CN112705127B - Reactor and method for producing low-carbon olefin - Google Patents
Reactor and method for producing low-carbon olefin Download PDFInfo
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- CN112705127B CN112705127B CN201911019850.5A CN201911019850A CN112705127B CN 112705127 B CN112705127 B CN 112705127B CN 201911019850 A CN201911019850 A CN 201911019850A CN 112705127 B CN112705127 B CN 112705127B
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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 a silicoaluminophosphate molecular sieve catalyst to a process for preparing olefin by converting methanol is studied in detail in the patent of US4499327, and SAPO-34 is considered to be the first catalyst for an 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 a methanol-to-olefin reaction equipment, 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 equipment 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 1-2s.
CN104437274 discloses a dense-phase fluidized bed reactor for preparing olefin by methanol conversion, which uses a special gas pre-lift pipe extending into the bed layer of the dense-phase fluidized bed reactor, and introduces gas to the bed layer in a radial direction, and the design of a special baffle in the reactor can greatly improve the selectivity of low-carbon olefin in the product in the process of a once-through reaction, and the retention time can be controlled within 0.5-1.5 s.
According to the published patent literature reports, the MTO reactor comprises various fluidization types and processes such as a bubbling fluidized bed, a dense-phase fluidized bed, a fast fluidized bed and the like at present, 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 bottom edge of the conical section is vertically 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 is radially angled from 30 to 65 ° with respect to the tangent to the wall of the reactor extension.
According to some embodiments of the invention, the ratio epsilon between the connecting line of the centers of the catalyst feed tubes and the connecting line of the gas flow section and the extension section is 1.2 to 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 feeding pipes are uniformly arranged along the circumference of the section when the number of the catalyst feeding pipes is multiple.
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 extension section is between 2.0 and 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, the ratio γ 2 of the length of the stretch to the line connecting the flow section and the stretch is between 12 and 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 distance between the horizontal height of the inlet of the communicating pipe and the top end of the settling section (6) is 1/3-1/2 of the length of the settling section.
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 at the center of the extension section (5), a small amount of fine powder is carried by the communicating pipe (6) and enters the gas-solid separator (7) for separation, solid-phase fine powder falls into the stripper downwards 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 combined with gas at the outlet of the stripper into product gas to enter the 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 0.5wt% to 6wt%.
According to some embodiments of the invention, the catalyst carbon deposition is 4wt% to 5wt%.
According to some embodiments of the invention, the feedstock consisting essentially of methanol is preheated to a temperature of from 100 to 200 ℃ before entering the reactor.
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 gas flow section of the reactor is in the range of 200 to 300 ℃.
According to some embodiments of the invention, the reaction temperature of the extension and settling sections is between 350 and 510 ℃.
According to some embodiments of the invention, the stripper has a temperature of 200 to 350 ℃ and a reaction pressure of 0.01 to 1MPa.
According to some embodiments of the invention, the gas-solid contact time of the feed gas and the catalyst in the reactor is 0.1 to 2s.
According to some embodiments of the invention, the gas-solid contact time of the feed gas and the catalyst in the reactor is 0.2 to 0.6s.
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) In some embodiments, the SAPO-34 catalyst is adopted, so that the gas-solid contact time can be reduced to the optimized 0.2-0.5 s, and the selectivity of carbon groups 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 an auxiliary illustration of the structure of the reactor for producing light olefins in fig. 1.
Fig. 3 is a partial enlarged view of H-H in fig. 2.
Fig. 4 isbase:Sub>A cross-sectional viewbase:Sub>A-base:Sub>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 are as follows:
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 0.8wt%, 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 axial wall included angle alpha (alpha =90 degrees) of each catalyst feeding pipe, the radial wall included angle theta (theta =35 degrees) of each catalyst feeding pipe is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and an intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the largest inner diameter position of the top of each 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 a intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting part is 4.5, the flow guide member is in a conical shape as shown in figure 6 (1), and the height of the bottom end and the intersegment connecting line is equal. 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 68.2wt% 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 0.8wt%, 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 = 68) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta = 35) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe to a connecting line between the sections is 1.5, the length of a gas flow section of a reactor and a connecting line between the sections is 3.6, the ratio beta 1 of the length of the largest 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 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 flow guide member is in a cone shape, and the height of the bottom end and the connecting line between the sections is equal as shown in figure 6 (1). 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 67.5wt% 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 0.8wt%, 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 = 110) of the axial wall surface of each catalyst feeding pipe is included, the included angle theta (theta = 35) of the radial wall surface tangent line is included, the ratio epsilon of a central connecting line of each feeding pipe 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 largest 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 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, and the flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 67.8wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial direction and the tangent line of the wall surface is, the ratio epsilon of a central connecting line of each feeding pipe to a connecting line between the sections is 1.5, the length of a gas flow section of a reactor and a connecting line between the sections is 3.6, the ratio beta 1 of the length of the largest 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 connecting line 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, and a flow guide member is in a conical shape as shown in figure 6 (1), and the connecting line between the bottom end and the section is not overlapped and the central line of the catalyst feeding pipes. 