CN110819373A - Device and method for preparing gasoline by using oxygen-containing compound - Google Patents

Device and method for preparing gasoline by using oxygen-containing compound Download PDF

Info

Publication number
CN110819373A
CN110819373A CN201810888047.4A CN201810888047A CN110819373A CN 110819373 A CN110819373 A CN 110819373A CN 201810888047 A CN201810888047 A CN 201810888047A CN 110819373 A CN110819373 A CN 110819373A
Authority
CN
China
Prior art keywords
reactor
regenerator
catalyst
spent
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201810888047.4A
Other languages
Chinese (zh)
Other versions
CN110819373B (en
Inventor
刘昱
施磊
乔立功
李海瑞
张洁
昌国平
王雷
吴咏斐
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Engineering Group Co Ltd
Sinopec Guangzhou Engineering Co Ltd
Original Assignee
Sinopec Engineering Group Co Ltd
Sinopec Guangzhou Engineering Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sinopec Engineering Group Co Ltd, Sinopec Guangzhou Engineering Co Ltd filed Critical Sinopec Engineering Group Co Ltd
Priority to CN201810888047.4A priority Critical patent/CN110819373B/en
Publication of CN110819373A publication Critical patent/CN110819373A/en
Application granted granted Critical
Publication of CN110819373B publication Critical patent/CN110819373B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
    • C10G3/55—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds
    • C10G3/57—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds according to the fluidised bed technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/62—Catalyst regeneration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The invention discloses a device for preparing gasoline by using oxygen-containing compounds in the field of petrochemical industry, which comprises a reactor, a regenerator, an external heat remover and a spent stripper, wherein the reactor comprises a first reactor, a second reactor and a riser reactor, the regenerator is connected with the riser reactor through a regeneration slide valve, and the riser reactor extends into the first reactor; the first reactor is communicated with the second reactor; an external heat remover is arranged in the second reactor; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator. The device provided by the invention can improve the selectivity of target products to the maximum extent, such as the selectivity and yield of gasoline or aromatic hydrocarbon products; the problems of high bed layer and difficult fluidization of the catalyst in the reactor and the regenerator are solved, and the fluidization state is maintained; can meet the requirements of reaction regeneration conditions of the MTG process.

Description

Device and method for preparing gasoline by using oxygen-containing compound
Technical Field
The invention relates to the technical field of hydrocarbon preparation from one or more non-hydrocarbon compounds, in particular to a device and a method for preparing gasoline from oxygen-containing compounds.
Background
Methanol is an important chemical product and chemical raw material, and is one of the future clean energy sources. As a key product of chemical engineering, methanol is the best way to produce other chemical products or synthetic fuels from natural gas or coal, and its importance is self-evident. Although the methanol can be directly blended into gasoline to be used as methanol gasoline fuel, the methanol has better economic benefit value when being directly converted into gasoline than when being blended into gasoline for use. Therefore, the successful development and the industrial application of the technology for preparing the gasoline from the methanol not only relieve the problems of petroleum shortage, excessive methanol and the like in China, but also enrich the technical route of preparing the oil from the coal, and have important strategic and practical significance.
Oxygen-containing organic compounds represented by methanol or dimethyl ether are typical oxygen-containing organic compounds, and are mainly produced from coal-based or natural gas-based synthesis gas. The process for producing gasoline from an oxygen-containing organic compound represented by methanol is currently mainly the MTG technology. At present, the processes for preparing gasoline by using methanol in the world mainly comprise: the process comprises a process for preparing gasoline from exxon-Mobil Methanol (MTG), a Fischer-Tropsch synthesis process (FT), a Torpo integrated gasoline synthesis process (TIGAS) and a domestic one-step methanol conversion gasoline preparation technology. Wherein the Exxon-Mobil methanol-to-gasoline process (MTG) technology is the most mature, and the industrial application is the most in the world.
In recent years, the method of producing gasoline from oxygenates has become a focus and focus of research for those skilled in the art. People have conducted extensive research and exploration in the aspects of process flows, equipment structures and the like.
Chinese patent CN101182276B discloses a method for preparing gasoline by methanol conversion, which is to increase the total catalyst bed length of the reactor, and at the same time, add several pairs of material inlets and outlets on the side wall of the reactor, these material inlets and outlets divide the catalyst bed in the reactor into several sections of shorter catalyst beds, and through the switch of the valves installed on the inlets and outlets, the reaction materials always pass through the shorter catalyst beds when passing through the reactor, so as to achieve the purpose of realizing the complete conversion of methanol, reducing the pressure drop of the bed, prolonging the regeneration period and the replacement period of the catalyst, simplifying the process operation, and improving the production efficiency and the process technology and economic performance. The invention is only suitable for the fixed bed, needs frequent regeneration, has long operation period, is not beneficial to the timely export of reaction heat, and has the problem of non-uniform temperature distribution of the reaction bed layer.
