CN111875465A - Method for producing low-carbon olefin by using oxygen-containing compound - Google Patents
Method for producing low-carbon olefin by using oxygen-containing compound Download PDFInfo
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- CN111875465A CN111875465A CN202010661528.9A CN202010661528A CN111875465A CN 111875465 A CN111875465 A CN 111875465A CN 202010661528 A CN202010661528 A CN 202010661528A CN 111875465 A CN111875465 A CN 111875465A
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- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 79
- 239000001301 oxygen Substances 0.000 title claims abstract description 79
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 78
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 78
- 150000001875 compounds Chemical class 0.000 title claims abstract description 74
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 257
- 239000003054 catalyst Substances 0.000 claims abstract description 211
- 239000002994 raw material Substances 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 26
- 230000009471 action Effects 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 58
- 239000004215 Carbon black (E152) Substances 0.000 claims description 33
- 229930195733 hydrocarbon Natural products 0.000 claims description 33
- 150000002430 hydrocarbons Chemical class 0.000 claims description 33
- 238000000926 separation method Methods 0.000 claims description 31
- 150000001336 alkenes Chemical class 0.000 claims description 25
- 238000011069 regeneration method Methods 0.000 claims description 22
- 239000007787 solid Substances 0.000 claims description 21
- 230000008929 regeneration Effects 0.000 claims description 18
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 14
- 238000009826 distribution Methods 0.000 claims description 13
- 239000007795 chemical reaction product Substances 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 11
- 238000005192 partition Methods 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 57
- 239000003795 chemical substances by application Substances 0.000 description 28
- 239000000047 product Substances 0.000 description 15
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 11
- 239000003546 flue gas Substances 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- 239000002699 waste material Substances 0.000 description 7
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 238000005336 cracking Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 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
- 239000003245 coal Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- -1 ethylene, propylene, butadiene Chemical class 0.000 description 3
- 150000002894 organic compounds Chemical class 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 229940126214 compound 3 Drugs 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 241000269350 Anura Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- GHTGICGKYCGOSY-UHFFFAOYSA-K aluminum silicon(4+) phosphate Chemical compound [Al+3].P(=O)([O-])([O-])[O-].[Si+4] GHTGICGKYCGOSY-UHFFFAOYSA-K 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010523 cascade reaction Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000031700 light absorption Effects 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000003786 synthesis reaction Methods 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
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention discloses a method for producing low-carbon olefin by using oxygen-containing compounds in the technical field of petrochemical industry.A reaction raw material in an auxiliary reaction zone enters the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone after being preheated, is directly contacted with a high-temperature catalyst from a regenerator, and rapidly reacts under the action of the catalyst; the method is suitable for the characteristics of rapid reaction, strong heat release, low catalyst-alcohol ratio, high product selectivity and the like of a process for preparing the low-carbon olefin from the oxygen-containing compound, and aims to solve the problems of low-carbon olefin selectivity, furthest exert the advantages of the reaction and improve the low-carbon olefin selectivity in the prior art.
Description
Technical Field
The invention belongs to the technical field of olefin preparation, and particularly relates to a method and a device for producing low-carbon olefin by using an efficient oxygen-containing compound.
Background
Light olefins (ethylene, propylene, butadiene) and light aromatics (benzene, toluene, xylene) are basic feedstocks for petrochemical industry. The traditional preparation route of ethylene and propylene is produced by naphtha cracking, and the disadvantage is that the traditional preparation route is excessively dependent on petroleum. The preparation of low-carbon olefins (MTO for short) such as ethylene and propylene from Methanol is another process route for preparing olefins, and the development of the prior process technology tends To be mature. The industrialization of MTO technology opens up a new process route for producing petrochemical basic raw materials by gasifying coal or natural gas, is favorable for changing the product pattern of the traditional coal chemical industry, and is an effective way for realizing the extension development of the coal chemical industry to the petrochemical industry.
Oxygen-containing organic compounds represented by methanol or dimethyl ether are typical oxygen-containing organic compounds, and are mainly produced from coal-based or natural gas-based synthesis gas. The process for producing low-carbon olefins mainly comprising ethylene and propylene by using oxygen-containing organic compounds represented by methanol as raw materials mainly comprises MTO and MTP technologies at present.
The reaction features fast reaction, strong heat release, low alcohol-to-agent ratio, and reaction and regeneration in continuous reaction-regeneration dense-phase fluidized bed reactor. The high-temperature oil gas which is generated by the reaction and is rich in low-carbon olefins such as ethylene, propylene and the like needs to be quenched and washed by water, the catalyst in the oil gas is removed, the temperature of the oil gas is reduced, and then the oil gas is sent to an olefin separation system for separation. The existing on-stream device for preparing olefin from oxygen-containing compound has the following common problems: the selectivity of olefin is lower than that of the laboratory, and the unit consumption of methanol is increased.
In recent years, methods for improving the selectivity of lower olefins have become a focus and focus of research by those skilled in the art. People have conducted extensive research and exploration in the aspects of process flows, equipment structures and the like.
A process for converting an oxygenate feedstock to light olefins is disclosed in exxonmobil chemical patent CN1102317238B and relates to a process for converting a feedstock comprising oxygenate to a product comprising light olefins. In particular, the invention relates to the conversion of an oxygenate feedstock to a product comprising light olefins in a reaction apparatus using a silicoaluminophosphate catalyst. More specifically, the present invention provides a means by which an optimum coke level can be determined and used to produce an optimum or near-optimum yield of light olefins, such as ethylene and propylene, in an oxygenate to olefin system.
