CN112705127A - Reactor and method for producing low-carbon olefin - Google Patents
Reactor and method for producing low-carbon olefin Download PDFInfo
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- CN112705127A CN112705127A CN201911019850.5A CN201911019850A CN112705127A CN 112705127 A CN112705127 A CN 112705127A CN 201911019850 A CN201911019850 A CN 201911019850A CN 112705127 A CN112705127 A CN 112705127A
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- 229910052799 carbon Inorganic materials 0.000 title abstract description 80
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title abstract description 46
- 238000004519 manufacturing process Methods 0.000 title abstract description 8
- 239000003054 catalyst Substances 0.000 abstract description 136
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 102
- 238000006243 chemical reaction Methods 0.000 abstract description 61
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 44
- 239000007787 solid Substances 0.000 abstract description 34
- 239000002994 raw material Substances 0.000 abstract description 29
- 230000008021 deposition Effects 0.000 abstract description 23
- 150000001336 alkenes Chemical class 0.000 abstract description 18
- 238000000034 method Methods 0.000 abstract description 13
- 230000008569 process Effects 0.000 abstract description 8
- 230000035484 reaction time Effects 0.000 abstract description 4
- 239000000843 powder Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 238000005728 strengthening Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 148
- 239000012071 phase Substances 0.000 description 23
- 239000002808 molecular sieve Substances 0.000 description 22
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 22
- 150000001993 dienes Chemical class 0.000 description 20
- 238000004458 analytical method Methods 0.000 description 9
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- -1 carbon olefins Chemical class 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 2
- 239000007806 chemical reaction intermediate Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000008602 contraction Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
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- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000012822 chemical development Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/0035—Periodical feeding or evacuation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/082—Controlling processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/085—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
- C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
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- 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
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- 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
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- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P30/40—Ethylene production
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Abstract
The invention discloses a reactor and a method for producing low-carbon olefin, which mainly solve the problem of low selectivity of a target product of the low-carbon olefin in the process of producing the olefin by converting methanol. The reactor mainly comprises an airflow section, an extension section and a settling section, and the selectivity of a target product is improved by strengthening the reaction generation process of low-carbon olefin after the contact of a material agent in a very short time. The process comprises the steps that a raw material mainly comprising methanol is introduced into a reactor from a raw material distributor, flows into an air flow section of the reactor, is contracted and accelerated, then enters an extension section and is in cross flow rapid contact with a catalyst from a catalyst blanking pipe to react, tail gas after the reaction enters gas-solid separation equipment through a communicating pipe to separate a small amount of catalyst fine powder carried, the catalyst entering the reactor is gathered in a side wall area after the reaction and falls into a settling section, and then is introduced into a stripper through a discharging inclined pipe to be stripped and then collected for reuse, the reaction time is short, the carbon deposition amount of the catalyst is low, the catalyst can be directly recycled, and the use load of a regenerator is greatly reduced.
Description
Technical Field
The invention relates to the field of methanol-to-olefin, in particular to a reactor and a method for producing low-carbon olefin.
Background
Olefins, especially low carbon olefins such as ethylene and propylene, are important basic organic chemical raw materials, and the annual yield of the olefins can be measured by the chemical development level of a country. The production of olefin by methanol conversion refers to a technology of producing methanol from natural gas or coal as a raw material through synthesis gas, and then generating low-carbon olefin such as ethylene, propylene and the like from the methanol under the action of a catalyst, and the product is proved to be completely suitable for the production of products such as polyolefin and the like.
At present, the self-supporting rate of low-carbon olefins in China is about 50%, and with the rapid development of national economy and chemical industry, the demand for low-carbon olefins is continuously increased, and the contradiction between supply and demand is increasingly prominent. The method combines the energy current situation of more coal, lean oil and less gas in China, and utilizes methanol as a raw material to convert and produce olefin, so that the pressure of insufficient crude oil supply in China can be reduced, the method has important significance for promoting the forward development of chemical industry, and the method is a research focus for synthesizing olefin from unconventional petroleum resources. Through research on reaction mechanism, the first step in the MTO reaction process is mainly a reaction intermediate for generating the polymethyl benzene, and the reaction rate of continuously converting the methyl benzene into the olefin from the reaction intermediate is very fast.
