CN111807916A - Device of low carbon olefin of high efficiency oxygen compound production - Google Patents
Device of low carbon olefin of high efficiency oxygen compound production Download PDFInfo
- Publication number
- CN111807916A CN111807916A CN202010662029.1A CN202010662029A CN111807916A CN 111807916 A CN111807916 A CN 111807916A CN 202010662029 A CN202010662029 A CN 202010662029A CN 111807916 A CN111807916 A CN 111807916A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- reactor
- reaction zone
- oxygen
- containing compounds
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 59
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 9
- -1 carbon olefin Chemical class 0.000 title claims description 9
- 150000002927 oxygen compounds Chemical class 0.000 title claims description 4
- 238000006243 chemical reaction Methods 0.000 claims abstract description 204
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 82
- 239000001301 oxygen Substances 0.000 claims abstract description 82
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 81
- 150000001875 compounds Chemical class 0.000 claims abstract description 77
- 239000003054 catalyst Substances 0.000 claims description 173
- 239000007789 gas Substances 0.000 claims description 60
- 150000001336 alkenes Chemical class 0.000 claims description 40
- 238000000926 separation method Methods 0.000 claims description 39
- 239000004215 Carbon black (E152) Substances 0.000 claims description 34
- 229930195733 hydrocarbon Natural products 0.000 claims description 34
- 150000002430 hydrocarbons Chemical class 0.000 claims description 34
- 239000003795 chemical substances by application Substances 0.000 claims description 25
- 239000007787 solid Substances 0.000 claims description 24
- 239000002994 raw material Substances 0.000 claims description 22
- 238000011069 regeneration method Methods 0.000 claims description 19
- 230000008929 regeneration Effects 0.000 claims description 15
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 14
- 238000009826 distribution Methods 0.000 claims description 13
- 238000005192 partition Methods 0.000 claims description 11
- 239000003546 flue gas Substances 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 230000007704 transition Effects 0.000 claims description 4
- 238000004939 coking Methods 0.000 claims description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 66
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 24
- 238000000034 method Methods 0.000 description 16
- 239000012071 phase Substances 0.000 description 15
- 239000000047 product Substances 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 238000000605 extraction Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- 239000007795 chemical reaction product Substances 0.000 description 4
- 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
- 239000002699 waste material Substances 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
- 238000002156 mixing Methods 0.000 description 3
- 150000002894 organic compounds Chemical class 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
- 230000009471 action Effects 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 229940126214 compound 3 Drugs 0.000 description 2
- 238000001816 cooling Methods 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
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 241000269350 Anura Species 0.000 description 1
- 235000004035 Cryptotaenia japonica Nutrition 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
- 102000007641 Trefoil Factors Human genes 0.000 description 1
- 235000015724 Trifolium pratense Nutrition 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
- 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
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000002349 favourable effect Effects 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
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000012495 reaction gas 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
- 238000012546 transfer Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Images
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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
-
- 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 device for producing low-carbon olefin by using an efficient oxygen-containing compound, which belongs to the technical field of petrochemical industry, and is suitable for the characteristics of quick reaction, strong heat release, lower alcohol-to-alcohol ratio, high product selectivity and the like of a process for preparing low-carbon olefin by using the oxygen-containing compound, so that the problem of low-carbon olefin selectivity in the prior art is solved, the advantages of the reaction can be exerted to the greatest extent, and the problem of low-carbon olefin selectivity is improved.
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, 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.