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 66.2wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =15 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor is 3.6 of a connecting line gamma 1 between the gas flow section and the reactor, the ratio beta 1 of the length of the largest 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 position of the intersegment connecting line is 4.5, the flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 65.9wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =80 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor is 3.6 of a connecting line gamma 1 between the gas flow section and the reactor, the ratio beta 1 of the length of the largest 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 position of the intersegment connecting line is 4.5, the flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 66.2wt% 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 0.8wt%, 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 = 90) of the axial wall surface of the catalyst feeding pipe is included, the included angle theta (theta = 35) of the radial wall surface tangent line is included, the ratio epsilon of a central connecting line of the feeding pipe to a connecting line between the sections is 1.5, the length of a gas flow section of a reactor and a connecting line between the sections is 3.6, the ratio beta 1 of the length of the largest 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 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, and the flow guide member is in the form of a cone, and the height of the connecting line between the bottom and the sections is equal to that of figure 6 (1). 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 63.2wt% 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 0.8wt%, 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 of each feeding pipe is rectangular as shown in figure 5 (1), the included angle alpha (alpha = 90) of the axial wall surface of each catalyst feeding pipe, the included angle theta (theta = 35) of the radial wall surface tangent line, the ratio epsilon of a central connecting line of each feeding pipe 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 line is 4.5, and a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 65.1wt% 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 0.8wt%, 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 circular as shown in figure 5 (3), the included angle alpha (alpha =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and an intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the largest 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 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 flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 67.4wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest 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 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 flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 67.2wt% after analysis.
[ example 11 ] A method for producing a polycarbonate
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 0.8wt%, 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 axial wall included angle alpha (alpha =90 degrees) of each catalyst feeding pipe, the radial wall included angle theta (theta =35 degrees) of each catalyst feeding pipe is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 1.5, the length of a gas flow section of a reactor and an intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the largest inner diameter position of 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 of the intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting part is 4.5, the flow guide member is in a conical shape as shown in figure 6 (1), and the height of the bottom end and the intersegment connecting line is equal. 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 to be 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 67.9wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest inner diameter position of 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 position of the intersegment connecting position is 17.5, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting position is 4.5, a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 67.2wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest inner diameter position of 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 position 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 7.5, a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 to be 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 65.4wt% after analysis.
[ example 14 ]
A reactor for producing low-carbon olefin adopts SAPO-34 molecular sieve catalyst as an active component, the carbon deposition of the catalyst is 4.5wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest inner diameter position of 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 position 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, a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 85.7wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest inner diameter position of 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 position 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, a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 64.5wt% 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 0.8wt%, 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 =90 degrees) of the axial wall surface of each catalyst feeding pipe is, the included angle theta (theta =35 degrees) of the radial wall surface tangent line is, the ratio epsilon of a central connecting line of each feeding pipe 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 largest inner diameter position of 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 position 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, a flow guide member is in a cone shape, and the height of the bottom end and the intersegment connecting line is equal as shown in figure 6 (1). 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 one-way diene (carbon-based) selectivity of the tail gas of the reactor is 66.8wt% after analysis.
[ 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 0.8wt%, 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 axial wall included angle alpha (alpha =90 degrees) of each catalyst feeding pipe, the radial wall included angle theta (theta =35 degrees) of each catalyst feeding pipe is, the ratio epsilon of a central connecting line of each feeding pipe to an intersegment connecting line is 2.5, the length of a gas flow section of a reactor and an intersegment connecting line gamma 1 are 3.6, the ratio beta 1 of the length of the largest inner diameter position of the top of each 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 of a intersegment connecting part is 14.6, the ratio beta 2 of the inner diameter of the bottom of the extension section to the intersegment connecting part is 4.5, the flow guide member is in a conical shape as shown in figure 6 (1), and the height of the bottom end and the intersegment connecting line is equal. 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 62.5wt% 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 0.8wt%, 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 60.8wt%.
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 4.5wt%, 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 81.2wt%.
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 (16)
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 discharge 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 (8);
the flow guide component (11) is conical or partially conical, and the conical sharp angle (f) is upward; 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).
2. Reactor according to claim 1, characterized in that the base (ee) of said conical section coincides with the connecting line (bb) of said flow section (4) and extension (5).
3. Reactor according to any of claims 1-2, characterized in that the catalyst feed pipe (2) is axially angled with respect to the reactor extension (5) wall by an angle α,60 ° < α <120 °;
and/or an included angle theta between the radial direction of the catalyst feeding pipe (2) and the wall tangent of the reactor extension section (5) is less than or equal to 90 degrees when the angle is 0 degrees and less than or equal to theta;
and/or the ratio epsilon of a connecting line (dd) at the center of the catalyst feeding pipe (2) to a connecting line (bb) of the airflow section (4) and the extension section (5) is 1.2-3.