The oil products on the globe CN1830926A discloses a catalyst cooler for an oxygenate conversion reactor. The invention comprises contacting an oxygenate feed stream with a catalyst in a reactor and converting the oxygenate feed stream to said light olefins. When reaction deposits block pores on the surface of the catalyst, the catalyst fails. A portion of the spent catalyst is regenerated in a regenerator and this portion is recycled back for contact with more oxygenate feed stream. A catalyst cooler coupled to the reactor is capable of cooling the spent catalyst circulated through the cooler before the spent catalyst is contacted with more of the oxygenate feed stream. In one embodiment, all of the spent catalyst entering the catalyst cooler is withdrawn from the bottom of the catalyst cooler.
The invention discloses a method for improving the yield of low-carbon olefin in a process for preparing olefin from methanol, which relates to a method for improving the yield of low-carbon olefin in a process for preparing olefin from methanol, and mainly solves the problem of low yield of low-carbon olefin in the prior art. The invention adopts a method for improving the yield of low-carbon olefin in a process for preparing olefin from methanol, which mainly comprises the following steps: (1) the method comprises the following steps that a raw material containing methanol enters a first fast fluidized bed reaction zone and contacts with a silicon-aluminum phosphate molecular sieve catalyst to generate a product material flow I containing low-carbon olefin and form an inactivated catalyst; (2) the deactivated catalyst enters a regenerator for regeneration, the regenerated catalyst enters a riser reaction zone and contacts with a raw material containing hydrocarbon with more than four carbon atoms, and the generated product and the catalyst enter a second fast fluidized bed reaction zone and contact with the raw material containing hydrocarbon with more than four carbon atoms and a second catalyst from the regenerator to generate a product material flow II containing low-carbon olefin and form a pre-carbon-deposited catalyst at the same time; (3) the product material flow II is mixed with the product material flow I after gas-solid separation and enters a separation section, and the catalyst of the pre-deposited carbon returns to the first fast bed reaction zone.
Chinese patent CN103073377B discloses a method for preparing low-carbon olefin by catalytic conversion of oxygen-containing compound, a method for generating low-carbon olefin by catalytic conversion of oxygen-containing compound, introducing oxygen-containing compound raw material into an internal circulation gas-solid fluidized bed reactor from the bottom, contacting with a cracking catalyst in a reaction zone and moving upwards, and carrying out alkylation and cracking reaction; after the reaction, the oil gas and the carbon deposition catalyst are subjected to gas-solid separation through a gas-solid separation zone at the upper part of the reaction zone, and the separated oil gas is further separated in a subsequent separation system; the separated carbon-deposited catalyst is settled in a stripping zone, oil gas adsorbed and carried in the catalyst is stripped, a part of the carbon-deposited catalyst in the stripping zone enters a catalyst descending zone to move downwards, and enters the bottom of a reaction zone through a gap at the bottom of the catalyst descending zone for recycling; the other part of the carbon-deposited catalyst is introduced into a catalyst regenerator through a catalyst inclined tube to be regenerated and burnt for regeneration, and the regenerated catalyst returns to the internal circulation gas-solid fluidized bed reactor for recycling. The reactor provided by the invention can be used for a method for preparing low-carbon olefin by using an oxygen-containing compound, and has the advantages of simple operation and high yield of the low-carbon olefin.
In summary, the reaction characteristics of the process for preparing low-carbon olefin from oxygen-containing compound (methanol is typically adopted at present) are rapid reaction, strong heat release and low alcohol content, and the reaction and the regeneration are carried out in a continuous reaction-regeneration dense-phase fluidized bed reactor. The high-temperature oil gas which is generated by the reaction and is rich in low-carbon olefins such as ethylene, propylene and the like needs to be quenched and washed by water, the catalyst in the high-temperature oil gas is removed, and the high-temperature oil gas is sent to a lower olefin separation system for separation after being cooled. The SAPO catalyst used in the process has high manufacturing cost, the price is 10-30 times that of a common catalytic cracking catalyst, and the abrasion and the running loss of the catalyst are reduced to the maximum extent during engineering design and equipment selection. Aiming at the reaction characteristics of the process, various types of device types are developed, and a representative reactor type comprises a fixed bed, a riser, a fast fluidized bed and the like.
In summary, in the prior art, the olefin selectivity is improved to a certain extent by optimizing the internal structure of the reactor, optimizing the process flow and optimizing the operating conditions, but the problem of low olefin selectivity still exists in the existing on-line device, and the invention specifically solves the problem.