Chinese patent CN102190548B discloses a method for increasing the yield of low-carbon olefins in a process for preparing olefins 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, 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 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-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 high-efficiency device for producing low-carbon olefin by using an oxygen-containing compound, which is suitable for the characteristics of rapid reaction, strong heat release, low alcohol-to-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, capability of exerting the advantages of the reaction to the greatest extent and improvement of 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 utility model provides a device of high-efficient oxygen compound production low carbon olefin, mainly includes reactor, regenerator, waits to give birth to stripper and regeneration stripper, its characterized in that: the reactor comprises a main reaction zone, an auxiliary reaction zone and a catalyst collecting zone, wherein the main reaction zone is positioned below the catalyst collecting zone, the auxiliary reaction zone is arranged in the catalyst collecting zone and is separated from the main reaction zone by a partition plate, and the main reaction zone and the auxiliary reaction zone are communicated through a catalyst circulating pipe and an auxiliary reaction catalyst circulating pipe; the regenerator is connected with a regenerated catalyst conveying pipe through a regenerated stripper and a regenerated slide valve, and the regenerated catalyst conveying pipe extends into the upper part of the auxiliary reaction zone; the spent stripper is respectively communicated with the catalyst collecting region of the reactor and the bottom of the regenerator.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the reactor is internally divided into a catalyst collecting region, an auxiliary reaction region and a main reaction region from top to bottom, the auxiliary reaction region is arranged in the catalyst collecting region and is separated from the catalyst collecting region through a partition plate, the auxiliary reaction region and the main reaction region are of an integral structure and are separated from the main reaction region through a dilute phase pipe, and a catalyst fast-separating device is arranged at the top of the dilute phase pipe.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the reactor catalyst collecting area is provided with a catalyst fast separation device and a reactor gas-solid separation facility, the top of the catalyst collecting area is provided with an oil-gas collecting chamber, and oil gas is introduced into the oil-gas collecting chamber. The catalyst quick separation device can be selected from one of an umbrella cap type, an inverted L type, a T type and a trefoil type, and can also be connected with a primary cyclone separator of a gas-solid separation facility of the reactor.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the reactor gas-solid separation facility is a one-stage or/and two-stage cyclone separator, and the one-stage or/and two-stage cyclone separator is introduced into the oil gas collection chamber.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further technically characterized in that: the main reaction zone is provided with an inner heat collector and/or an outer heat collector, the inner heat collector is positioned in the main reaction zone of the reactor, and the outer heat collector is respectively communicated with a catalyst collecting zone and the main reaction zone of the reactor.
The invention relates to a high-efficiency device for producing low-carbon olefin by using 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 oxygen-containing compounds such as methanol and dimethyl ether and light hydrocarbon gas (C) are arranged4～C10) The feed may be injected into the lower portion of the main reaction zone in one or more separate streams.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further technically characterized in that: one or more feeding distributors are arranged at the lower part of the auxiliary reaction zone, and oxygen-containing compound raw materials such as methanol, dimethyl ether and the like and light hydrocarbon gas (C) are arranged4～C10) The raw materials are distributed by means of respective feed distributors.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further 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, preferably a distribution pipe.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerated catalyst transfer line may be used as a riser reactor. When light hydrocarbon gas (C) is recycled4～C10) In the process, the regenerated catalyst conveying pipe can be used as a riser reactor, and light hydrocarbon gas (C) is preferably fed into the riser reactor4～C10) Light hydrocarbon gas (C)4～C10) Can be injected into the upper, middle or lower part of the riser reactor in one or more portions. When light hydrocarbon gas (C) is not recycled4～C10) The regenerated catalyst conveying pipe can be used for conveying regenerated catalyst and conveying mediumSteam is preferred.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further technically characterized in that: the auxiliary reaction catalyst circulating pipe is a catalyst conveying pipe and is used for replenishing fresh catalyst to the main reaction area of the reactor, an inlet of the auxiliary reaction catalyst circulating pipe is connected with the middle part or the lower part of the auxiliary reaction area of the reactor, and an outlet of the auxiliary reaction catalyst circulating pipe is connected with the lower part of the main reaction area of the reactor or can be connected to different positions of the lower part of the main reaction area of the reactor. A slide valve is arranged on the auxiliary reaction catalyst circulating pipe.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the catalyst circulating pipe is arranged between the catalyst collecting area and the main reaction area, the catalyst circulating pipe is a catalyst conveying pipe and is used for controlling the airspeed of the main reaction area of the reactor so as to adjust the selectivity of olefin in the main reaction area, the inlet of the catalyst circulating pipe is connected with the lower part of the catalyst collecting area of the reactor, the outlet of the catalyst circulating pipe is connected with the middle part and the lower part of the main reaction area of the reactor, and the catalyst circulating pipe is provided with a slide valve. The catalyst circulating pipe can also be an internal circulating pipe, the internal circulating pipe is arranged in the middle of the reaction zone of the main reactor and is coaxially arranged with the internal circulating pipe, the inlet is connected with the catalyst collecting zone of the reactor, the outlet is connected with the bottom of the main reaction zone of the reactor, and the catalyst circulating pipe is provided with a plug valve and is positioned at the bottom of the main reaction zone of the reactor. The catalyst circulating pipe can be one or more.