4. A reactor according to claim 3, characterized in that the catalyst feed (2) is axially angled with respect to the wall of the reactor extension (5) by an angle α of 80-100 °;
and/or the included angle theta between the radial direction of the catalyst feeding pipe (2) and the wall tangent of the reactor extension section (5) is 30-65 degrees;
and/or the ratio epsilon of a connecting line (dd) of the center of the catalyst feeding pipe (2) to a connecting line (bb) of the gas flow section (4) and the extension section (5) is 1-2.
5. The reactor according to any of claims 1-2, characterized in that the catalyst feed pipe (2) has a cross-sectional shape of a rectangle, ellipse or circle;
and/or the number of the catalyst feeding pipes (2) is one or more;
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.
6. The reactor according to claim 5, characterized in that the catalyst feeding pipe (2) has a rectangular cross-sectional shape;
and/or the number of the catalyst feeding pipes (2) is four.
7. Reactor according to any of claims 1-2, 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 stretch section (5) is between 2.0 and 5.0;
and/or the ratio beta 1 of the length (aa) of the part with the largest 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.
8. The reactor according to claim 7, 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 stretch section (5) is between 3.1 and 4.0;
and/or the ratio beta 1 of the length (aa) of the part with the largest 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 1.6-2.0.
9. A reactor according to any one of claims 1 to 2, 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 comprised between 12 and 18;
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.
10. Reactor according to claim 9, characterized in that the ratio γ 2 of the length (L2) of said stretch (5) to the connection line (bb) of said gas flow section (4) and stretch (5) is 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 3-5.
11. The reactor according to any one of claims 1-2, wherein the communicating tube (6) penetrates 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 settling section (10) from the top end of the settling section (10).
12. A method for producing lower olefins using the reactor according to any one of claims 1 to 11, 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.
13. The method of claim 12, wherein the active component of the catalyst is SAPO-34 molecular sieve and/or catalyst carbon deposition is 0.5wt% to 6wt%;
and/or, a preheating step is carried out before the raw material mainly comprising the methanol enters the reactor, and the preheating temperature is 100-200 ℃.
14. The method of claim 13, wherein the catalyst carbon deposition is 4wt% to 5wt%.
15. The process according to any one of claims 12 to 14, characterized in that the auxiliary gas on the catalyst feed (2) is 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.
16. The method of claim 15, wherein the gas-solid contact time of the raw material gas and the catalyst in the reactor is 0.2 to 0.6s.
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|---|---|---|---|---|
| CN1530423A (en) * | 2003-03-11 | 2004-09-22 | 中国石油化工股份有限公司 | Descending naphtholite catalytic cracking method |
| CN101165017A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Production increasing method for propylene |
| CN101279873A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether |
| CN102276397A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for producing light olefins with high selectivity by using methanol as raw material |
| CN102875281A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Method for catalytically converting methanol to low-carbon olefins |
| WO2015081484A1 (en) * | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
| CN105218288A (en) * | 2014-07-03 | 2016-01-06 | 中国石油化工股份有限公司 | For efficient gas-solid sharp separation and the sedimentation method of methanol-to-olefins |
| CN105315119A (en) * | 2014-07-03 | 2016-02-10 | 中国石油化工股份有限公司 | Methanol-to-olefin method based on high-density reactor |
| CN107400532A (en) * | 2017-06-13 | 2017-11-28 | 神华集团有限责任公司 | Preparing light olefins from methanol device |
| WO2018196360A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Device and method for preparing para-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and toluene |
| CN109012513A (en) * | 2018-08-16 | 2018-12-18 | 中国石油大学(北京) | A kind of methanol to olefins reaction device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9023286B2 (en) * | 2012-03-23 | 2015-05-05 | Uop Llc | MTO regenerator multi-pass grids |
-
2019
- 2019-10-24 CN CN201911019850.5A patent/CN112705127B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1530423A (en) * | 2003-03-11 | 2004-09-22 | 中国石油化工股份有限公司 | Descending naphtholite catalytic cracking method |
| CN101165017A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Production increasing method for propylene |
| CN101279873A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether |
| CN102276397A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for producing light olefins with high selectivity by using methanol as raw material |
| CN102875281A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Method for catalytically converting methanol to low-carbon olefins |
| WO2015081484A1 (en) * | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
| CN105218288A (en) * | 2014-07-03 | 2016-01-06 | 中国石油化工股份有限公司 | For efficient gas-solid sharp separation and the sedimentation method of methanol-to-olefins |
| CN105315119A (en) * | 2014-07-03 | 2016-02-10 | 中国石油化工股份有限公司 | Methanol-to-olefin method based on high-density reactor |
| WO2018196360A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Device and method for preparing para-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and toluene |
| CN107400532A (en) * | 2017-06-13 | 2017-11-28 | 神华集团有限责任公司 | Preparing light olefins from methanol device |
| CN109012513A (en) * | 2018-08-16 | 2018-12-18 | 中国石油大学(北京) | A kind of methanol to olefins reaction device |
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