Disclosure of Invention
The invention provides a method for producing low-carbon olefin by using an efficient oxygen-containing compound, which is suitable for the characteristics of rapid reaction, strong heat release, low alcohol-alcohol ratio, high product selectivity and the like of a process for preparing low-carbon olefin by using the oxygen-containing compound, and aims to solve the problems of low-carbon olefin selectivity, furthest play the advantages of the reaction and improve the low-carbon olefin selectivity in the prior art.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
the method for producing the low-carbon olefin by using the oxygen-containing compound is characterized by comprising the following steps of:
1) preheating reaction raw materials in an auxiliary reaction zone, feeding the preheated reaction raw materials into the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone, directly contacting with a high-temperature catalyst from a regenerator, quickly reacting under the action of the catalyst, feeding reaction products into a catalyst collecting zone of a reactor, feeding part of a spent catalyst after reaction to a main reaction zone of the reactor through an auxiliary reaction catalyst circulating pipe, feeding part of the spent catalyst into a spent stripper through a spent catalyst inlet pipe for stripping, and feeding the stripped spent catalyst into the regenerator through a spent catalyst conveying pipe;
2) preheating reaction raw materials in the main reaction zone, feeding the preheated reaction raw materials into the main reaction zone of the reactor through a feeding distributor at the bottom of the main reaction zone, reacting the preheated reaction raw materials with a catalyst from the auxiliary reaction zone, separating a reaction product in the main reaction zone from a reaction oil gas through a gas-solid quick separation device, removing most of the carried catalyst together with the reaction product entering a catalyst collecting zone of the reactor in the step 1) through a gas-solid separation facility of the reactor, and leading out from the top of the reactor;
3) the catalyst in the auxiliary reaction zone of the reactor passes through an auxiliary reaction catalyst circulating pipe, and the spent catalyst in the catalyst collecting zone of the reactor passes through the catalyst circulating pipe and respectively enters the main reaction zone of the reactor to provide the catalyst required by the reaction for the main reaction zone of the reactor;
4) the spent catalyst which loses activity after reaction enters a spent stripper from a catalyst collecting region for steam stripping and then enters a regenerator through a spent conveying pipe; or one part enters the regenerator through the spent conveying pipe, and the other part enters the main reaction zone of the reactor;
5) after the catalyst to be regenerated is burnt in the regenerator, the regenerated catalyst is stripped by the regenerated stripper, and the stripped regenerated catalyst enters the catalyst collecting region through the regenerated catalyst conveying pipe.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the auxiliary reaction zone is arranged in the catalyst collecting zone and is separated from the catalyst collecting zone and the main reaction zone by a partition plate, and the main reaction zone and the auxiliary reaction zone are communicated by an auxiliary reaction catalyst circulating pipe; the circulating pipe is provided with a slide valve or a plug valve for controlling the circulating amount of the catalyst.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the main reaction zone is arranged below the catalyst collecting zone and separated from the catalyst collecting zone by a dilute phase pipe, the top of the dilute phase pipe is provided with a catalyst fast-separating device, and the outlet of the catalyst fast-separating device is connected with the inlet of a gas-solid separation facility of the reactor. A catalyst circulating pipe is arranged between the main reaction area and the catalyst collecting area of the reactor, and a slide valve or a plug valve is arranged on the catalyst circulating pipe to control the circulating amount of the catalyst.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the reaction raw material entering the auxiliary reaction zone can be light hydrocarbon gas (C)4～C10) And/or oxygenates, preferably light hydrocarbon gas (C)4～C10) (ii) a The reaction raw material entering the main reaction zone can also be light hydrocarbon gas (C)4～C10) And/or an oxygenate, preferably an oxygenate.
The invention relates toThe method for producing the low-carbon olefin by the oxygen-containing compound is further characterized by comprising the following steps: the oxygen-containing compound is an oxygen-containing compound mainly comprising methanol or dimethyl ether, and the light hydrocarbon gas is C4～C10A gas.
The invention relates to a method for producing low-carbon olefin by using high-efficiency oxygen-containing compounds, which is further technically characterized in that: one or more feed distributors are arranged at the lower part of the main reaction zone, and the oxygen-containing compound raw material taking methanol or dimethyl ether as the main component can be injected into the lower part of the main reaction zone in one or more strands.
The invention relates to a method for producing low-carbon olefin by using high-efficiency oxygen-containing compounds, which is further technically characterized in that: one or more feeding distributors for light hydrocarbon gas (C) are arranged at the lower part of the auxiliary reaction zone4～C10) The raw material can be injected into the lower part of the auxiliary reaction zone in one or more branches.
The invention relates to a method for producing low-carbon olefin by using high-efficiency oxygen-containing compounds, which is further characterized by comprising the following steps: the feeding distributor is positioned at the lower part of each reaction zone and is a distribution pipe or a distribution plate, preferably a distribution pipe.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the main reaction zone and the auxiliary reaction zone of the reactor are both fluidized bed reactors. The secondary reaction zone is preferably a turbulent bed reactor and the primary reaction zone may be a fast bed reactor or a turbulent bed reactor.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the catalyst in the auxiliary reaction area of the reactor passes through the auxiliary reaction catalyst circulating pipe, and the catalyst in the catalyst collecting area of the reactor passes through the catalyst circulating pipe and respectively enters the main reaction area of the reactor, so that the catalyst required by the reaction is provided for the main reaction area of the reactor, and the catalyst is used for controlling the airspeed of the main reaction area of the reactor so as to adjust the olefin selectivity of the main reaction area.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the regenerated catalyst conveying pipe can also be used as a riser reactor, and light hydrocarbon gas can be injected when the regenerated catalyst conveying pipe is used as the riser reactor, and the light hydrocarbon gas can be injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands (2-5 strands).
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the raw material feeding pipe line is provided with a light hydrocarbon gas injection port, and light hydrocarbon gas enters the main reaction area and the auxiliary reaction area of the reactor through the raw material feeding pipe independently or after being mixed with oxygen-containing compounds.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: and 2) removing the entrained catalyst from the reaction product in the step 2) through a reactor three-stage cyclone separator and a reactor four-stage cyclone separator, leading out, and sending to a rear quenching and water washing system after heat exchange. The catalyst recovered by the reactor three-stage cyclone separator and the reactor four-stage cyclone separator enters a waste reactor three-cyclone recovery catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a discharging agent pipeline.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: and 4) a stripping grating or a stripping baffle plate is arranged in the spent stripper, and a stripping medium distribution ring is also arranged in the spent stripper.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: one end of the auxiliary reaction spent stripper in the step 1) is communicated with the lower part of an auxiliary reaction area of the reactor through a spent agent inlet pipe (II), and the other end of the auxiliary reaction spent stripper is communicated with the regenerator through a spent agent conveying pipe (IV); and a slide valve is arranged on the spent agent conveying pipe (IV).