The invention relates to a high-efficiency device 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 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. According to the reaction requirement, the reaction raw materials are respectively fed into all reaction zones, and fed into auxiliary reaction zone and can be light hydrocarbon gas (C)4～C10) Oxygen-containing compounds such as methanol and dimethyl ether, or mixtures thereof; preference for light hydrocarbon gases (C)4～C10). Light hydrocarbon gas (C) can also enter the main reaction zone4～C10) Oxygen-containing compounds such as methanol and dimethyl ether, orThey are mixtures thereof, with preference being given to oxygen-containing compounds.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: 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 high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: one end of the spent stripper is communicated with the lower part of a catalyst collecting region of the reactor through a spent agent inlet pipe, and the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe; or the other end is respectively communicated with the regenerator and the bottom of the main reaction zone of the reactor through a spent agent conveying pipe. A slide valve is arranged on the spent agent conveying pipe.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distribution ring.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: a third cyclone, preferably external, is provided outside or inside the reactor. Is coaxial with the reactor when being arranged inside the reactor; the reactor three-stage cyclone separator can be vertical or horizontal, and is preferably horizontal.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: a reactor fourth-stage cyclone separator is arranged outside the reactor, one end of the reactor fourth-stage cyclone separator is communicated with the reactor third-stage cyclone separator, and the other end of the reactor fourth-stage cyclone separator is communicated with a reactor third-stage recovery catalyst storage tank.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator. The regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section. The regenerator char section may be a turbulent bed or a fast bed or a combination of both.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the dilute phase section of the regenerator is provided with a gas-solid separation facility, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet.
The main wind distributor can be a distribution pipe and/or a distribution plate, and is preferably a distribution pipe. Not only the main wind is evenly distributed and is wear-resistant, but also the service life is long.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the gas-solid separation device in the regenerator is preferably a cyclone separator, and the cyclone separator is 1-3 grade.
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 high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: an internal heat extraction facility and/or an external heat extraction facility are/is arranged in the regenerator.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerated stripper has the double functions of stripping and cooling the regenerated catalyst, and is internally provided with a stripping grid or a stripping baffle, a stripping medium distribution ring and a heat extraction tube bundle.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: arranging an internal heat taking facility and/or an external heat taking facility in the main reaction zone, wherein the internal heat taking medium can be one or more of an oxygen-containing compound raw material, light hydrocarbon, water, an inert medium and heat conducting oil, preferably the light hydrocarbon and the oxygen-containing compound raw material are used as heat taking media, the oxygen-containing compound raw material is preferably a liquid phase raw material, and the temperature can be within the range of 25-200 ℃, preferably within the range of 25-150 ℃; the internal heat extraction facility is arranged in the main reaction zone of the high-efficiency reactor and above the feeding distributor of the reaction zone. And an external heat taking facility is arranged in the main reaction zone, and the heat taking medium is preferably deoxygenated water so as to generate steam with different grades.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: an external heat-taking device is arranged in the regenerator, and the external heat-taking device can be selected from one of an up-flow type, a down-flow type and a back-mixing type according to the flowing state and the flowing mode of the catalyst, and is preferably a back-mixing type external heat-taking device. The heat-taking medium is preferably deoxygenated water to generate different grades of steam.
The invention relates to a high-efficiency device for producing low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the reactor is a multi-stage series reactor, which comprises a main reaction zone and an auxiliary reaction zone, and can be a fast bed reactor or a turbulent bed. Raw materials are respectively fed into each reaction zone according to the reaction requirements, and the raw materials fed into the auxiliary reaction zone can be light hydrocarbon gas (C)4～C10) And oxygen-containing compounds such as methanol and dimethyl ether, or a mixture of both. Preference for light hydrocarbon gases (C)4～C10). The oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or the mixture of the light hydrocarbon gas, the methanol, the dimethyl ether and the like can also enter the main reaction zone. Oxygen-containing compounds are preferred.
The device for producing the low-carbon olefin by the high-efficiency oxygen-containing compound, disclosed by the invention, 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 selectivity, and can be used for industrial production of liquid products produced 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 device 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 device 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) By adopting the device provided by the invention, the characteristics of strong heat release of the conversion of the oxygen-containing compound into the olefin and strong heat absorption of the conversion reaction of the light hydrocarbon gas are utilized, the light hydrocarbon gas reaction is carried out in a high-temperature area, the conversion requirement of the reaction is met, the heat coupling can be realized, and the mutual connection complete system is formed by coupling.
4) By adopting the device 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 device provided by the invention, the auxiliary reaction zone and the main reaction zone form the high-efficiency reactor, thereby saving the investment and the occupied area of the device.