Chinese patent CN105419849A discloses an energy-saving process for preparing gasoline by methanol conversion, which comprises the following steps: gasifying the raw material methanol and then entering a first pre-reactor for pre-reaction; the outlet gas of the first pre-reactor 1 enters a second pre-reactor for reaction, the reaction outlet gas of the second pre-reactor enters a synthetic oil reactor for reaction and then enters an oil-gas-water separator for separation, the separated oil phase product is sent to an oil product separator, and a gasoline product, a heavy oil product and a liquefied petroleum gas product are obtained after separation. The invention has the advantages of stable reaction temperature, low circulating energy consumption and low circulating investment. The invention is only suitable for the fixed bed, needs frequent regeneration, has long operation period, is not beneficial to the timely export of reaction heat, and has the problem of non-uniform temperature distribution of the reaction bed layer.
Chinese patent CN105018129B discloses a fluidized bed methanol-to-gasoline device and method, and the invention discloses a fluidized bed methanol-to-gasoline device and method in the fields of coal chemical industry and petrochemical industry, so as to solve the problems of low conversion rate of methanol to gasoline and the like in the prior art. The reactor (26) of the apparatus of the invention is a tubular reactor in which chevron baffles (23) are arranged. A settler (16) is arranged above the reactor, a regenerated catalyst conveying pipe (25) is arranged between the lower part of the regenerator (2) and the settler, and a cooler (27) is arranged on the regenerated catalyst conveying pipe. A heat-taking circulating pipe (15) is arranged outside the reactor, and a heat collector (14) is arranged on the heat-taking circulating pipe. A circulating inclined pipe is arranged between the bottom of the reactor and the lower part of the heat-taking circulating pipe, and a standby vertical pipe is arranged between the circulating inclined pipe and an inlet of the standby inclined pipe; the outlet of the spent inclined tube is connected with the lower part of the spent catalyst conveying pipe (6). The invention discloses a method for preparing gasoline from methanol in a fluidized bed by using the device. The reactor is internally provided with the herringbone baffle, the bottom of the reactor is provided with the feeding distributor, the catalyst bed layer is higher, and the problems of difficult fluidization of the catalyst and the like exist.
Chinese patent CN106794437A discloses an apparatus and process for producing gasoline, olefin and aromatic compounds from oxygenates, which invention provides an apparatus and process for converting oxygenate feedstocks such as methanol and dimethyl ether to hydrocarbons such as gasoline boiling components, olefin and aromatic compounds in a fluidized bed containing a catalyst. The invention has the problems that the reactor is a single reactor, and the catalyst bed layer is high, and the fluidization is difficult.
In summary, in the prior art, the product selectivity is improved to a certain extent by optimizing the internal structure of the reactor, optimizing the process flow and optimizing the operating conditions, but the device type in the prior art has the problems of high catalyst bed layer, difficult catalyst fluidization, difficult heat extraction and large selectivity in the reactor and the regenerator, and the invention specifically solves the problems.
Disclosure of Invention
The invention provides a device and a method for preparing gasoline by using an oxygen-containing compound, which are suitable for the characteristics of high temperature, pressurization, strong heat release, high conversion rate requirement, product selectivity requirement and the like of a process for preparing gasoline by using the oxygen-containing compound, and are used for solving the problems of high catalyst bed layer, difficult fluidization, different gas circulation requirement conditions and the like in the prior art, giving full play to the advantages of respective reactions to the greatest extent and improving the selectivity of target products.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
the device for preparing gasoline by using oxygen-containing compounds comprises a reactor, a regenerator, an external heat remover and a spent stripper, and is characterized in that: the reactor comprises a first reactor and a second reactor, the regenerator is connected with a regenerated catalyst conveying pipe through a regenerated slide valve, and the regenerated catalyst conveying pipe extends into the first reactor; the first reactor is communicated with the second reactor; the spent stripper is respectively communicated with the bottoms of the second reactor and the regenerator, and the second reactor is provided with an external heat remover; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator, and the second reactor is higher than the first reactor; and feeding distributors are arranged at the bottoms of the first reactor and the second reactor, and raw materials are introduced into the feeding distributors for distribution.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the regenerated catalyst transfer line may be used as a riser reactor. When light hydrocarbon is recycled, gas (C) is returned2～C4Gas), the regenerated catalyst conveying pipe can be used as a riser reactor, and the riser reactor is fed with preferably light hydrocarbon return gas (C)2～C4Gas), the riser reactor is provided with a light hydrocarbon return gas injection port, and light hydrocarbon return gas can be injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands. When the light hydrocarbon is not recycled, the gas (C) is returned2～C4Gas), the regenerated catalyst transfer line may be used to transfer regenerated catalyst, with the transfer medium preferably being steam.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle part and the lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor. A slide valve is arranged on the spent catalyst circulating pipe. The spent catalyst circulating pipe is an internal circulating pipe which is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the bottom of the second reactor, and an outlet is connected with the bottom of the first reactor. A plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are both fluidized bed reactors, preferably turbulent bed reactors. The second reactor is preferably a turbulent bed reactor and the first reactor may be a fast bed reactor or a turbulent bed reactor. Raw materials are adopted to respectively enter each reactor according to reaction requirements, and oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or a mixture of the light hydrocarbon gas, the methanol and the dimethyl ether enter the first reactor. The oxygen-containing compound such as light hydrocarbon gas, methanol, dimethyl ether and the like or the mixture of the two can also enter the second reactor, and the oxygen-containing compound is preferred.