The application of silicoaluminophosphate molecular sieve catalyst to a process for preparing olefin by methanol conversion is studied in detail in the patent of US4499327, and SAPO-34 is considered to be the first catalyst for MTO process. The SAPO-34 catalyst has high selectivity and high activity for low-carbon olefin, and can ensure that the reaction time for converting methanol into the low-carbon olefin reaches a degree of less than 10 seconds, even reaches the reaction time range of a riser.
CN205024117 discloses an invention patent of a methanol-to-olefin reaction device, which adopts a dense-phase fluidized bed reactor with a transverse grid with a specific structure at the bottom, can break bubbles to enhance gas-solid mixing, can shorten the free space at the upper part of the reaction device on the other hand, and can reduce the gas-solid reaction time, thereby improving the product selectivity and the olefin yield. According to the patent, the gas reaction residence time of the methanol-to-olefin reaction equipment can be shortened to 1-2 s.
CN104437274 discloses an invention patent of a dense-phase fluidized bed reactor for preparing olefin by methanol conversion, which uses a special gas pre-lifting pipe extending into the bed layer of the dense-phase fluidized bed reactor, and leads the gas to flow radially to the bed layer, and the selectivity of low carbon olefin in products in a single-pass reaction process can be greatly improved by combining with the design of a special baffle in the reactor, and the retention time can be controlled within 0.5-1.5 s.
According to the reports of published patent documents, the prior MTO reactor comprises a bubbling fluidized bed, a dense-phase fluidized bed, a fast fluidized bed and other fluidization types and processes, but still has the problem that the selectivity of the low-carbon olefin is difficult to further improve.
Disclosure of Invention
One of the technical problems to be solved by the invention is the problem of low selectivity of low-carbon olefin in the prior art of producing olefin by converting methanol, so that a reactor for producing olefin is provided. The reactor has the advantages that the rapid contact and rapid separation of the raw materials and the catalyst are realized through a specific structure, the selectivity of the target product of the low-carbon olefin is improved, and the carbon deposition of the catalyst is less in the reaction process.
The second technical problem to be solved by the present invention is to provide a process method corresponding to the first technical problem. In the technical scheme, the catalyst used as an active component is an SAPO-34 molecular sieve catalyst.
The invention provides a reactor for producing low-carbon olefin, which comprises a gas flow section, an extension section, a sedimentation section and a flow guide member, is connected with a gas-solid separator and a stripper, and is characterized in that the gas flow section, the extension section and the sedimentation section are coaxially and sequentially connected from top to bottom and are communicated with each other in inner cavities; the gas flow section is internally provided with a raw material gas inlet distributor and the flow guide component, and the joint of the gas flow section and the extension section is of a contraction structure; a catalyst feeding pipe is arranged at the upper part of the extension section near the gas flow section; the settling section built-in communicating pipe penetrates through the side wall surface of the settling section to be connected with the gas-solid separator, and a catalyst discharging pipe is arranged at the bottom of the settling section to be connected with the stripper; the stripper and the reactor are arranged in parallel, the gas-solid separator and the stripper are arranged vertically, and a solid-phase outlet at the end of the gas-solid separator is introduced into the stripper.
According to some embodiments of the invention, the flow guide member is tapered or partially tapered, the angle of the taper facing upwards; the vertical direction of the bottom edge of the conical section is positioned between the connecting line of the gas flow section and the extension section and the central connecting line of the catalyst feeding pipe.
According to some embodiments of the invention, the base of the cone section coincides with the line connecting the gas flow section and the extension section.
According to some embodiments of the invention, the catalyst feed pipe is axially angled with respect to the reactor extension wall by an angle α of 60 ° < α <120 °.
According to some embodiments of the invention, the catalyst feed pipe is axially angled with respect to the wall of the reactor extension by an angle α of 80 to 100 °.
According to some embodiments of the invention, the angle θ between the radial direction of the catalyst feed pipe and the tangent to the wall of the reactor extension section is 0 ° < θ ≦ 90 °.
According to some embodiments of the invention, the catalyst feed pipe has an angle θ of 30 to 65 ° with respect to the tangential line of the wall of the reactor extension section.
According to some embodiments of the invention, the ratio epsilon of the connecting line of the center of the catalyst feeding pipe to the connecting lines of the gas flow section and the extension section is 1.2-3.
According to some embodiments of the invention, the catalyst feed pipe center connecting line to the connecting line of the gas flow section and the extension) ratio epsilon is 1-2.
According to some embodiments of the invention, the catalyst feed conduit has a cross-sectional shape that is rectangular, oval or circular.
According to some embodiments of the invention, the number of catalyst feed pipes is one or more.