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: a stripping grating or a stripping baffle and a stripping medium distribution ring are arranged in the auxiliary spent stripper in the step 1).
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: a stripping grating or a stripping baffle and/or a heat taking facility and a stripping medium distribution circulator are arranged in the regeneration stripper in the step 5).
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: and 5) removing most of carried catalyst from the flue gas generated after the catalyst and main air are contacted and burned in a countercurrent mode through a two-stage cyclone separator, discharging the flue gas, sending the flue gas to a waste heat boiler through a pressure reducing valve (if needed), a double-acting slide valve and a pressure reducing pore plate to recover heat, and exhausting the flue gas to atmosphere through a chimney.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: and the spent catalyst in the catalyst collecting area of the reactor enters the external heat remover through an external heat-taking inlet pipe to get heat, and then returns to the main reaction area of the reactor.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: an internal heat collector and/or an external heat collector are arranged in the regenerator.
The regeneration mode of the catalyst in the regenerator can adopt incomplete regeneration or complete regeneration, and preferably adopts incomplete regeneration.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the auxiliary reaction zone can be positioned in a catalyst collecting zone of the reactor and is separated from the catalyst collecting zone by a partition plate. The ratio of the cross sectional area of the auxiliary reaction zone to the main reaction zone is in the range of 1-30%, preferably 3-20%, one or more annular partition plates can be arranged in the middle of the auxiliary reaction zone to partition the auxiliary reaction zone into two or more reaction bed layers with equal area so as to meet the requirements of reaction process conditions.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the reaction temperature of the auxiliary reaction zone of the reactor is in the range of 350-700 ℃, preferably 450-650 ℃; the reaction temperature of the main reaction zone is within the range of 250-650 ℃, preferably within the range of 350-600 ℃; the linear speed of the reactor is in the range of 0.1-5 m/s, the linear speed of the main reaction zone is preferably in the range of 0.6-3 m/s, and the linear speed of the auxiliary reaction zone is preferably in the range of 0.1-1 m/s.
The regeneration temperature is within the range of 400-700 ℃, preferably within the range of 450-650 ℃; the reaction pressure is in the range of 0.05-3.0 MPaG, preferably in the range of 0.1-2.0 MPaG; the regeneration pressure is in the range of 0.1-3.0 MPaG, preferably in the range of 0.1-2.0 MPaG.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: the temperature of the reactor three-stage cyclone separator is within the range of 300-650 ℃, preferably within the range of 400-550 ℃; the pressure is in the range of 0.01 to 3.0MPaG, preferably in the range of 0.04 to 2.0 MPaG.
The method for producing the low-carbon olefin by the oxygen-containing compound better solves the problem of low selectivity of the low-carbon olefin in the prior art, exerts the advantages of each reaction zone to the maximum extent, improves the selectivity of the low-carbon olefin, and can be used in the industrial production of producing liquid products by the oxygen-containing compound, such as: MTO technology (methanol to olefin technology), MTP technology (methanol to propylene technology), MTA technology (methanol to aromatics technology), MTG technology (methanol to gasoline technology) and the like. In addition, the equipment has the advantages of simple structure, easy realization, wide application range, low equipment investment and the like, and can be widely applied to devices for preparing low-carbon olefin products by converting oxygen-containing compounds.
Compared with the prior art, the invention has the advantages that:
1) the method provided by the invention can improve the linear speed of the reactor, reduce the diameter of the reactor and improve the handling capacity of the device.
2) By adopting the method provided by the invention, the reactor adopts cascade reaction zones, and the characteristics of different reaction zones can be utilized to efficiently improve the selectivity of target products, such as the selectivity and the yield of low-carbon olefin products; by arranging the auxiliary reaction zone, the regenerated catalyst is pre-carbonized, the temperature of the catalyst entering the main reaction zone is reduced, and the activity of the outer surface of the catalyst is reduced. The cracking reaction in the auxiliary reaction zone is an endothermic reaction, so that the contact temperature of reaction oil gas and a high-temperature regenerated catalyst in the main reactor is reduced, the occurrence of non-target reactions is reduced, and the selectivity of low-carbon olefin is improved; the catalyst adsorbing a small amount of coke continuously performs exothermic reaction with the oxygen-containing compound, so that the influence of an induction period on the reaction is reduced, and the improvement of the selectivity of the low-carbon olefin is facilitated. The yield of ethylene and propylene can be increased simultaneously through the cracking reaction of light hydrocarbon gas.
3) The method provided by the invention utilizes the characteristics of strong heat release of oxygen-containing compound converted olefin and strong heat absorption of light hydrocarbon gas conversion reaction to carry out light hydrocarbon gas reaction in a high-temperature region, thereby not only meeting the conversion requirement of the reaction, but also realizing the coupling of heat and forming an interconnected complete system by coupling.
4) By adopting the method provided by the invention, the same catalyst is adopted in the reactions of strong heat release of the oxygen-containing compound converted olefin and light hydrocarbon gas conversion, and the mixing caused by using different catalysts is avoided; both the two are carried out in different reaction zones in a fluidized reaction mode, so that the advantages of respective reactions are exerted to the maximum extent, and the selectivity of a target product is improved; the products are distributed similarly and can share a set of separation system.
5) By adopting the method provided by the invention, the auxiliary reaction zone and the main reaction zone form a high-efficiency reactor, so that the investment and the occupied area of the device are saved.
The invention is further described with reference to the following figures and detailed description. But not to limit the scope of the invention.
Drawings
FIG. 1 is a schematic flow chart of a method for producing low-carbon olefins by using an oxygen-containing compound according to the present invention.
The reference symbols shown in the figures are: 1-regenerated catalyst conveying pipe, 2-light hydrocarbon gas, 3-oxygen-containing compound mainly containing methanol or dimethyl ether, 4-feeding distributor II, 5-spent slide valve (I), 6-heat taking facility in main reaction zone, 7-reactor main reaction zone, 8-auxiliary reaction catalyst circulating pipe, 9-feeding distributor I, 10-reactor auxiliary reaction zone, 11-partition plate, 12-catalyst fast-separating device, 13-reactor catalyst collecting zone, 14-reaction oil gas, 15-waste catalyst, 16-reactor triple-recycling catalyst storage tank, 17-reactor four-stage cyclone separator, 18-reactor four-stage cyclone separator outlet gas, 19-reactor three-stage cyclone separator and 20-reactor three-stage cyclone separator outlet gas, 21-oil gas collection chamber, 22-reactor gas-solid separation facility, 23-reactor, 24-dilute phase pipe, 25-spent agent inlet pipe (I), 26-catalyst circulation pipe, 27-main reaction zone external heat extractor inlet, 28-spent circulation slide valve/plug valve, 29-main reaction zone external heat extractor, 30-spent slide valve (II), 31-spent agent delivery pipe (I), 32-spent stripper, 33-regenerator internal heat extractor, 34-regenerator coke burning section, 35-flue gas, 36-flue gas collection chamber, 37-regenerator gas-solid separation facility, 38-regenerator, 39-regenerator dilute phase section, 40-regenerator transition section, 41-regenerator external heat extractor inlet and outlet, 42-regenerator external heat extractor, 43-main air, 44-main air distributor, 45-regeneration stripper, 46-regeneration slide valve, 47-conveying gas or raw material, 48-spent agent inlet pipe (II), 49-spent agent conveying pipe (II), 50-reaction external heat-taking slide valve, 51-spent agent conveying pipe (III), 52-spent slide valve (III), 53-spent agent inlet pipe (II), 54-auxiliary reaction spent stripper, 55-spent slide valve (IV) and 56-spent agent conveying pipe (IV).
Detailed Description
As shown in the attached figure 1, the method for producing low-carbon olefin by using the oxygen-containing compound comprises a reactor 23, a regenerator 38, a reactor three-stage cyclone separator 19, a reactor four-stage cyclone separator 17, a reactor three-cyclone recovered catalyst storage tank 16, a spent stripper 32, an auxiliary reaction spent stripper 54, a regeneration stripper 45, a main reaction zone external heat remover 29 and a regenerator external heat remover 42. The reactor 23 comprises a main reaction zone 7, an auxiliary reaction zone 10 and a catalyst collection zone 13, the main reaction zone 7 of the reactor being located below the catalyst collection zone 13 and the auxiliary reaction zone 10 being located above the main reaction zone 7. The main reaction zone 7 is connected with the catalyst collecting zone 13 through a dilute phase pipe 24, the top of the dilute phase pipe 24 is provided with a catalyst fast separation device 12, and the outlet of the catalyst fast separation device 12 is connected with a reactor gas-solid separation facility 22. The catalyst collecting area 13 is communicated with the main reaction area 7 through a catalyst circulating pipe 26; the auxiliary reaction zone 10 is located in the main reactor catalyst collection zone 13, separated by a partition 11. One or more annular partition plates can be arranged in the middle of the auxiliary reaction zone to divide the auxiliary reaction zone into two or more reaction zones with equal areas so as to meet the requirements of reaction process conditions.
An auxiliary reaction spent stripper 54 is additionally arranged at the bottom of the auxiliary reaction area 10 of the reactor, one end of the auxiliary reaction spent stripper 54 is communicated with the bottom of the auxiliary reaction area 10 of the reactor through a spent agent inlet pipe (II) 53, the other end of the auxiliary reaction spent stripper is communicated with the regenerator 38 through a spent agent conveying pipe (IV) 56, and a spent agent conveying pipe (IV) 55 is arranged on the spent agent conveying pipe (IV) 56.
Light hydrocarbon gas (C4-C10) 2 reaction raw materials enter a first feeding distributor 9 at the bottom of an auxiliary reaction zone 10 after being preheated, the light hydrocarbon gas (C4-C10) 2 in the auxiliary reaction zone 10 directly contacts with a high-temperature catalyst from a regenerator 38, the reaction is rapidly carried out under the action of the catalyst, a reaction product enters a catalyst collecting zone 13 of the reactor, the reacted spent catalyst is sent to a main reaction zone 7 of the reactor through an auxiliary reaction catalyst circulating pipe 8, or the reacted spent catalyst is divided into two parts, one part is sent to the main reaction zone 7 of the reactor through the auxiliary reaction catalyst circulating pipe 8, the other part enters an auxiliary reaction spent stripper through a spent catalyst inlet pipe (two) 53 for stripping 54 used for stripping reaction gas carried by the spent catalyst, and the stripped spent catalyst enters a regenerator through a spent catalyst conveying pipe (four) 56.
The main reaction zone 7 is communicated with the auxiliary reaction zone 10 through an auxiliary reaction catalyst circulating pipe 8; the reactor 23 is communicated with a spent stripper 32, an auxiliary reaction spent stripper 54, a heat remover 29 outside the main reaction zone and a reactor three-stage cyclone separator 19; the reactor 23 is provided with a heat remover 29 outside the main reaction zone, is connected with the catalyst collecting zone 13 of the reactor through a spent agent inlet pipe (II) 48 and is connected with the main reaction zone 7 through a spent agent conveying pipe (II) 49. The regenerator 38 is communicated with a regeneration stripper 45, an external regenerator 42, a spent agent conveying pipe (I) 31 and a spent agent conveying pipe (IV) 56. The regenerator 38 is provided with an external regenerator heater 42, and is connected to the regenerator 38 through an external regenerator heat inlet 41.
The bottom of the auxiliary reaction zone 10 is provided with a first feeding distributor 9, the bottom of the main reaction zone 7 is provided with a second feeding distributor 4, and the raw material feeding pipes are introduced into the first feeding distributor 9 or the second feeding distributor 4 for distribution.
One end of the spent stripper 32 is communicated with the bottom of the catalyst collecting zone 13 of the reactor through a spent agent inlet pipe (I) 25, and the other end is communicated with the regenerator 38 through a spent agent conveying pipe (I) 31, or the spent stripper is divided into two parts, one part enters the regenerator 38 through the spent conveying pipe (I) 31, and the other part enters the main reaction zone 7 of the reactor through a spent conveying pipe (III) 51; the reactor 23 is internally provided with a catalyst fast separation device 12 and a reactor gas-solid separation facility 22. A regenerator gas-solid separation facility 37 is disposed within the regenerator 38. The regenerator 38 is provided with a regenerator inner heat-taking facility 33 and a regenerator outer heat-taking facility 42; the reactor 23 is provided with internal and external heat extraction means, preferably internal heat extraction means 6 in the main reaction zone 7.
An auxiliary reaction catalyst circulating pipe 8 is arranged between the main reaction zone 7 and the auxiliary reaction zone 10, the auxiliary reaction catalyst circulating pipe 8 is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle and lower parts of the auxiliary reaction zone 10, the outlet of the external circulating pipe is connected with the lower part of the main reaction zone 7, and the external circulating pipe can also be connected to different positions of the main reaction zone 7. A spent slide valve (I) 5 is arranged on the auxiliary reaction catalyst circulating pipe 8.
A catalyst circulation pipe 26 is arranged between the main reaction zone 7 and the catalyst collecting zone 13 of the reactor. When the catalyst circulation pipe 26 is an external circulation pipe, the inlet of the external circulation pipe is connected to the middle and lower portions of the catalyst collection zone 13 of the reactor, and the outlet thereof is connected to the main reaction zone 7. A spent cycle slide/plug valve 28 is provided on the catalyst circulation pipe 26. When the catalyst circulation pipe 26 is an internal circulation pipe, the internal circulation pipe is arranged at the middle part of the reactor 23 and is coaxially arranged with the internal circulation pipe, the inlet is connected with the catalyst collection zone 13 of the reactor, and the outlet is connected with the bottom of the main reaction zone 7. A spent slide valve (II)/plug valve 28 is provided on the catalyst circulation pipe 26 and is located at the bottom of the main reaction zone 7. The catalyst circulation pipe 26 may be one or more.
The interior of the reactor 23 is divided into a catalyst collecting zone 13, an auxiliary reaction zone 10 and a main reaction zone 7 from top to bottom. The top of the reactor 23 is provided with an oil gas collection chamber 21, the reaction oil gas 14 and the catalyst are primarily separated at the outlet of the dilute phase pipe 24 through the catalyst fast separation device 12, and are further separated through a reactor gas-solid separation facility 22 and then are introduced into the oil gas collection chamber 21. The regenerator 38 is internally divided into a regenerator dilute phase section 39, a regenerator transition section 40, and a regenerator char section 34. The regenerator char section 34 may be a turbulent bed or a fast bed or a combination of both. The regenerator dilute phase section 39 is provided with a regenerator gas-solid separation facility 37, the top of the regenerator dilute phase section is provided with a flue gas 35 outlet, the regeneration burning section 34 is provided with a main air distributor 44, and the bottom of the regenerator is provided with a main air 43 inlet.
Light hydrocarbon gas (C4-C10) 2 reaction raw materials enter a first feeding distributor 9 at the bottom of an auxiliary reaction zone 10 after being preheated, the light hydrocarbon gas (C4-C10) 2 in the auxiliary reaction zone 10 directly contacts with a high-temperature catalyst from a regenerator 38, the reaction is rapidly carried out under the action of the catalyst, reaction products enter a catalyst collecting zone 13 of the reactor, the reacted spent catalyst is sent to a main reaction zone 7 of the reactor through an auxiliary catalyst circulating pipe 8 or divided into two streams, one stream of spent catalyst is sent to the main reaction zone 7 of the reactor through the auxiliary catalyst circulating pipe 8, the other stream of spent catalyst enters a stripping device 54 of the auxiliary reaction spent stripper through a spent catalyst inlet pipe (II) 53, and the auxiliary reaction spent stripper 54 is internally provided with a stripping grid or a stripping baffle and a stripping medium distribution ring. Used for stripping reaction gas carried by spent catalyst, and the stripped spent catalyst enters the regenerator through a spent agent conveying pipe (IV) 56.
Preheating an oxygen-containing compound 3 mainly containing methanol or dimethyl ether, then feeding the oxygen-containing compound into a second feeding distributor 4 in a main reaction zone 7 of the reactor, reacting the oxygen-containing compound in the main reaction zone 7 with a spent catalyst from an auxiliary reaction zone 10, and rapidly reacting under the action of the catalyst; the reaction product is separated from the reaction oil gas by a catalyst fast separation device 12, most of the carried catalyst is removed by the reaction product of the auxiliary reaction zone 10 through a gas-solid separation facility 22 of the reactor, and the catalyst carried by the reaction product is removed by a reactor three-stage cyclone separator 19 and a reactor four-stage cyclone separator 17 and then is led out; the outlet gas 18 of the reactor fourth-stage cyclone separator and the outlet gas 20 of the reactor third-stage cyclone separator are combined together, and are sent to a rear quenching and water washing system after heat exchange. The reactor gas-solid separation facility 22 is a two-stage cyclone. The catalyst recovered by the reactor three-stage cyclone separator 19 and the reactor four-stage cyclone separator 17 enters a reactor three-stage recovery waste catalyst storage tank 16, and the waste catalyst 15 enters a waste catalyst tank 16 through a discharging pipeline.
The spent catalyst which loses activity after reaction enters a spent stripper 32 for stripping, and a stripping grid or a stripping baffle plate and a stripping medium distribution ring are arranged in the spent stripper 32. The device is used for stripping reaction gas carried by spent catalyst, the stripped spent catalyst enters the regenerator 38 through a spent agent conveying pipe (I) 31, or the stripped spent catalyst is divided into two parts, one part enters the regenerator 38 through the spent agent conveying pipe (I) 31, and the other part enters the reaction zone 7 of the main reactor through a spent agent conveying pipe (III) 51; the spent agent delivery pipe (I) 31 is provided with a spent sliding valve (II) 30, and the spent agent delivery pipe (III) 51 is provided with a spent sliding valve (III) 52 which are respectively used for controlling the circulation amount of the catalyst. After the spent catalyst is in countercurrent contact with the main air 43 in the regenerator 38 for burning, the regenerated catalyst is stripped by the regeneration stripper 45 for stripping flue gas carried by the regenerated catalyst, and the stripped regenerated catalyst enters the auxiliary reaction area 10 of the reactor through the regenerated catalyst conveying pipe 1 and enters the light hydrocarbon gas (C4-C10) 2 distributed in the feeding distributor I9 for reaction. The regenerated flue gas 35 is discharged from the top of the regenerator through a flue gas collection chamber 36 after most of the carried catalyst is removed by a regenerator gas-solid separation facility 37, and is sent to a waste heat boiler to recover heat after passing through a pressure reducing valve (if needed), a double-acting slide valve and a pressure reducing pore plate, and then is discharged to the atmosphere through a chimney.
According to the reaction requirement, the raw materials enter each reaction zone respectively, and the raw materials enter the auxiliary reaction zone 10 and can be light hydrocarbon gas (C4-C10), oxygen-containing compounds such as methanol, dimethyl ether and the like, or a mixture of the two. Light hydrocarbon gas (C4-C10) 2 is preferred. The gas entering the main reaction zone 7 can also be light hydrocarbon gas (C4-C10), oxygen-containing compounds such as methanol, dimethyl ether and the like, or a mixture of the two. The oxygen-containing compound 3 is preferably recommended.
The regenerated catalyst conveying pipe 1 can also be used as a riser reactor, light hydrocarbon gas (C4-C10) 2 can enter the riser reactor, the injection position of the light hydrocarbon gas (C4-C10) 2 can be arranged on a raw material feeding pipe, and the light hydrocarbon gas and the oxygen-containing compound are mixed and then enter an auxiliary reaction zone 10 or a main reaction zone 7; or can be arranged at the upper part, the middle part or/and the lower part of the riser reactor and can be divided into one or more strands of light hydrocarbon gas (C4-C10) 2. When the light hydrocarbon gas (C4-C10) 2 is not recycled in the regenerated catalyst conveying pipe 1, the regenerated catalyst conveying pipe is used for conveying the regenerated catalyst, and the conveying medium 47 is preferably steam.
Claims (20)
1. The method for producing the low-carbon olefin by using the oxygen-containing compound is characterized by comprising the following steps of:
1) preheating reaction raw materials in an auxiliary reaction zone, feeding the preheated reaction raw materials into the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone, directly contacting with a high-temperature catalyst from a regenerator, quickly reacting under the action of the catalyst, feeding reaction products into a catalyst collecting zone of a reactor, feeding part of a spent catalyst after reaction to a main reaction zone of the reactor through an auxiliary reaction catalyst circulating pipe, feeding part of the spent catalyst into a spent stripper through a spent catalyst inlet pipe for stripping, and feeding the stripped spent catalyst into the regenerator through a spent catalyst conveying pipe;
2) preheating reaction raw materials in the main reaction zone, feeding the preheated reaction raw materials into the main reaction zone of the reactor through a feeding distributor at the bottom of the main reaction zone, reacting the preheated reaction raw materials with a catalyst from the auxiliary reaction zone, separating a reaction product in the main reaction zone from a reaction oil gas through a gas-solid quick separation device, removing most of the carried catalyst together with the reaction product entering a catalyst collecting zone of the reactor in the step 1) through a gas-solid separation facility of the reactor, and leading out from the top of the reactor;
3) the catalyst in the auxiliary reaction zone of the reactor passes through an auxiliary reaction catalyst circulating pipe, and the spent catalyst in the catalyst collecting zone of the reactor passes through the catalyst circulating pipe and respectively enters the main reaction zone of the reactor to provide the catalyst required by the reaction for the main reaction zone of the reactor;
4) the spent catalyst which loses activity after reaction enters a spent stripper from a catalyst collecting region for steam stripping and then enters a regenerator through a spent conveying pipe; or one part enters the regenerator through the spent conveying pipe, and the other part enters the main reaction zone of the reactor;
5) after the catalyst to be regenerated is burnt in the regenerator, the regenerated catalyst is stripped by the regenerated stripper, and the stripped regenerated catalyst enters the catalyst collecting region through the regenerated catalyst conveying pipe.
2. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the auxiliary reaction zone is arranged in the catalyst collecting zone and is separated from the catalyst collecting zone and the main reaction zone by a partition plate, and the main reaction zone and the auxiliary reaction zone are communicated by an auxiliary reaction catalyst circulating pipe; the circulating pipe is provided with a slide valve or a plug valve for controlling the circulating amount of the catalyst.
3. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the main reaction zone is arranged below the catalyst collecting zone and is separated from the catalyst collecting zone by a dilute phase pipe, the top of the dilute phase pipe is provided with a catalyst fast-separating device, and the outlet of the catalyst fast-separating device is connected with the inlet of a gas-solid separation facility of the reactor; a catalyst circulating pipe is arranged between the main reaction area and the catalyst collecting area of the reactor, and a slide valve or a plug valve is arranged on the catalyst circulating pipe to control the circulating amount of the catalyst.
4. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the reaction raw material entering the auxiliary reaction zone and the reaction raw material entering the main reaction zone are C4～C10Light hydrocarbon gases and/or oxygenates.
5. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 4, characterized in that: the reaction raw material entering the auxiliary reaction zone is C4～C10A light hydrocarbon gas; the reaction raw material entering the reaction zone is an oxygen-containing compound.
6. The method for producing low-carbon olefin by using the oxygen-containing compound according to claim 5, is further technically characterized in that: one or more feed distributors are positioned in the lower portion of the main reaction zone and the oxygenate feedstock is injected into the lower portion of the main reaction zone in one or more streams.
7. The method for producing low-carbon olefin by using the oxygen-containing compound according to claim 5, is further technically characterized in that: one or more feeding distributors for light hydrocarbon gas (C) are arranged at the lower part of the auxiliary reaction zone4～C10) The raw material is injected into the lower part of the auxiliary reaction zone in one or more branches.
8. The method for producing lower olefins from the oxygen-containing compound according to claim 6 or 7, further characterized by: the feeding distributor is positioned at the lower part of each reaction area and is a distribution pipe or a distribution plate.
9. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the main reaction zone and the auxiliary reaction zone of the reactor are both fluidized bed reactors.
10. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the regenerated catalyst conveying pipe is used as a riser reactor, and light hydrocarbon gas is injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands.
11. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: and 4) a stripping grating or a stripping baffle plate and a stripping medium distribution ring device are arranged in the spent stripper.
12. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: a stripping grating or a stripping baffle and/or a heat taking facility and a stripping medium distribution circulator are arranged in the regeneration stripper in the step 5).
13. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: an inner heat collector and/or an outer heat collector are/is arranged in the main reaction zone of the reactor.
14. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 13, characterized in that: the inner heat collector is positioned in the main reaction zone of the reactor.
15. The process for producing lower olefins from oxygenates of claim 113, characterized by: the external heat collector is respectively communicated with the catalyst collecting region and the main reaction region of the reactor, and the spent catalyst in the catalyst collecting region of the reactor enters the external heat collector through the external heat collecting inlet pipe to be heated and then returns to the main reaction region of the reactor.
16. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: an internal heat collector and/or an external heat collector are arranged in the regenerator.
17. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the ratio of the cross-sectional area of the auxiliary reaction zone to the main reaction zone is in the range of 1-30%, one or more annular partition plates are arranged in the middle of the auxiliary reaction zone to partition the auxiliary reaction zone into two or more reaction bed layers with equal area.
18. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the reaction temperature of the auxiliary reaction zone of the reactor is in the range of 350-700 ℃; the linear speed of the auxiliary reaction zone is in the range of 0.1-1 m/s.
19. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the reaction temperature of the main reaction zone is within the range of 250-650 ℃; the reaction pressure is in the range of 0.05-3.0 MPaG, and the linear speed of the reactor is in the range of 0.1-5 m/s.
20. The method for producing low-carbon olefins by using the oxygen-containing compound according to claim 1, characterized in that: the regeneration temperature is within the range of 400-700 ℃, and the regeneration pressure is within the range of 0.1-3.0 MPaG.
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| CN113087584A (en) * | 2021-03-15 | 2021-07-09 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
| CN113354496A (en) * | 2021-03-15 | 2021-09-07 | 中石化洛阳工程有限公司 | Device for producing low-carbon olefin by using oxygen-containing compound |
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| CN101402538A (en) * | 2008-11-21 | 2009-04-08 | 中国石油化工股份有限公司 | Method for improving yield of light olefins |
| CN110818521A (en) * | 2018-08-07 | 2020-02-21 | 中石化广州工程有限公司 | Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound |
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| CN101402538A (en) * | 2008-11-21 | 2009-04-08 | 中国石油化工股份有限公司 | Method for improving yield of light olefins |
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| CN113087584A (en) * | 2021-03-15 | 2021-07-09 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
| CN113354496A (en) * | 2021-03-15 | 2021-09-07 | 中石化洛阳工程有限公司 | Device for producing low-carbon olefin by using oxygen-containing compound |
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