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are connected through a gas-solid distributor or a pipeline.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: one end of the spent stripper is communicated with the bottom of the second reactor through a spent agent inlet pipe, and the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe. A slide valve is arranged on the spent agent conveying pipe.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distributor. The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the feed distributor is positioned at the bottom of the first reactor and the second reactor and is a distribution pipe or a distribution plate, preferably a distribution pipe.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the interior of the second reactor is divided into a reactor dilute phase section, a reactor transition section and a reactor dense phase section from top to bottom.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and a gas-solid separation facility is arranged in the second reactor, an oil-gas collection chamber is arranged at the top of the second reactor, and the gas-solid separation facility is introduced into the oil-gas collection chamber.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the gas-solid separation device is a primary cyclone separator and a secondary cyclone separator, and the secondary cyclone separator is introduced into the oil gas collection chamber.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: a third cyclone, preferably external, is provided outside or inside the second reactor. Is coaxial with the reactor when being arranged in the second reactor; the reactor three-stage cyclone separator can be vertical or horizontal.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and a reactor fourth-stage cyclone separator is arranged outside the second reactor, one end of the reactor fourth-stage cyclone separator is communicated with the reactor third-stage cyclone separator, and the other end of the reactor fourth-stage cyclone separator is communicated with a reactor third-stage recovery catalyst storage tank.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator. The regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section. The regenerator char section may be a turbulent bed or a fast bed or a combination of both.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the dilute phase section of the regenerator is provided with a gas-solid separation device, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet.
The main wind distributor can be a distribution pipe or/and a distribution plate, preferably a distribution pipe. Not only the main wind is evenly distributed and is wear-resistant, but also the service life is long.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator, preferably a turbulent fluidized bed regenerator.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the gas-solid separation device in the regenerator is preferably a cyclone separator, and the cyclone separator is 1-3 grade.
The regeneration mode of the catalyst in the regenerator can adopt incomplete regeneration or complete regeneration, and preferably adopts incomplete regeneration.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and heat taking facilities are arranged in the regenerator, the first reactor and the second reactor.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: arranging internal and/or heat-taking facilities in the first reactor and the second reactor, wherein the internal heat-taking and heat-taking medium can be one or more of an oxygen-containing compound raw material, water, an inert medium and heat conducting oil, preferably, the oxygen-containing compound raw material is used as the heat-taking medium, the oxygen-containing compound raw material is preferably a liquid-phase raw material, and the temperature can be within the range of 25-200 ℃, preferably, within the range of 25-150 ℃; the internal heat extraction facility is arranged at the middle lower part of the reaction section of each reactor and above the feeding distributor of the reactor. The external heat-removal means may be provided in consideration of the fact that the lower catalyst is returned to any of the upper, middle and lower portions of the first reactor, preferably the middle portion. And an external heat taking facility is arranged in the second reactor, and the heat taking medium is preferably deoxygenated water so as to generate steam with different grades.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: an external heat taking facility is arranged in the regenerator, and the heat taking medium is preferably deoxygenated water so as to generate steam with different grades.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the first reactor, the second reactor and the regenerator are all high beds, and the ratio of the height of the catalyst bed in the dense-phase section of the reactor to the diameter of the dense-phase section of the reactor is within the range of 0.5-20.0, preferably within the range of 1-10. The ratio of the height of the catalyst bed in the dense phase section of the regenerator to the diameter of the dense phase section of the regenerator is in the range of 0.5 to 30.0, preferably in the range of 1 to 20.
The reactor of the device for preparing gasoline by using oxygen-containing compounds is a multistage series reactor and comprises a first reactor and a second reactor, wherein the reactors can be fast bed reactors or turbulent beds, and the first reactor and the second reactor can be connected by using a gas-solid distributor. Raw materials are adopted to respectively enter each reactor according to reaction requirements, and oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or a mixture of the light hydrocarbon gas, the methanol and the dimethyl ether enter the first reactor. The oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or the mixture of the light hydrocarbon gas, the methanol, the dimethyl ether and the like can also enter the second reactor. Oxygen-containing compounds are preferred.
The invention also provides a method for preparing gasoline by using the oxygenated chemicals, which is carried out by the device for preparing gasoline by using the oxygenated chemicals, and specifically comprises the following steps:
a method for preparing gasoline by using oxygenated chemicals is characterized by comprising the following steps:
1) preheating reaction raw materials, then feeding the preheated reaction raw materials into a first reactor, directly contacting the reaction raw materials with a high-temperature catalyst from a regenerated catalyst conveying pipe in the first reactor, quickly reacting under the action of the catalyst, and feeding reaction products into a second reactor through the top of the first reactor;
2) preheating reaction raw materials, then feeding the preheated reaction raw materials into a second reactor for reaction, removing most of carried catalyst from reaction products fed into the second reactor in the step 1) through a gas-solid separation facility of the second reactor, removing the carried catalyst through a three-stage cyclone separator of the reactor and a four-stage cyclone separator of the reactor, and then leading out;
3) the spent catalyst in the second reactor enters an external heat collector for heat extraction; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor, and a slide valve or a plug valve is arranged on the spent catalyst circulating pipe to control the circulating amount of the spent catalyst;
4) the spent catalyst which loses activity after reaction enters a spent stripper for stripping reaction gas carried by the spent catalyst, and the spent catalyst after stripping enters a regenerator through a spent conveying pipe;
5) after the spent catalyst in the regenerator contacts with the main air in a countercurrent manner for burning, the regenerated catalyst enters a regenerated catalyst conveying pipe through a regeneration slide valve and then enters a first reactor and a second reactor.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the reaction raw material entering the first reactor is an oxygen-containing compound single feed or a mixed feed of the oxygen-containing compound and light hydrocarbon return gas. The reaction feedstock entering the second reactor is an oxygenate and/or light hydrocarbon return gas, preferably an oxygenate.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the oxygen-containing compound is an oxygen-containing compound mainly comprising methanol or dimethyl ether, and the light hydrocarbon return gas is C2-C4 gas.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are both fluidized bed reactors,
the invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the regenerated catalyst conveying pipe can also be used as a riser reactor, and light hydrocarbon return gas can be injected when the regenerated catalyst conveying pipe is used as the riser reactor, and the light hydrocarbon return gas can be injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands (2-5 strands).
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: a light hydrocarbon return gas injection port is arranged on the raw material feeding pipe, and light hydrocarbon return gas enters the reactor through the raw material feeding pipe independently or after being mixed with the oxygen-containing compound.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor. A slide valve is arranged on the spent catalyst circulating pipe.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the spent catalyst circulating pipe is an internal circulating pipe which is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the lower part of the second reactor, and an outlet is connected with the lower part of the first reactor. A plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and 2) removing the entrained catalyst from the reaction product in the step 2) through a reactor three-stage cyclone separator and a reactor four-stage cyclone separator, leading out, and sending to a rear quenching and water washing system after heat exchange. The catalyst recovered by the reactor three-stage cyclone separator and the reactor four-stage cyclone separator enters a reactor three-cyclone recovery catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a discharging agent pipeline.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the reaction product in the step 2) enters a second reactor through a gas-solid distributor at the top of the first reactor to continue to react,
the invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and 4) a stripping grating or a stripping baffle plate and a stripping medium distributor are arranged in the spent stripper.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: and 5) removing most of carried catalyst from the flue gas generated after the catalyst and main air are contacted and burned in a countercurrent mode through a two-stage cyclone separator, discharging the flue gas, sending the flue gas to a waste heat boiler through a pressure reducing valve (if needed), a double-acting slide valve and a pressure reducing pore plate to recover heat, and exhausting the flue gas to atmosphere through a chimney.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: an internal heat-taking facility is arranged in the first reactor, an internal and/or external heat-taking facility is arranged in the second reactor, and an external heat-taking device is arranged outside the regenerator.
The invention relates to a device for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator, preferably a turbulent fluidized bed regenerator.
The regeneration mode of the catalyst in the regenerator can adopt incomplete regeneration or complete regeneration, and preferably adopts incomplete regeneration.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the reaction temperature is within the range of 250-650 ℃, preferably within the range of 300-500 ℃; the regeneration temperature is in the range of 350-700 ℃, preferably 450-650 ℃; the reaction pressure is in the range of 0.1-3.0 MPaG, preferably in the range of 0.1-2.0 MPaG; the regeneration pressure is in the range of 0.1-3.0 MPaG, preferably in the range of 0.1-2.0 MPaG.
The invention relates to a method for preparing gasoline by using oxygen-containing compounds, which is further characterized in that: the temperature of the reaction gas three-stage cyclone separator is within the range of 300-600 ℃, preferably within the range of 400-500 ℃; the pressure is in the range of 0.1 to 3.0MPaG, preferably in the range of 0.4 to 2.0 MPaG.
The device for preparing the gasoline by using the oxygen-containing compound better solves the problems of high catalyst bed layer, difficult catalyst fluidization, difficult heat extraction and poor selectivity in the prior art, and can be used in the industrial production of preparing liquid products by converting the oxygen-containing compound, such as: MTA process (methanol to aromatics process), MTG process (methanol to gasoline process), and the like. In addition, the equipment has the advantages of simple structure, easy realization, wide application range, low equipment investment and the like, and can be widely applied to devices for preparing liquid products by converting oxygen-containing compounds.
Compared with the prior art, the invention has the advantages that:
(1) the device provided by the invention can improve the selectivity of target products, such as the selectivity and yield of gasoline products to the maximum extent;
(2) by adopting the device provided by the invention, the problems of high bed layer and difficult fluidization of the catalyst in the reactor and the regenerator are solved, and the fluidization state is maintained;
(3) the device provided by the invention can meet the requirements of reaction regeneration conditions of the MTG process. Namely, the reaction gas has long retention time, the catalyst has long retention time and the catalyst has low circulation volume. The reaction condition and the regeneration condition can be effectively controlled, the problem of reaction heat extraction caused by high pressure and strong heat release is solved, and the heat balance of the device can be realized. Simple operation and low equipment investment.
The invention is further described with reference to the following figures and detailed description. But not to limit the scope of the invention.
Drawings
FIG. 1 is a diagram of an apparatus for producing gasoline from an oxygenate according to the present invention.
The reference symbols shown in the figures are: 1-regenerated catalyst conveying pipe, 2-light hydrocarbon return gas, 3-raw material feeding pipe, 4-external heat collector, 5-external heat-collecting inlet pipe, 6-second reactor internal heat-collecting facility, 7-reactor dense-phase section, 8-reactor transition section, 9-reactor dilute-phase section, 10-reactor gas-solid separation facility, 11-waste catalyst, 12-reactor triple-rotation recovered catalyst storage tank, 13-reactor four-stage cyclone separator, 14-reactor four-stage cyclone separator outlet gas, 15-reactor three-stage cyclone separator, 17-reaction oil gas, 18-oil gas collection chamber, 19-spent agent inlet pipe, 20-flue gas, 21-regenerator separation facility, 22-regenerator, 23-regenerator dilute-phase section, 24-a regenerator transition section, 25-a regenerator burning section, 26-a regenerator external heat taking inlet and outlet, 27-a regenerator external heat taking device, 28-main air, 29-conveying gas or raw materials, 30-a regeneration slide valve, 31-a spent slide valve, 32-a spent agent conveying pipe, 33-a spent stripper, 34-a feeding distributor I, 35-a main air distributor, 36-a feeding distributor II, 37-a spent slide valve II/plug valve, 38-a spent catalyst circulating pipe, 39-a first reactor, 40-a second reactor, 41-a gas-solid distributor and 42-a heat taking facility in the first reactor.
Detailed Description
As shown in fig. 1, the device for preparing gasoline from oxygen-containing compounds comprises a first reactor 39, a second reactor 40, a regenerator 22, a reactor third-stage cyclone 15, a reactor fourth-stage cyclone 13, a reactor third-stage recovery catalyst storage tank 12, a spent stripper 33, an external heat remover 4 and an external regenerator 27. The first reactor 39 is communicated with the second reactor 40 through a gas-solid distributor 41, and the first reactor 39 is communicated with the spent catalyst circulating pipe 38 and the regenerated catalyst conveying pipe 1; the second reactor 40 is communicated with the spent stripper 33, the external heat collector 4 and the reactor tertiary cyclone separator 15; the second reactor 40 is provided with an external heat collector 4, and is connected with the second reactor 40 through an external heat outlet inlet pipe 5. The regenerator 22 is communicated with a regenerated catalyst conveying pipe 1, a regenerator external heat remover 27 and a spent agent conveying pipe 32. The regenerator 22 is provided with an external regenerator 27 and is connected to the regenerator 22 through an external regenerator heat inlet/outlet 26.
The first reactor 39 and the second reactor 40 are arranged coaxially and in parallel with the regenerator 22, the second reactor 40 being higher than the first reactor 39; the bottom of the first reactor 39 is provided with a raw material feeding pipe 3 and a first feeding distributor 34, the bottom of the second reactor 40 is provided with a raw material feeding pipe 3 and a second feeding distributor 36, and the raw material feeding pipe 3 is introduced into the feeding distributors for distribution.