According to some embodiments of the invention, the number of catalyst feed pipes is four.
According to some embodiments of the invention, the catalyst feed pipes are arranged in a plurality and are uniformly distributed along the circumference of the cross section.
According to some embodiments of the invention, a ratio γ 1 of a length of the gas flow section to a length of a connecting line of the gas flow section and the extension section is 2.0 to 5.0.
According to some embodiments of the invention, the ratio γ 1 of the length of the flow section to the length of the line connecting the flow section and the stretch section is between 3.1 and 4.0.
According to some embodiments of the invention, the ratio β 1 of the length of the top of the flow section where the inner diameter is largest to the line connecting the flow section and the extension is 1.5-3.2.
According to some embodiments of the invention, the ratio β 1 of the length of the top of the gas flow section where the inner diameter is largest to the line connecting the gas flow section and the extension section is 1.6-2.0.
According to some embodiments of the invention, a ratio γ 2 of a length of the extension to a connecting line of the air flow section and the extension is 12 to 18.
According to some embodiments of the invention, the ratio γ 2 of the length of the stretch to the line connecting the flow section and the stretch is between 13 and 15.
According to some embodiments of the invention, the ratio β 2 of the maximum inner diameter at the bottom of the stretch to the line connecting the gas flow section and the stretch is 2 to 8.
According to some embodiments of the invention, the ratio β 2 of the maximum inner diameter at the bottom of the stretch to the line connecting the gas flow section and the stretch is 3 to 5.
According to some embodiments of the invention, the communicating pipe penetrates through the side wall surface of the settling section and is connected with the inlet of the gas-solid separator, the inlet direction of the communicating pipe is vertically downward, and the horizontal height of the inlet of the communicating pipe is 1/3-1/2 of the length of the settling section from the top end of the settling section (6).
A second aspect of the present invention provides a method for producing lower olefins using the reactor according to the first aspect, comprising the steps of: the raw material mainly comprising methanol is introduced into the gas flow section (4) of the reactor through a raw material gas inlet distributor (3), enters the extension section (5) through rectification and acceleration under the action of the gas flow section (4) and a flow guide member (11), contacts and reacts with the catalyst falling from the catalyst inlet pipe (2) at the upper part of the extension section (5), and the reacted catalyst is gathered on the near wall surface, falls to the settling section (10) along the near wall surface, and is introduced into a stripper (8) through a catalyst discharge pipe (9) for stripping; gas after reaction is gathered in the center of the extension section (5), a small amount of fine powder is carried by a communicating pipe (6) and enters a gas-solid separator (7) for separation, solid-phase fine powder falls downwards into a stripper and is stripped together with other catalysts for recycling or regeneration of the catalysts, and the separated gas is discharged from the top and is merged with gas at the outlet of the stripper into product gas to enter a subsequent flow.
According to some embodiments of the invention, the active component of the catalyst is a SAPO-34 molecular sieve.
According to some embodiments of the invention, the catalyst carbon deposition is 0.5 wt% to 6 wt%.
According to some embodiments of the invention, the catalyst carbon deposition is 4 wt% to 5 wt%.
According to some embodiments of the present invention, a pre-heating step is performed before the raw material mainly comprising methanol enters the reactor, wherein the pre-heating temperature is 100-200 ℃.
According to some embodiments of the invention, the medium of the auxiliary gas on the catalyst feed line is steam or nitrogen.
According to some embodiments of the invention, the temperature of the reactor gas flow section is 200-300 ℃.
According to some embodiments of the invention, the reaction temperature of the extension section and the settling section is 350 to 510 ℃.
According to some embodiments of the invention, the temperature of the stripper is 200 to 350 ℃ and the reaction pressure is 0.01 to 1 MPa.
According to some embodiments of the invention, the gas-solid contact time of the feedstock gas and the catalyst in the reactor is 0.1 to 2 seconds.
According to some embodiments of the invention, the gas-solid contact time of the feedstock gas and the catalyst in the reactor is 0.2 to 0.6 s.