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 diagram of an efficient apparatus for producing low-carbon olefins from oxygenates according to the 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) and 52-spent slide valve (III).
Detailed Description
The invention is described in further detail below with reference to the figures and the specific examples, which do not limit the scope of the invention as claimed.
As shown in the attached figure 1, the device for producing the low-carbon olefin by the high-efficiency 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, a regenerated 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.
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, 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 raw material feeding is 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 cycle slide/plug valve 28 is provided on the catalyst recycle line 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 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 is directly contacted 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, and the reacted catalyst to be generated is sent to a main reaction zone 7 of the reactor through an auxiliary catalyst circulating pipe 8. 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 and is burnt, the regenerated catalyst is stripped by the regeneration stripper 45 and is used 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 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 (21)
1. The utility model provides a device of high-efficient oxygen compound production low carbon olefin, mainly includes reactor, regenerator, waits to give birth to stripper and regeneration stripper, its characterized in that: the reactor comprises a main reaction zone, an auxiliary reaction zone and a catalyst collecting zone, wherein the main reaction zone is positioned below the catalyst collecting zone, 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 through an auxiliary reaction catalyst circulating pipe; the main reaction zone and the catalyst collecting zone are communicated through a catalyst circulating pipe, the regenerator is connected with a regenerated catalyst conveying pipe through a regenerated stripper and a regenerated slide valve, and the regenerated catalyst conveying pipe extends into the upper part of the auxiliary reaction zone; the spent stripper is respectively communicated with the catalyst collecting region of the reactor and the bottom of the regenerator.
2. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the reactor is internally divided into a catalyst collecting region, an auxiliary reaction region and a main reaction region from top to bottom, the main reaction region is arranged below the catalyst collecting region, a dilute phase pipe and a reactor gas-solid separation facility are further arranged in the catalyst collecting region, the main reaction region and the catalyst collecting region are separated through the dilute phase pipe, a catalyst fast separation device is arranged at the top of the dilute phase pipe, and an outlet of the catalyst fast separation device is connected with an inlet of the reactor gas-solid separation facility.
3. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: and an oil-gas collection chamber is arranged at the top of the catalyst collection area, and oil gas is introduced into the oil-gas collection chamber.
4. The apparatus for producing light olefins from oxygen-containing compounds according to claim 2, wherein: the catalyst quick separation device is selected from one of an umbrella cap type, an inverted L type, a T type and a trilobal type.
5. The apparatus for producing light olefins from oxygen-containing compounds according to claim 2, wherein: the gas-solid separation facility of the reactor is a one-stage or/and two-stage cyclone separator.
6. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: and a slide valve or a plug valve is arranged on the auxiliary reaction catalyst circulating pipe and the catalyst circulating pipe to control the circulating amount of the catalyst.
7. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the main reaction zone is provided with an inner heat collector and/or an outer heat collector, the inner heat collector is positioned in the main reaction zone of the reactor, and the outer heat collector is respectively communicated with a catalyst collecting zone and the main reaction zone of the reactor.
8. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: one or more feeding distributors are arranged at the lower part of the main reaction zone and the lower part of the auxiliary reaction zone, and raw materials are injected into the lower parts of the main reaction zone and the auxiliary reaction zone in one or more strands.
9. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the feeding distributor is a distribution pipe or a distribution plate.
10. The apparatus for producing light olefins from oxygen-containing compounds 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.
11. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the inlet of the auxiliary reaction catalyst circulating pipe is connected with the middle part or the lower part of the auxiliary reaction area of the reactor, and the outlet of the auxiliary reaction catalyst circulating pipe is connected with the lower part of the main reaction area of the reactor.
12. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the catalyst circulating pipe is an external circulating pipe, an inlet of the catalyst circulating pipe is connected with the lower part of a catalyst collecting area of the reactor, an outlet of the catalyst circulating pipe is connected with the middle part and the lower part of a main reaction area of the reactor, and a slide valve is arranged on the catalyst circulating pipe.
13. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the catalyst circulating pipe is an internal circulating pipe, the internal circulating pipe is arranged in the middle of the reaction zone of the main reactor and is coaxially arranged with the internal circulating pipe, an inlet is connected with the catalyst collecting zone of the reactor, an outlet is connected with the bottom of the main reaction zone of the reactor, and a plug valve is arranged on the catalyst circulating pipe.
14. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the main reaction zone and the auxiliary reaction zone of the reactor are both fluidized bed reactors.
15. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the auxiliary reaction zone is a turbulent bed reactor, and the main reaction zone is a fast bed reactor or a turbulent bed reactor.
16. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the ratio of the cross sectional area of the auxiliary reaction zone to the main reaction zone is 1-30%, and 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 areas.
17. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: one end of the spent stripper is communicated with the lower part of a catalyst collecting region of the reactor through a spent agent inlet pipe, and the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe; or the other end is respectively communicated with the regenerator and the bottom of the main reaction zone of the reactor through a spent agent conveying pipe; a slide valve is arranged on the spent agent conveying pipe.
18. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distribution ring.
19. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: and a third-stage cyclone separator is arranged outside or inside the reactor, and a fourth-stage cyclone separator is arranged outside the reactor.
20. The apparatus for producing light olefins from oxygen-containing compounds according to claim 1, wherein: the regenerator is a fluidized bed regenerator, and the regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section.
21. The apparatus for producing light olefins from oxygenates according to claim 20, characterized in that: the dilute phase section of the regenerator is provided with a gas-solid separation facility, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010662029.1A CN111807916B (en) | 2020-07-10 | 2020-07-10 | Device for producing low-carbon olefin by efficient oxygen-containing compound |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010662029.1A CN111807916B (en) | 2020-07-10 | 2020-07-10 | Device for producing low-carbon olefin by efficient oxygen-containing compound |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111807916A true CN111807916A (en) | 2020-10-23 |
| CN111807916B CN111807916B (en) | 2023-11-03 |
Family
ID=72841740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010662029.1A Active CN111807916B (en) | 2020-07-10 | 2020-07-10 | Device for producing low-carbon olefin by efficient oxygen-containing compound |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111807916B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113509897A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Device of low carbon olefin of high efficiency oxygen compound production |
| CN113509893A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using efficient oxygen-containing compound |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2020
- 2020-07-10 CN CN202010662029.1A patent/CN111807916B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113509897A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Device of low carbon olefin of high efficiency oxygen compound production |
| CN113509893A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using efficient oxygen-containing compound |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111807916B (en) | 2023-11-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111807916B (en) | Device for producing low-carbon olefin by efficient oxygen-containing compound | |
| CN110818521B (en) | Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound | |
| KR101847474B1 (en) | Method for preparing a light olefin using an oxygen-containing compound | |
| CN110117214B (en) | Device and method for preparing low-carbon olefin by efficiently converting methanol | |
| CN109012513B (en) | Methanol-to-olefin reactor | |
| CN111875465B (en) | Method for producing low-carbon olefin by oxygen-containing compound | |
| CN111871343A (en) | Device for producing low-carbon olefin by using oxygen-containing compound | |
| CN204474555U (en) | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons | |
| CN110818522B (en) | Device and method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compound | |
| CN110194967B (en) | Catalytic reaction regeneration method for producing more propylene | |
| CN111018646A (en) | Method and device for improving selectivity of low-carbon olefin prepared by converting oxygen-containing compound | |
| CN111004077A (en) | Method and device for improving selectivity of preparing low-carbon olefin by methanol conversion | |
| CN110950730B (en) | Method and equipment for improving selectivity of low-carbon olefin | |
| CN111875464B (en) | Method for producing low-carbon olefin by high-efficiency oxygen-containing compound | |
| CN105983455B (en) | A kind of regeneration method of organic oxide catalytic cracking arenes catalytic agent | |
| CN114717021A (en) | Method and reaction device for preparing olefin and aromatic hydrocarbon through catalytic cracking | |
| CN113509897A (en) | Device of low carbon olefin of high efficiency oxygen compound production | |
| CN113354496A (en) | Device for producing low-carbon olefin by using oxygen-containing compound | |
| CN108325477B (en) | Cascade moving bed reaction system for converting oxygen-containing compounds and application method | |
| CN102276389A (en) | Reaction and regeneration device for catalyzing and converting methanol and naphtha into lower olefins | |
| CN113087584A (en) | Method for producing low-carbon olefin by using oxygen-containing compound | |
| CN113509893A (en) | Method for producing low-carbon olefin by using efficient oxygen-containing compound | |
| CN110818520B (en) | Device and method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compound | |
| CN110950729B (en) | Method and equipment for improving selectivity of low-carbon olefin | |
| CN110819373B (en) | Device and method for preparing gasoline by using oxygen-containing compound |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |