CN111875465B - Method for producing low-carbon olefin by oxygen-containing compound - Google Patents
Method for producing low-carbon olefin by oxygen-containing compound Download PDFInfo
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- CN111875465B CN111875465B CN202010661528.9A CN202010661528A CN111875465B CN 111875465 B CN111875465 B CN 111875465B CN 202010661528 A CN202010661528 A CN 202010661528A CN 111875465 B CN111875465 B CN 111875465B
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- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 82
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 82
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 71
- 239000001301 oxygen Substances 0.000 title claims abstract description 71
- 150000001875 compounds Chemical class 0.000 title claims abstract description 65
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 claims abstract description 247
- 239000003054 catalyst Substances 0.000 claims abstract description 217
- 239000002994 raw material Substances 0.000 claims abstract description 31
- 230000009471 action Effects 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 55
- 238000000926 separation method Methods 0.000 claims description 37
- 239000004215 Carbon black (E152) Substances 0.000 claims description 29
- 229930195733 hydrocarbon Natural products 0.000 claims description 29
- 150000002430 hydrocarbons Chemical class 0.000 claims description 29
- 239000007787 solid Substances 0.000 claims description 21
- 238000011069 regeneration method Methods 0.000 claims description 19
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 15
- 230000008929 regeneration Effects 0.000 claims description 15
- 239000007795 chemical reaction product Substances 0.000 claims description 11
- 238000009826 distribution Methods 0.000 claims description 10
- 238000005192 partition Methods 0.000 claims description 9
- 239000012495 reaction gas Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 34
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 49
- 239000003795 chemical substances by application Substances 0.000 description 26
- 150000001336 alkenes Chemical class 0.000 description 20
- 230000008569 process Effects 0.000 description 19
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000003546 flue gas Substances 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- 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
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 230000008021 deposition Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 238000005336 cracking Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- -1 ethylene, propylene, butadiene Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000003860 storage Methods 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
- 229940126214 compound 3 Drugs 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 150000002894 organic compounds Chemical class 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000000694 effects Effects 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
- 239000011148 porous material 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
- 238000004064 recycling Methods 0.000 description 2
- 238000011160 research 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
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 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
- 238000004939 coking Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 238000009776 industrial production Methods 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
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000001172 regenerating effect Effects 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
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for producing low-carbon olefin by oxygen-containing compound in the technical field of petrochemical industry, wherein after the reaction raw materials in an auxiliary reaction zone are preheated, the reaction raw materials enter the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone, are in direct contact with a high-temperature catalyst from a regenerator, and react rapidly under the action of the catalyst; the method is suitable for the characteristics of quick reaction, strong heat release, low catalyst-alcohol ratio, high product selectivity and the like of the process for preparing the low-carbon olefin from the oxygen-containing compound, so as to solve the problem of low-carbon olefin selectivity in the prior art, exert the advantage of the reaction to the greatest extent and improve the low-carbon olefin selectivity.
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 fundamental raw materials for petrochemical industry. The traditional ethylene and propylene preparation route is produced by naphtha pyrolysis, and has the disadvantage of being excessively dependent on petroleum. The preparation of low-carbon olefins (MTO) such as ethylene and propylene from Methanol is another process route for preparing olefins, and the development of the current process technology is mature. The industrialization of the MTO technology opens up a new process route for producing petrochemical basic raw materials by gasifying coal or natural gas, is beneficial to changing the product pattern of the traditional coal chemical industry, and is an effective way for realizing the extension and development of the coal chemical industry to the petrochemical industry.
Oxygen-containing organic compounds, typified by methanol or dimethyl ether, are typical oxygen-containing organic compounds, and are produced mainly from coal-based or natural gas-based synthesis gas. The technology for producing low-carbon olefin mainly containing ethylene and propylene by using oxygen-containing organic compound represented by methanol as raw material currently mainly comprises MTO and MTP technologies.
The reaction characteristic of the process for preparing the low-carbon olefin from the oxygen-containing compound is that the reaction is quick, the heat release is strong, the alcohol-to-agent ratio is low, 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, the catalyst in the high-temperature oil gas is removed, the temperature of the high-temperature oil gas is reduced, and the high-temperature oil gas is sent to an olefin separation system for separation. The oxygenate to olefins plant that has been put into production at present has the following common problems: the olefin selectivity is lower than that of a laboratory, and the unit consumption of methanol is increased.