The invention has the beneficial effects that:
1) the gas-solid contact mode of the traditional fluidized bed in the process of producing olefin by converting methanol is designed into the contact mode of local gas-solid cross flow at the top of the extension section of the reactor and integral gas-solid descending, and is matched with the atmospheric velocity, so that the gas-solid contact time is greatly reduced, the optimal conditions in the reaction process are met, and the selectivity of reacting low-carbon olefin is improved;
2) the special gas inlet structure and the flow guide component are set, so that the gas velocity of raw material gas is greatly improved after passing through the contraction structure, on one hand, the contact time is reduced, and meanwhile, near-wall local negative pressure is formed to improve the fluidity of the catalyst and improve the gas-solid contact efficiency;
3) a specific catalyst feeding pipe is designed, so that a catalyst enters a reactor tangentially at a certain angle in the horizontal direction, after gas is fixedly connected at a high gas speed, the centrifugal action of catalyst particles is further enhanced to form downward rotational flow around a central shaft main body of the reactor, an aggregation layer is formed relative to a near-wall area of the reactor, and gas is concentrated in an axial central area of an extension section of the reactor after flowing around a flow guide member, so that the gas and solid phases are quickly separated after initial contact, secondary reaction is reduced, and the catalyst is reduced from being carried out;
4) the gas in the extension section of the reactor is in a downward plug flow in an approximate flowing state, so that the back mixing of the gas in the reactor is reduced to the maximum extent, the gas is separated from the reactor quickly, the gas retention time is reduced, and possible side reactions are further inhibited;
5) according to the low-carbon olefin produced by the technical scheme, in some embodiments, the SAPO-34 catalyst is adopted, the gas-solid contact time can be reduced to 0.2-0.5 s, and the carbon-based selectivity of ethylene and propylene in the product composition can reach more than 85 wt%.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic diagram of the structure and process flow of a reactor for producing lower olefins according to an embodiment of the present invention.
FIG. 2 is a view for explaining the structure of the reactor for producing lower olefins in FIG. 1.
Fig. 3 is a partial enlarged view of H-H in fig. 2.
Fig. 4 is a cross-sectional view a-a of fig. 1.
Fig. 5 is a sectional view in the direction of catalyst feed line E-E in fig. 4.
Fig. 6 is a schematic view of the shape of the flow guide member of fig. 1.
Reference numerals:
1: reactor, 2: catalyst feed pipe, 3: raw material inlet distributor, 4: gas flow section, 5: extension, 6: communication pipe, 7: cyclone, 8: stripper, 9: catalyst discharge pipe, 10: settling section, 11: a flow guide member.
Detailed Description
The present invention will be described in detail below with reference to the drawings and examples, but the present invention is not limited to the examples.
[ example 1 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.3s, and the selectivity of the diene (carbon base) in one pass is 68.2 wt% after the tail gas of the reactor is analyzed.
[ example 2 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 68 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.4s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.5 wt% after analysis.
[ example 3 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 110 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.2s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.8 wt% after analysis.
[ example 4 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), an included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, an included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section and the inner diameter at the intersegment connecting position is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting position is 4.5, and a. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.8s, and the selectivity of the diene (carbon) in one pass is 66.2 wt% after the tail gas of the reactor is analyzed.
[ example 5 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta) of the radial direction and the tangent line of the wall surface is 15 degrees, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 1.8s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 65.9 wt% after analysis.
[ example 6 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta) of the radial direction and the tangent line of the wall surface is 80 degrees, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.7s, and the selectivity of the diene (carbon) in one pass is 66.2 wt% after the tail gas of the reactor is analyzed.
[ example 7 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst is fed by using a single catalyst feeding pipe, the cross section of the feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of the catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial wall surface tangent line, the ratio epsilon of the central connecting line of the feeding pipe to the connecting line between the sections is 1.5, the length of the gas flow section of the reactor and the connecting line between the sections is 3.6, the ratio beta 1 of the length of the maximum inner diameter position of the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of the extension section to the inner diameter of the connecting position between the sections is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the connecting position between the sections is 4.5. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.3s, and the selectivity of the diene (carbon base) in one pass is 63.2 wt% after the tail gas of the reactor is analyzed.
[ example 8 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. Two catalyst feeding pipes are used for feeding, the cross section shapes of the feeding pipes are rectangular as shown in figure 5(1), an included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, an included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter position of the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter position of the intersegment connecting line is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.3s, and the selectivity of the diene (carbon) in one pass is 65.1 wt% after the tail gas of the reactor is analyzed.
[ example 9 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst is fed by using 4 catalyst feeding pipes, the cross sections of the feeding pipes are circular as shown in fig. 5(3), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial wall surface tangent line, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter position of the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter of the intersegment connecting position is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting position is 4.5. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.4s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.4 wt% after analysis.
[ example 10 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 2.0, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 1.8, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.2s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.2 wt% after analysis.
[ example 11 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.3s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.9 wt% after analysis.
[ example 12 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 17.5, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.5s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 67.2 wt% after analysis.
[ example 13 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.6s, and the selectivity of the diene (carbon) in one pass is 65.4 wt% after the tail gas of the reactor is analyzed.
[ example 14 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 4.5 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.6s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 85.7 wt% after analysis.
[ example 15 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 1.1s, and the one-way diene (carbon-based) selectivity of the tail gas of the reactor is 64.5 wt% after analysis.
[ example 16 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 46m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.1s, and the selectivity of the diene (carbon) in one pass is 66.8 wt% after the tail gas of the reactor is analyzed.
[ example 17 ]
A reactor for producing low-carbon olefin adopts a SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 0.8 wt%, gas-phase methanol is preheated to 180 ℃ for feeding, and the structure of the reactor is shown in figure 1. The catalyst feeding pipe is fed by 4 catalyst feeding pipes, the cross section of each feeding pipe is rectangular as shown in figure 5(1), the included angle alpha (alpha is 90 degrees) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta is 35 degrees) of the radial direction and the tangent line of the wall surface, the ratio epsilon of a central connecting line of the feeding pipes to an intersegment connecting line is 2.5, the length of a gas flow section of a reactor and the intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the maximum inner diameter at the top of the gas flow section to the connecting line is 3.0, the ratio gamma 2 of the length of an extension section to the inner diameter at the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter at the bottom of the extension section to the intersegment connecting part. The reaction temperature in the reactor is 480 ℃, the raw material gas enters the local ejection gas velocity of the extension section after passing through the flow guide component and is 25m/s, the auxiliary gas is steam, the reaction pressure is 125kPa, the gas-solid contact time is 0.5s, and the selectivity of the diene (carbon) in one pass is 62.5 wt% after the tail gas of the reactor is analyzed.
Comparative example 1
In a fluidized bed system for continuous reaction and regeneration of olefin prepared by methanol conversion, the active component is SAPO-34 molecular sieve catalyst, the carbon deposition of the catalyst is 0.8 wt%, the gas phase methanol is preheated to 180 ℃ for feeding, the reaction temperature in a fast bed reactor is 480 ℃, the reaction pressure is 125kPa, and the selectivity of diene (carbon) per pass is 60.8 wt%.
Comparative example 2
In a fluidized bed system for continuous reaction and regeneration of olefin prepared by methanol conversion, the active component is SAPO-34 molecular sieve catalyst, the carbon deposition of the catalyst is 4.5 wt%, the gas phase methanol is preheated to 180 ℃ for feeding, the reaction temperature in a fast bed reactor is 480 ℃, the reaction pressure is 125kPa, and the selectivity of single-pass diene (carbon base) is 81.2 wt%.
The parameters and the once-through diene (carbon based) selectivity of the examples and comparative examples are compared in table 1.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (10)
1. A reactor (1) for producing low-carbon olefin comprises a gas flow section (4), an extension section (5), a sedimentation section (10) and a flow guide member (11), and is connected with a gas-solid separator (7) and a stripper (8), and is characterized in that the gas flow section (4), the extension section (5) and the sedimentation section (10) are coaxially connected from top to bottom in sequence and communicated with each other in inner cavities; a raw material air inlet distributor (3) and the flow guide component (11) are arranged in the air flow section (4), and the joint of the air flow section (4) and the extension section (5) is of a contraction structure; a catalyst feeding pipe (2) is arranged at the upper part of the extension section (5) close to the gas flow section (4); a communicating pipe (6) arranged in the settling section (10) penetrates through the side wall surface of the settling section (10) to be connected with the gas-solid separator (7), and a catalyst discharging pipe (9) arranged at the bottom of the settling section (10) is connected with the stripper (8); the stripper (8) and the reactor (1) are arranged in parallel, the gas-solid separator (7) and the stripper (8) are arranged vertically, and a solid phase outlet at the end of the gas-solid separator (7) is introduced into the stripper (7).
2. A reactor according to claim 1, wherein said flow-guide means (11) are conical or partially conical, with the point (f) of said cone pointing upwards; the bottom edge (ee) of the conical section is located vertically between the connecting line (bb) of the gas flow section (4) and the extension section (5) and the central connecting line (dd) of the catalyst feed pipe (2), preferably the bottom edge (ee) of the conical section coincides with the connecting line (bb) of the gas flow section (4) and the extension section (5).
3. Reactor according to claim 1 or 2, characterized in that the catalyst feed (2) is axially angled with respect to the wall of the reactor extension (5) by an angle α, 60 ° < α <120 °, preferably 80-100 °;
and/or the included angle theta between the radial direction of the catalyst feeding pipe (2) and the wall tangent of the extension section (5) of the reactor is 0 degree < theta is less than or equal to 90 degrees, and preferably is 30-65 degrees;
and/or the ratio epsilon of the central connecting line (dd) of the catalyst feeding pipe (2) to the connecting line (bb) of the gas flow section (4) and the extension section (5) is 1.2-3, preferably 1-2.
4. A reactor according to any one of claims 1 to 3, characterized in that the catalyst feed (2) has a cross-sectional shape which is rectangular, oval or circular, preferably rectangular;
and/or the number of the catalyst feeding pipes (2) is one or more, preferably four;
and/or the catalyst feeding pipes (2) are uniformly arranged along the circumference of the cross section when the number of the catalyst feeding pipes is multiple.
5. The reactor according to any of claims 1 to 4, characterized in that the ratio γ 1 of the length (L1) of the gas flow section (4) to the length of the connecting line (bb) of the gas flow section (4) and the extension section (5) is between 2.0 and 5.0, preferably between 3.1 and 4.0;
and/or the ratio beta 1 of the length (aa) of the maximum inner diameter at the top of the gas flow section (4) to the connecting line (bb) of the gas flow section (4) and the extension section (5) is 1.5-3.2, preferably 1.6-2.0.
6. A reactor according to any one of claims 1 to 5, characterized in that the ratio γ 2 of the length (L2) of said stretch (5) to the line (bb) joining said gas flow section (4) and said stretch (5) is between 12 and 18, preferably between 13 and 15;
and/or the ratio beta 2 of the maximum inner diameter (cc) at the bottom of the extension (5) to the connecting line (bb) of the gas flow section (4) and the extension (5) is 2-8, preferably 3-5.
7. The reactor according to any one of claims 1 to 6, characterized in that the communicating tube (6) passes through the side wall surface of the settling section (10) and is connected with the inlet of the gas-solid separator (7), the inlet direction of the communicating tube (6) is vertically downward, and the horizontal height of the inlet of the communicating tube (6) is 1/3-1/2 of the length of the top end of the settling section (10).
8. A method for producing lower olefins using the reactor according to any one of claims 1 to 7, comprising the steps of: the raw material mainly comprising methanol is introduced into the gas flow section (4) of the reactor through a raw material gas inlet distributor (3), enters the extension section (5) through rectification and acceleration under the action of the gas flow section (4) and a flow guide member (11), contacts and reacts with the catalyst falling from the catalyst inlet pipe (2) at the upper part of the extension section (5), and the reacted catalyst is gathered on the near wall surface, falls to the settling section (10) along the near wall surface, and is introduced into a stripper (8) through a catalyst discharge pipe (9) for stripping; gas after reaction is gathered in the center of the extension section (5), a small amount of fine powder is carried by a communicating pipe (6) and enters a gas-solid separator (7) for separation, solid-phase fine powder falls downwards into a stripper and is stripped together with other catalysts for recycling or regeneration of the catalysts, and the separated gas is discharged from the top and is merged with gas at the outlet of the stripper into product gas to enter a subsequent flow.
9. The method of claim 8, wherein the active component of the catalyst is SAPO-34 molecular sieve, preferably with 0.5 wt% to 6 wt% of catalyst carbon deposit, more preferably with 4 wt% to 5 wt% of catalyst carbon deposit;
and/or a preheating step is carried out before the raw material mainly comprising the methanol enters the reactor, wherein the preheating temperature is 100-200 ℃.
10. The process according to claim 8 or 9, characterized in that the auxiliary gas is fed to the catalyst feed (2) in the medium of steam or nitrogen;
and/or the temperature of the gas flow section (4) of the reactor is 200-300 ℃;
and/or the reaction temperature of the extension section (5) and the sedimentation section (10) is 350-510 ℃;
and/or the temperature of the stripper (8) is 200-350 ℃, and the reaction pressure is 0.01-1 MPa;
and/or the gas-solid contact time of the raw material gas and the catalyst in the reactor is 0.1-2 s, and the preferable range is 0.2-0.6 s.
Priority Applications (1)
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