the olefin catalytic cracking product.
7. The method for producing propylene according to claim 5 or 6, wherein the absorbent is cooled to 40-42 ℃ by a cooling medium and then enters the absorption tower.
8. The process for producing propylene according to claim 5, wherein the operating pressure of the absorption column is 1.0 to 1.5 MPaG; and/or the number of theoretical plates of the absorption tower is 20-40.
9. The process for producing propylene according to claim 5, wherein the olefin catalytic cracking feedstock comprises at least one of a carbon tetramonoolefin and a carbon pentamonoolefin.
10. The method for producing propylene according to claim 5, wherein the temperature of the reaction for catalytic cracking of olefin is 500 to 600 ℃; and/or the pressure of the olefin catalytic cracking reaction is 0.01-0.2 MPaG.
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| CN202010394877.9A CN113651669B (en) | 2020-05-12 | Apparatus and process for producing propylene |
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