In recent years, methods for improving the selectivity of low-carbon olefins have become a focus and focus of research by those skilled in the art. Extensive research and exploration has been conducted in terms of process flows, equipment structures, and the like.
A process for converting an oxygenate feedstock to light olefins is disclosed in the exxonmobil chemical patent company CN1102317238B, which invention relates to a process for converting a feedstock comprising oxygenates to a product comprising light olefins. In particular, the invention relates to the conversion of an oxygenate feedstock to products including light olefins with a silicoaluminophosphate catalyst in a reaction apparatus. More specifically, the present invention provides a means by which optimum coke levels can be determined and used to produce optimum or near-optimum yields of light olefins such as ethylene and propylene in an oxygenate to olefin system.
The world oil company CN1830926a discloses a catalyst cooler for an oxygenate conversion reactor. The invention includes contacting an oxygenate feedstream with a catalyst in a reactor and converting the oxygenate feedstream to the light olefins. The catalyst becomes spent when the reaction deposits clog the pores on the catalyst surface. A portion of the spent catalyst is regenerated in a regenerator and the portion is recycled back into contact with more of the oxygenate feed stream. A catalyst cooler coupled to the reactor can cool the spent catalyst circulated through the cooler before the spent catalyst is contacted with more of the oxygenate feed stream. In one embodiment, all 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 methanol-to-olefin process, which relates to a method for improving the yield of low-carbon olefin in a methanol-to-olefin process, and mainly solves the problem of low yield of low-carbon olefin in the prior art. The invention relates to 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) Feeding a raw material comprising methanol into a first rapid fluidized bed reaction zone, and contacting the raw material with a molecular sieve catalyst comprising silicoaluminophosphate to generate a product stream I comprising low-carbon olefin and simultaneously 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 comprising more than four carbon atoms, the generated product and the catalyst enter a second fast fluidized bed reaction zone and contact with the raw material comprising more than four carbon atoms and a second catalyst from the regenerator to generate a product material flow II comprising low carbon olefin and simultaneously form a pre-carbon-deposited catalyst; (3) The product material flow II is mixed with the product material flow I after gas-solid separation to enter a separation section, and the catalyst with pre-carbon deposition returns to the first rapid bed reaction zone.
Chinese patent CN103073377B discloses a method for preparing low-carbon olefins by catalytic conversion of an oxygenate, a method for generating low-carbon olefins by catalytic conversion of an oxygenate, introducing an oxygenate raw material into an internal circulation gas-solid fluidized bed reactor from the bottom, contacting with a cracking catalyst in a reaction zone to move upwards together, and carrying out alkylation and cracking reactions; 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 deposition catalyst is settled into a stripping zone, the adsorbed and entrained oil gas in the catalyst is stripped and removed, a part of the carbon deposition 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; and introducing the other part of the carbon deposition catalyst into a catalyst regenerator through a spent catalyst inclined tube for burning and regenerating, and returning the regenerated catalyst 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 from oxygen-containing compounds, and has the advantages of simplicity in operation and high low-carbon olefin yield.
In summary, the reaction characteristics of the process for preparing the low-carbon olefin from the oxygen-containing compound (methanol is typically adopted at present) are that the reaction is rapid, the heat release is strong, the catalyst alcohol is relatively low, 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, the catalyst is removed, the temperature is reduced, and the high-temperature oil gas is sent to a lower olefin separation system for separation. The cost of the SAPO catalyst used in the process 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 greatest extent during engineering design and equipment selection. For the reaction characteristics of the process, various types of device types are developed, and a fixed bed, a riser, a fast fluidized bed and the like are compared with a representative reactor type.
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 lower olefin selectivity still exists in the existing put-into-service device, and the invention specifically solves the problem.
Disclosure of Invention
The invention provides a method for producing low-carbon olefin by high-efficiency oxygen-containing compounds, which is suitable for the characteristics of quick reaction, strong heat release, relatively low catalyst-alcohol ratio, high product selectivity and the like of the process for preparing the low-carbon olefin by the oxygen-containing compounds, and aims to solve the problems of relatively low-carbon olefin selectivity, furthest playing the advantages of reaction, and improving the low-carbon olefin selectivity in the prior art.
In order to solve the technical problems, the invention adopts the following technical scheme:
the method for producing the low-carbon olefin by the oxygen-containing compound is characterized by comprising the following steps of:
1) After the reaction raw materials in the auxiliary reaction zone are preheated, the reaction raw materials enter the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone, are in direct contact with a high-temperature catalyst from a regenerator, and react rapidly under the action of the catalyst, the reaction products enter a catalyst collecting zone of the reactor, part of the reacted spent catalyst is sent to a main reaction zone of the reactor through an auxiliary reaction catalyst circulating pipe, and the part of the reacted spent catalyst enters a spent stripper for stripping through a spent catalyst inlet pipe and is used for stripping reaction gas carried by the spent catalyst, and the stripped spent catalyst enters the regenerator through a spent catalyst conveying pipe;
2) After the reaction raw materials in the main reaction zone are preheated, the reaction raw materials enter the main reaction zone of the reactor through a feeding distributor at the bottom of the main reaction zone, react with the catalyst from the auxiliary reaction zone, and after the reaction products in the main reaction zone are separated from the reaction oil gas through a gas-solid fast separation device, the reaction products entering the catalyst collecting zone of the reactor in the step 1) are removed most of the carried catalyst through a gas-solid separation facility of the reactor together, and the catalyst is led 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 a catalyst circulating pipe and respectively enters a 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 is deactivated after the reaction enters a spent stripper from a catalyst collecting area to be stripped and then enters a regenerator through a spent conveying pipe; or one part of the waste water enters the regenerator through a waiting conveying pipe, and the other part of the waste water enters a main reaction zone of the reactor;
5) After the spent catalyst in the regenerator is burnt, the regenerated catalyst is stripped by a regenerated stripper, and the stripped regenerated catalyst enters a catalyst collecting area through a regenerated catalyst conveying pipe.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the auxiliary reaction zone is arranged in the catalyst collecting zone, is separated from the catalyst collecting zone and the main reaction zone by a partition board, and is communicated with the main reaction zone by an auxiliary reaction catalyst circulating pipe; a slide valve or a plug valve is arranged on the 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 in that: the main reaction zone is arranged below the catalyst collecting zone and separated from the catalyst collecting zone through a dilute phase pipe, a catalyst rapid separation device is arranged at the top of the dilute phase pipe, and an outlet of the catalyst rapid separation device is connected with an inlet of a gas-solid separation facility of the reactor. A catalyst circulating pipe is arranged between the main reaction zone and the catalyst collecting zone of the reactor, and a slide valve or a plug valve is arranged on the 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 in that: the reaction raw material entering the auxiliary reaction zone can be light hydrocarbon gas (C 4 ～C 10 ) And/or an oxygen-containing compound, preferably a light hydrocarbon gas (C 4 ～C 10 ) The method comprises the steps of carrying out a first treatment on the surface of the The reaction raw material entering the main reaction zone can also be light hydrocarbon gas (C 4 ～C 10 ) And/or an oxygenate, preferably an oxygenate.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the oxygen-containing compound is mainly methanol or dimethyl ether, and the light hydrocarbon gas is C 4 ～C 10 And (3) gas.
The invention relates to a method for producing low-carbon olefin by high-efficiency oxygen-containing compounds, which is further technically characterized in that: one or more feeding distributors are arranged at the lower part of the main reaction zone, and the oxygen-containing compound raw material mainly comprising methanol or dimethyl ether 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 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 auxiliary reaction zone, and light hydrocarbon gas (C 4 ～C 10 ) The feedstock may be fed in one or more streams into the lower portion of the auxiliary reaction zone.
The invention relates to a method for producing low-carbon olefin by high-efficiency oxygen-containing compounds, which is further characterized in that: the feed 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 in that: the main reaction zone and the auxiliary reaction zone of the reactor are fluidized bed reactors. The secondary reaction zone is preferably a turbulent bed reactor and the primary reaction zone may be a rapid 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 in that: the catalyst in the auxiliary reaction zone of the reactor passes through an auxiliary reaction catalyst circulating pipe, the catalyst in the catalyst collecting zone of the reactor passes through a 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, and the catalyst is used for controlling the space velocity of the main reaction zone of the reactor so as to adjust the selectivity of olefin in the main reaction zone.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerated catalyst conveying pipe can also be used as a riser reactor, 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 in that: the raw material feeding pipe is provided with a light hydrocarbon gas injection port, and the light hydrocarbon gas singly or after being mixed with oxygen-containing compounds through the raw material feeding pipe respectively enters a main reaction zone and an auxiliary reaction zone of the reactor.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and 2) removing entrained catalyst from the reaction product in the step 2) through a three-stage cyclone separator and a four-stage cyclone separator of the reactor, leading out, exchanging heat, and delivering to a rear quenching and washing system. The catalyst recovered from the three-stage cyclone separator and the four-stage cyclone separator enters a waste reactor three-rotation recovered catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a catalyst unloading pipeline.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and step 4) a stripping grid or a stripping baffle plate and a stripping medium distribution ring are 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 in that: one end of the auxiliary reaction spent stripper in the step 1) is communicated with the lower part of an auxiliary reaction zone 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 in that: the auxiliary spent stripper in the step 1) is internally provided with a stripping grid or a stripping baffle and a stripping medium distribution ring.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and 5) a stripping grid or a stripping baffle and/or a heat-taking facility are arranged in the regeneration stripper, and a stripping medium distributor is also arranged.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and 5) removing most of carried catalyst from the flue gas after the catalyst is burnt in countercurrent contact with main wind through a two-stage cyclone separator, discharging the flue gas, and discharging the flue gas through a pressure reducing valve (if needed), a double-acting slide valve and a pressure reducing pore plate, and discharging the flue gas through a chimney after heat recovery of the waste heat boiler.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: an inner heat collector and/or an outer heat collector are arranged in a main reaction zone of the reactor, the inner heat collector is positioned in the main reaction zone of the reactor, the outer heat collector is respectively communicated with a catalyst collecting zone and the main reaction zone of the reactor, and a spent catalyst in the catalyst collecting zone of the reactor enters the outer heat collector through an outer heat collecting inlet pipe to collect heat, and then returns to the main reaction zone of the reactor.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: an inner heat collector and/or an outer heat collector are arranged in the regenerator.
The catalyst regeneration mode in the regenerator according to the present invention may be either incomplete regeneration or complete regeneration, preferably incomplete regeneration.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the auxiliary reaction zone may be located within the catalyst collection zone of the reactor and separated from the catalyst collection zone by a partition. The ratio of the cross-sectional areas of the auxiliary reaction zone and the main reaction zone is in the range of 1% -30%, preferably 3% -20%, and 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 beds with equal areas 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 in that: the reaction temperature of the auxiliary reaction zone of the reactor is in the range of 350-700 ℃, preferably in the range of 450-650 ℃; the reaction temperature of the main reaction zone is in the range of 250 to 650 ℃, preferably in the range of 350 to 600 ℃; the linear velocity of the reactor is in the range of 0.1-5 m/s, the main reaction zone is preferably in the range of 0.6-3 m/s, and the linear velocity of the auxiliary reaction zone is preferably in the range of 0.1-1 m/s.
The regeneration temperature is in the range of 400-700 ℃, preferably 450-650 ℃; the reaction pressure is in the range of 0.05 to 3.0MPaG, preferably in the range of 0.1 to 2.0 MPaG; the regeneration pressure is in the range of 0.1 to 3.0MPaG, preferably in the range of 0.1 to 2.0 MPaG.
The invention relates to a method for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the temperature of the three-stage cyclone separator of the reactor is 300-650 ℃, preferably 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 well solves the problem of lower selectivity of the low-carbon olefin in the prior art, plays the advantages of each reaction zone to the greatest extent, improves the selectivity of the low-carbon olefin, and can be used for industrial production of liquid products by the oxygen-containing compound, such as: MTO process (methanol to olefins process), MTP process (methanol to propylene process), MTA process (methanol to aromatics process), MTG process (methanol to gasoline process) and the like. In addition, the equipment disclosed by the invention has the advantages of simple structure, easiness in 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 treatment capacity of the device.
2) By adopting the method provided by the invention, the reactor adopts cascade reaction areas, so that the characteristics of different reaction areas can be utilized to effectively 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 subjected to pre-coking, the temperature of the catalyst entering the main reaction zone is reduced, and the activity of the outer surface of the catalyst is reduced. Because the cracking reaction of the auxiliary reaction zone is an endothermic reaction, the contact temperature of the reaction oil gas and the high-temperature regenerated catalyst in the main reactor is reduced, the occurrence of non-target reaction is reduced, and the selectivity of the low-carbon olefin is improved; the catalyst which adsorbs a small amount of coke continues to react exothermically with the oxygen-containing compound, reducing the effect of the induction period on the reaction, and is advantageous for improving the selectivity of the low-carbon olefin. The ethylene and propylene yield can be increased through the light hydrocarbon gas cracking reaction.
3) The method provided by the invention utilizes the characteristics of strong heat release of the conversion of the oxygenated chemicals into olefin and strong heat absorption of the conversion reaction of the light hydrocarbon gas, and the light hydrocarbon gas reaction is carried out in a high temperature zone, so that the conversion requirement of the reaction is met, and the coupling of heat can be realized, so that a complete system of mutual connection is formed.
4) By adopting the method provided by the invention, the strong heat release of the conversion of the oxygenated chemicals into olefin and the conversion reaction of the light hydrocarbon gas adopt the same catalyst, so that the mixing caused by using different catalysts is avoided; the two are respectively carried out in different reaction areas in a fluidization reaction mode, so that the advantages of the respective reactions are brought into full play, and the selectivity of a target product is improved; the products are similarly distributed, and a set of separation systems can be shared.
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 below with reference to the drawings and detailed description. But do not limit the scope of the invention.
Drawings
FIG. 1 is a schematic flow chart of a method for producing low-carbon olefin by using an oxygen-containing compound.
The reference numerals shown in the figures are: 1-regenerated catalyst conveying pipe, 2-light hydrocarbon gas, 3-methanol or dimethyl ether-based oxygen-containing compound, 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-baffle, 12-catalyst quick separating device, 13-reactor catalyst collecting zone, 14-reaction oil gas, 15-spent catalyst, 16-reactor triple-rotating recovered catalyst storage tank, 17-reactor four-stage cyclone separator, 18-reactor four-stage cyclone separator outlet gas, 19-reactor three-stage cyclone separator, 20-reactor three-stage cyclone outlet gas, 21-oil gas plenum, 22-reactor gas-solid separation facility, 23-reactor, 24-dilute phase pipe, 25-spent agent inlet pipe (one), 26-catalyst circulation pipe, 27-main reaction zone external heat collector inlet, 28-spent circulation slide valve/plug valve, 29-main reaction zone external heat collector, 30-spent slide valve (two), 31-spent agent delivery pipe (one), 32-spent stripper, 33-regenerator internal heat collector facility, 34-regenerator burnt section, 35-flue gas, 36-flue gas plenum, 37-regenerator gas-solid separation facility, 38-regenerator, 39-regenerator dilute phase section, 40-regenerator transition section, 41-regenerator external heat collector inlet and outlet, 42-regenerator external heat collector, 43-main air, 44-main air distributor, 45-regeneration stripper, 46-regeneration slide valve, 47-gas or raw material conveying, 48-spent agent inlet pipe (II), 49-spent agent conveying pipe (II), 50-reaction external heat collecting 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 FIG. 1, the method for producing the low-carbon olefin by the oxygen-containing compound comprises a reactor 23, a regenerator 38, a third-stage cyclone 19 of the reactor, a fourth-stage cyclone 17 of the reactor, a three-rotating recycled catalyst storage tank 16 of the reactor, a spent stripper 32, an auxiliary reaction spent stripper 54, a regeneration stripper 45, a main reaction zone external heat collector 29 and a regenerator external heat collector 42. The reactor 23 comprises a main reaction zone 7, an auxiliary reaction zone 10 and a catalyst collection zone 13, the reactor main reaction zone 7 being located below the catalyst collection zone 13, 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 rapid separation device 12, and the outlet of the catalyst rapid separation device 12 is connected with a reactor gas-solid separation facility 22. The catalyst collecting zone 13 is communicated with the main reaction zone 7 through a catalyst circulation pipe 26; the auxiliary reaction zone 10 is located within the main reactor catalyst collection zone 13, separated by a partition 11. One or more annular partition boards can be arranged in the middle of the auxiliary reaction zone to partition 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 zone 10 of the reactor, one end of the auxiliary reaction spent stripper 54 is communicated with the bottom of the auxiliary reaction zone 10 of the reactor through a spent agent inlet pipe (II) 53, the other end of the auxiliary reaction spent stripper is communicated with a regenerator 38 through a spent agent conveying pipe (IV) 56, and a spent slide valve (IV) 55 is arranged on the spent agent conveying pipe (IV) 56.
The light hydrocarbon gas (C4-C10) 2 reaction raw materials are preheated and then enter a first feeding distributor 9 at the bottom of the auxiliary reaction zone 10, the light hydrocarbon gas (C4-C10) 2 in the auxiliary reaction zone 10 is in direct contact with a high-temperature catalyst from a regenerator 38 to rapidly react 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 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 for stripping 54 through a spent catalyst inlet pipe (II) 53 to strip the reaction gas carried by the spent catalyst, and the stripped spent catalyst enters the regenerator through a spent catalyst conveying pipe (IV) 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 main reaction zone external heat collector 29 and a three-stage cyclone separator 19; the reactor 23 is provided with a main reaction zone external heat collector 29 connected to the reactor catalyst collecting zone 13 through a spent agent inlet pipe (II) 48 and connected to the main reaction zone 7 through a spent agent delivery pipe (II) 49. The regenerator 38 is in communication with a regeneration stripper 45, an off-regenerator extractor 42, a spent agent transfer line (one) 31, and a spent agent transfer line (four) 56. The regenerator 38 is provided with an external regenerator heat collector 42, and is connected to the regenerator 38 through an external regenerator heat collector inlet and outlet 41.
A first feeding distributor 9 is arranged at the bottom of the auxiliary reaction zone 10, a second feeding distributor 4 is arranged at the bottom of the main reaction zone 7, and a raw material feeding pipe is led 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 area 13 of the reactor through a spent agent inlet pipe (I) 25, and the other end of the spent stripper is communicated with a regenerator 38 through a spent agent conveying pipe (I) 31, or is divided into two parts, wherein one part enters the regenerator 38 through the spent conveying pipe (I) 31, and the other part enters the main reaction area 7 of the reactor through a spent conveying pipe (III) 51; the reactor 23 is internally provided with a catalyst rapid separation device 12 and a reactor gas-solid separation facility 22. The regenerator 38 is internally provided with a regenerator gas-solid separation facility 37. The regenerator 38 is provided with an in-regenerator heat extraction facility 33 and an out-regenerator heat extractor 42; the reactor 23 is provided with internal and external heat extraction means, preferably with 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 outer circulating pipe, the inlet of the outer circulating pipe is connected with the middle and lower parts of the auxiliary reaction zone 10, the outlet is connected with the lower part of the main reaction zone 7, and the auxiliary reaction catalyst circulating pipe can also be connected to different positions of the main reaction zone 7. A spent slide valve (one) 5 is provided on the auxiliary reaction catalyst circulation pipe 8.
A catalyst circulation pipe 26 is arranged between the main reaction zone 7 and the catalyst collection zone 13 of the reactor. When the catalyst circulation pipe 26 is an outer circulation pipe, the inlet of the outer circulation pipe is connected to the middle and lower parts of the catalyst collecting zone 13 of the reactor, and the outlet is connected to the main reaction zone 7. A spent circulation spool valve 28 is provided on the catalyst circulation tube 26. When the catalyst circulation pipe 26 is an inner circulation pipe, the inner circulation pipe is arranged in the middle of the reactor 23 and is coaxially arranged with the reactor, the inlet is connected with the catalyst collecting area 13 of the reactor, and the outlet is connected with the bottom of the main reaction area 7. A spent spool valve 28 is provided on the catalyst circulation tube 26 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 collecting chamber 21, the reaction oil gas 14 and the catalyst are subjected to preliminary separation at the outlet of the dilute phase pipe 24 through the catalyst rapid separation device 12, and are further separated through a reactor gas-solid separation facility 22 and then are introduced into the oil gas collecting chamber 21. The interior of the regenerator 38 is 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 rapid bed or a combination of both. The regenerator dilute phase section 39 is provided with a regenerator gas-solid separation facility 37, the top is provided with a flue gas 35 outlet, the regenerated coke 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.
The light hydrocarbon gas (C4-C10) 2 is preheated and enters a first feeding distributor 9 at the bottom of the auxiliary reaction zone 10, the light hydrocarbon gas (C4-C10) 2 in the auxiliary reaction zone 10 is in direct contact with a high-temperature catalyst from a regenerator 38 to rapidly react 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 catalyst circulating pipe 8, or is split into two parts, one spent catalyst is sent to the main reaction zone 7 of the reactor through the auxiliary catalyst circulating pipe 8, the other spent catalyst enters an auxiliary reaction spent stripper for stripping 54 through an auxiliary catalyst inlet pipe (II) 53, and a stripping grid or a stripping baffle plate and a stripping medium distributing ring are arranged in the auxiliary reaction spent stripper 54. For stripping the reaction gas carried by the spent catalyst, and the stripped spent catalyst enters the regenerator through a spent agent delivery pipe (four) 56.
After preheating, the oxygen-containing compound 3 mainly comprising methanol or dimethyl ether enters a second feeding distributor 4 in a main reaction zone 7 of the reactor, the oxygen-containing compound in the main reaction zone 7 reacts with a spent catalyst from an auxiliary reaction zone 10, and the reaction is rapidly carried out under the action of the catalyst; the reaction product is subjected to catalyst and reaction oil-gas separation through a catalyst rapid separation device 12, and is discharged after most of carried catalyst is removed through a gas-solid separation facility 22 of the reactor together with the reaction product of the auxiliary reaction zone 10, and the carried catalyst is removed through a three-stage cyclone separator 19 of the reactor and a four-stage cyclone separator 17 of the reactor; the outlet gas 18 of the four-stage cyclone separator of the reactor and the outlet gas 20 of the three-stage cyclone separator of the reactor are combined together, and sent to a rear quenching and washing system after heat exchange. The reactor gas-solid separation facility 22 is a two-stage cyclone. The catalyst recovered from the three-stage cyclone 19 and the four-stage cyclone 17 enters the three-cyclone recovery spent catalyst storage tank 16, and the spent catalyst 15 enters the spent catalyst tank 16 through a catalyst unloading pipeline.
The spent catalyst which is deactivated after the reaction enters a spent stripper 32 for stripping, wherein a stripping grid or a stripping baffle plate and a stripping medium distribution ring are arranged in the spent stripper 32. The catalyst is used for stripping reaction gas carried by the spent catalyst, the stripped spent catalyst enters a regenerator 38 through a spent agent conveying pipe (I) 31, or is divided into two parts, one part enters the regenerator 38 through the spent agent conveying pipe (I) 31, and the other part enters a reaction zone 7 of the main reactor through a spent agent conveying pipe (III) 51; the spent slide valve (two) 30 is arranged on the spent agent delivery pipe (one) 31, and the spent slide valve (three) 52 is arranged on the spent agent delivery pipe (three) 51 and used for controlling the catalyst circulation amount respectively. After the spent catalyst is burnt in countercurrent contact with the main wind 43 in the regenerator 38, the regenerated catalyst is stripped by a regenerated stripper 45 and is used for stripping the flue gas carried by the regenerated catalyst, and the stripped regenerated catalyst enters the auxiliary reaction zone 10 of the reactor and enters the light hydrocarbon gas (C4-C10) 2 distributed by the first 9 of the feeding distributor for reaction through the regenerated catalyst conveying pipe 1. The regenerated flue gas 35 is discharged from the top of the regenerator through a flue gas collecting chamber 36 after most of 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 orifice plate, and then is discharged to exhaust gas by a chimney.
According to the reaction requirements, raw materials respectively enter each reaction zone, 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 gases (C4 to C10) 2 are preferably used. The main reaction zone 7 may be charged with light hydrocarbon gas (C4-C10), oxygen-containing compound such as methanol and dimethyl ether, or a mixture of both. Preferably, the oxygen-containing compound 3 is 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, and the injection position of the light hydrocarbon gas (C4-C10) 2 can be arranged on a raw material feeding pipe, and can be mixed with oxygen-containing compound 3 and then enter an auxiliary reaction zone 10 or a main reaction zone 7; or may be arranged in the upper part, middle part or/and lower part of the riser reactor, and may be divided into one or more light hydrocarbon gases (C4-C10) 2. When the light hydrocarbon gas (C4 to C10) 2 is not recycled in the regenerated catalyst transfer pipe 1, the regenerated catalyst transfer pipe is used for transferring the regenerated catalyst, and the transfer medium 47 is preferably steam.
Claims (17)
1. The method for producing the low-carbon olefin by the oxygen-containing compound is characterized by comprising the following steps of:
1) After the reaction raw materials in the auxiliary reaction zone are preheated, the reaction raw materials enter the auxiliary reaction zone through a feeding distributor at the bottom of the auxiliary reaction zone, are in direct contact with a high-temperature catalyst from a regenerator, and react rapidly under the action of the catalyst, the reaction products enter a catalyst collecting zone of the reactor, part of the reacted spent catalyst is sent to a main reaction zone of the reactor through an auxiliary reaction catalyst circulating pipe, and the part of the reacted spent catalyst enters a spent stripper for stripping through a spent catalyst inlet pipe and is used for stripping reaction gas carried by the spent catalyst, and the stripped spent catalyst enters the regenerator through a spent catalyst conveying pipe; the reaction raw materials entering the auxiliary reaction zone are C4-C10 light hydrocarbon gases; the reaction raw material entering the main reaction zone is an oxygen-containing compound;
2) After the reaction raw materials in the main reaction zone are preheated, the reaction raw materials enter the main reaction zone of the reactor through a feeding distributor at the bottom of the main reaction zone, react with the catalyst from the auxiliary reaction zone, and after the reaction products in the main reaction zone are separated from the reaction oil gas through a gas-solid fast separation device, the reaction products entering the catalyst collecting zone of the reactor in the step 1) are removed most of the carried catalyst through a gas-solid separation facility of the reactor together, and the catalyst is led 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 a catalyst circulating pipe and respectively enters a 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 is deactivated after the reaction enters a spent stripper from a catalyst collecting area to be stripped and then enters a regenerator through a spent conveying pipe; or one part of the waste water enters the regenerator through a waiting conveying pipe, and the other part of the waste water enters a main reaction zone of the reactor;
5) After the spent catalyst in the regenerator is burnt, the regenerated catalyst is stripped by a regenerated stripper, and the stripped regenerated catalyst enters a catalyst collecting area through a regenerated catalyst conveying pipe.
2. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the auxiliary reaction zone is arranged in the catalyst collecting zone, is separated from the catalyst collecting zone and the main reaction zone by a partition board, and is communicated with the main reaction zone by an auxiliary reaction catalyst circulating pipe; a slide valve or a plug valve is arranged on the circulating pipe to control the circulating amount of the catalyst.
3. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the main reaction zone is arranged below the catalyst collecting zone and is separated from the catalyst collecting zone through a dilute phase pipe, a catalyst rapid separation device is arranged at the top of the dilute phase pipe, and an outlet of the catalyst rapid separation device is connected with an inlet of a gas-solid separation facility of the reactor; a catalyst circulating pipe is arranged between the main reaction zone and the catalyst collecting zone of the reactor, and a slide valve or a plug valve is arranged on the circulating pipe to control the circulating amount of the catalyst.
4. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: one or more feed distributors are disposed 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.
5. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: one or more feed distributors are arranged at the lower part of the auxiliary reaction zone, C 4 ～C 10 The light hydrocarbon gas material is injected into the lower part of the auxiliary reaction zone in one or more strands.
6. The method for producing a low-carbon olefin from an oxygen-containing compound according to claim 4 or 5, characterized in that: the feeding distributor is positioned at the lower part of each reaction zone and is a distribution pipe or a distribution plate.
7. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the main reaction zone and the auxiliary reaction zone of the reactor are fluidized bed reactors.
8. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: 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.
9. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: and step 4) a stripping grid or a stripping baffle plate and a stripping medium distribution circulator are arranged in the spent stripper.
10. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: and 5) a stripping grid or a stripping baffle and/or a heat-taking facility are arranged in the regeneration stripper, and a stripping medium distributor is also arranged.
11. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: an inner heat collector and/or an outer heat collector are arranged in a main reaction zone of the reactor.
12. The method for producing low-carbon olefin from oxygen-containing compound according to claim 11, characterized in that: the external heat collector is respectively communicated with the catalyst collecting area and the main reaction area of the reactor, and the spent catalyst in the catalyst collecting area of the reactor enters the external heat collector through the external heat collecting inlet pipe to collect heat and then returns to the main reaction area of the reactor.
13. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: an inner heat collector and/or an outer heat collector are arranged in the regenerator.
14. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the ratio of the cross sectional area of the auxiliary reaction zone to that of the main reaction zone is within the range of 1-30%, and one or more annular partition plates are arranged in the middle of the auxiliary reaction zone to divide the auxiliary reaction zone into two or more reaction beds with equal area.
15. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the reaction temperature of the auxiliary reaction zone of the reactor is in the range of 350-700 ℃; the linear velocity of the auxiliary reaction zone is in the range of 0.1-1 m/s.
16. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the reaction temperature of the main reaction zone is in 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.
17. The method for producing low-carbon olefin from the oxygen-containing compound according to claim 1, wherein: the regeneration temperature is in the range of 400-700 ℃ and the regeneration pressure is in the range of 0.1-3.0 MPaG.
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| 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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| 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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