One end of the spent stripper 33 is communicated with the bottom of the second reactor 40 through a spent agent inlet pipe 19, and the other end is communicated with the regenerator 22 through a spent agent conveying pipe 32. The second reactor 40 is internally provided with a reactor gas-solid separation facility 10. The regenerator 22 is internally provided with a regenerator gas-solid separation facility 21. The regenerator 22 is provided with a regenerator external heat remover 27; the first reactor 39 is provided with internal and external heat-taking facilities, preferably a first reactor internal heat-taking facility 42; the second reactor 40 is provided with internal and external heat-taking means, preferably the internal heat-taking means 6 of the second reactor.
A spent catalyst circulation pipe 38 is provided between the first reactor 39 and the second reactor 40. When the spent catalyst circulating pipe 38 is an external circulating pipe, the inlet of the external circulating pipe is connected with the bottom of the second reactor 40, the outlet of the external circulating pipe is connected with the bottom of the first reactor 39, and a spent slide valve II 37 is arranged on the spent catalyst circulating pipe 38. When the spent catalyst circulation pipe 38 is an internal circulation pipe, the internal circulation pipe is arranged at the middle part of the first reactor 39 and is coaxially arranged with the first reactor, the inlet is connected with the bottom of the second reactor 40, and the outlet is connected with the bottom of the first reactor 39. A plug valve 37 is arranged on the spent catalyst circulating pipe 38 and is positioned at the bottom of the first reactor 39. The interior of the second reactor 40 is divided into a reactor dilute phase section 9, a reactor transition section 8 and a reactor dense phase section 7 from top to bottom. The top of the second reactor 40 is provided with an oil gas collection chamber 18, and the reaction oil gas 17 is introduced into the oil gas collection chamber 18 through the reactor gas-solid separation facility 10.
The regenerator 22 is internally divided into a regenerator dilute phase section 23, a regenerator transition section 24 and a regenerator char section 25. The regenerator char section 25 may be a turbulent bed or a fast bed or a combination of both. The regenerator dilute phase section 23 is provided with a regenerator gas-solid separation facility 21, the top of the regenerator dilute phase section is provided with a flue gas 20 outlet, the regeneration and burning section 25 is provided with a main air distributor 35, and the bottom of the regenerator is provided with a main air 28 inlet.
Preheating oxygen-containing compounds mainly including methanol or dimethyl ether and light hydrocarbon return gas 2, then entering a first feeding distributor 34 in a first reactor 39 from a raw material feeding pipe 3, directly contacting the oxygen compounds in the first reactor 39 with a high-temperature regenerated catalyst from a regenerated catalyst conveying pipe 1, and rapidly reacting under the action of the catalyst; the reaction product enters a second reactor 40 through a gas-solid distributor 41 at the top of the first reactor 39 to continue to react; and a part of preheated oxygen-containing compounds mainly containing methanol or dimethyl ether also enter the second reactor 40 for reaction, most of carried catalyst is removed from reaction products through a reactor gas-solid separation facility 10, the carried catalyst is removed through a reactor three-stage cyclone separator 15 and a reactor four-stage cyclone separator 13, the reaction products are led out, and the reaction products are sent to a rear quenching and water washing system after heat exchange. The reactor gas-solid separation facility 10 is a two-stage cyclone separator.
The catalyst recovered by the reactor three-stage cyclone separator 15 and the reactor four-stage cyclone separator 13 enters a reactor three-cycle recovered catalyst storage tank 12, and the waste catalyst 11 enters a waste catalyst tank through a discharging pipeline.
The spent catalyst enters a spent stripper 33 for stripping, and a stripping grid or a stripping baffle plate and a stripping medium distribution ring are arranged in the spent stripper 33. The device is used for stripping reaction gas carried by spent catalyst, and the stripped spent catalyst enters a spent agent conveying pipe 32 after passing through a spent slide valve 31 and then enters the regenerator 22. After the coke is burned in the regenerator 22 by counter-current contact with the main air 28, the regenerated catalyst enters the first reactor 39 and the second reactor 40 through the regenerated catalyst conveying pipe 1 for reaction. The regenerated flue gas 20 is passed through a regenerator gas-solid separation facility 21 to remove most of the carried catalyst, then passed through a pressure reducing valve (if necessary), a double-acting slide valve and a pressure reducing orifice plate, and then sent to a waste heat boiler to recover heat, and then discharged to atmosphere through a chimney.
Raw materials are respectively fed into each reactor according to the reaction requirements, and oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or a mixture of the light hydrocarbon gas, the methanol and the dimethyl ether are fed into the first reactor 39. The oxygen-containing compound entering the second reactor 40 may be light hydrocarbon gas, methanol, dimethyl ether, or a mixture thereof. Oxygen-containing compounds are preferred. The regenerated catalyst conveying pipe 1 can also be used as a riser reactor, and light hydrocarbon return gas 2 (C) can enter the riser reactor2～C4Gas), the injection position of the light hydrocarbon return gas 2, can be arranged on the raw material feeding pipe 3, and the light hydrocarbon return gas and the raw material feeding pipe are mixed and then enter the first reactor 39 or the second reactor 40 together; or can be arranged at the upper part, the middle part or/and the lower part of the riser reactor, and can be divided into one or more light hydrocarbon return gases. When light hydrocarbon returns to gas (C)2～C4Gas) is not recycled into the regenerated catalyst transfer pipe 1, the regenerated catalyst transfer pipe is used for transferring the regenerated catalyst, and the transfer medium 29 is preferably steam.

Claims (31)

1. The utility model provides a make petrol device with oxygenated chemicals, includes reactor, regenerator, external cooler and spent stripper, its characterized in that: the reactor comprises a first reactor and a second reactor, the regenerator is connected with a regenerated catalyst conveying pipe through a regenerated slide valve, and the regenerated catalyst conveying pipe extends into the first reactor; the first reactor is communicated with the second reactor; the spent stripper is respectively communicated with the bottoms of the second reactor and the regenerator, and the second reactor is provided with an external heat remover; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator, and the second reactor is higher than the first reactor; and feeding distributors are arranged at the bottoms of the first reactor and the second reactor, and raw materials are introduced into the feeding distributors for distribution.
2. The apparatus according to claim 1, wherein: the regenerated catalyst conveying pipe is used as a riser reactor, and light hydrocarbon return gas injection ports are arranged at the upper part, the middle part or the lower part of the riser reactor.
3. The apparatus according to claim 1, wherein: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor; a slide valve is arranged on the spent catalyst circulating pipe.
4. The apparatus according to claim 1, wherein: the spent catalyst circulating pipe is an internal circulating pipe which is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the bottom of the second reactor, and an outlet is connected with the bottom of the first reactor; a plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
5. The apparatus according to claim 1, wherein: the first reactor and the second reactor are both fluidized bed reactors.
6. The apparatus according to claim 1, wherein: the first reactor and the second reactor are connected through a gas-solid distributor or a pipeline.
7. The apparatus according to claim 1, wherein: one end of the spent stripper is communicated with the bottom of the second reactor through a spent agent inlet pipe, the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe, and a slide valve is arranged on the spent agent conveying pipe.
8. The apparatus according to claim 7, wherein: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distributor.
9. The apparatus according to claim 1, wherein: the feeding distributor is positioned at the bottom of the first reactor and the second reactor and is a distribution pipe or a distribution plate.
10. The apparatus according to claim 1, wherein: the interior of the second reactor is divided into a reactor dilute phase section, a reactor transition section and a reactor dense phase section from top to bottom.
11. The apparatus according to claim 1, wherein: and a gas-solid separation facility is arranged in the second reactor, an oil-gas collection chamber is arranged at the top of the second reactor, and the gas-solid separation facility is introduced into the oil-gas collection chamber.
12. The apparatus according to claim 11, wherein: the gas-solid separation facility is a primary cyclone separator and a secondary cyclone separator.
13. The apparatus according to claim 1, wherein: and a third-stage cyclone separator is arranged outside the second reactor, and the third-stage cyclone separator of the reactor is vertical or horizontal.
14. The apparatus according to claim 13, wherein: and a reactor fourth-stage cyclone separator is arranged outside the second reactor, one end of the reactor fourth-stage cyclone separator is communicated with the reactor third-stage cyclone separator, and the other end of the reactor fourth-stage cyclone separator is communicated with a reactor third-stage recovery catalyst storage tank.
15. The apparatus according to claim 1, wherein: the regenerator is a fluidized bed regenerator, and the regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section.
16. The apparatus according to claim 15, wherein: the dilute phase section of the regenerator is provided with a gas-solid separation device, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet.
17. The apparatus according to claim 1, wherein: and heat taking facilities are arranged in the regenerator, the first reactor and the second reactor.
18. The apparatus of claim 17, wherein the oxygenate comprises: an internal heat taking facility is arranged in the first reactor, and an internal and/or heat taking facility is arranged in the second reactor, is arranged at the middle lower part of each reactor and is arranged above the feeding distributor of the reactor; an external heat-taking facility is arranged outside the regenerator.
19. The apparatus according to claim 1, wherein: the first reactor, the second reactor and the regenerator are all high beds, and the ratio of the height of a catalyst bed in the dense-phase section of the reactor to the diameter of the dense-phase section of the reactor is 0.5-20.0; the ratio of the height of the catalyst bed in the dense-phase section of the regenerator to the diameter of the dense-phase section of the regenerator is 0.5 to 30.0.
20. A method for preparing gasoline by using oxygenated chemicals is characterized by comprising the following steps:
1) preheating reaction raw materials, then feeding the preheated reaction raw materials into a first reactor, directly contacting the reaction raw materials with a high-temperature catalyst from a riser reactor in the first reactor, quickly reacting under the action of the catalyst, and feeding a reaction product into a second reactor through the top of the first reactor;
2) preheating reaction raw materials, then feeding the preheated reaction raw materials into a second reactor for reaction, removing most of carried catalyst from reaction products fed into the second reactor in the step 1) through a gas-solid separation facility of the second reactor, removing the carried catalyst through a three-stage cyclone separator of the reactor and a four-stage cyclone separator of the reactor, and then leading out;
3) the spent catalyst in the second reactor enters an external heat collector for heat extraction; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor, and a slide valve or a plug valve is arranged on the spent catalyst circulating pipe to control the circulating amount of the spent catalyst;
4) the spent catalyst which loses activity after reaction enters a spent stripper for stripping reaction gas carried by the spent catalyst, and the spent catalyst after stripping enters a regenerator through a spent conveying pipe;
5) after the spent catalyst in the regenerator contacts with the main air in a countercurrent manner for burning, the regenerated catalyst enters a regenerated catalyst conveying pipe through a regeneration slide valve and then enters a first reactor and a second reactor.
21. The method of making gasoline from oxygenates of claim 20 wherein: the reaction raw material entering the first reactor is an oxygen-containing compound single feed or a mixed feed of the oxygen-containing compound and light hydrocarbon return gas. The reaction raw material entering the second reactor is an oxygen-containing compound and/or light hydrocarbon return gas.
22. The method of claim 20, wherein the oxygenate is selected from the group consisting of: the oxygen-containing compound is an oxygen-containing compound mainly comprising methanol or dimethyl ether, and the light hydrocarbon return gas is C2-C4 gas.
23. The method of claim 20, wherein the oxygenate is selected from the group consisting of: the regenerated catalyst conveying pipe is used as a riser reactor, light hydrocarbon return gas is injected when the regenerated catalyst conveying pipe is used as the riser reactor, and the light hydrocarbon return gas is injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands.
24. The method of claim 20, wherein the oxygenate is selected from the group consisting of: the first reactor and the second reactor are fluidized bed reactors; the regenerator is a fluidized bed regenerator.
25. The method of claim 20, wherein the oxygenate is selected from the group consisting of: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor. A slide valve is arranged on the spent catalyst circulating pipe.
26. The method of claim 20, wherein the oxygenate is selected from the group consisting of: the spent catalyst circulating pipe is an internal circulating pipe, the internal circulating pipe is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the lower part of the second reactor, an outlet is connected with the lower part of the first reactor, and a plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
27. The method of claim 20, wherein the oxygenate is selected from the group consisting of: removing the entrained catalyst from the reaction product obtained in the step 2) by a reactor three-stage cyclone separator and a reactor four-stage cyclone separator, leading out, and sending to a rear quenching and water washing system after heat exchange; the catalyst recovered by the reactor three-stage cyclone separator and the reactor four-stage cyclone separator enters a reactor three-cyclone recovery catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a discharging agent pipeline.
28. The method of making gasoline from an oxygenate according to claim 20, wherein: and 2) allowing the reaction product to enter a second reactor through a gas-solid distributor at the top of the first reactor for continuous reaction.
29. The method of claim 20 for making gasoline from oxygenates, characterized in that: and 5) removing most of carried catalyst from the regenerated flue gas by a two-stage cyclone separator, discharging, sending to a waste heat boiler through a pressure reducing valve, a double-acting slide valve and a pressure reducing pore plate, recovering heat, and discharging the air through a chimney.
30. The method of claim 20 for making gasoline from oxygenates, characterized in that: the reaction temperature is within the range of 250-650 ℃; the regeneration temperature is in the range of 350-700 ℃; the reaction pressure is in the range of 0.1-3.0 MPaG; the regeneration pressure is in the range of 0.1-3.0 MPaG.
31. The method of claim 30 for making gasoline from oxygenates, characterized in that: the reaction temperature is within the range of 300-500 ℃; the regeneration temperature is in the range of 450-650 ℃; the reaction pressure is in the range of 0.1-2.0 MPaG; the regeneration pressure is in the range of 0.1-2.0 MPaG.
CN201810888047.4A 2018-08-07 2018-08-07 Device and method for preparing gasoline by using oxygen-containing compound Active CN110819373B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810888047.4A CN110819373B (en) 2018-08-07 2018-08-07 Device and method for preparing gasoline by using oxygen-containing compound

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810888047.4A CN110819373B (en) 2018-08-07 2018-08-07 Device and method for preparing gasoline by using oxygen-containing compound

Publications (2)

Publication Number Publication Date
CN110819373A true CN110819373A (en) 2020-02-21
CN110819373B CN110819373B (en) 2021-12-14

Family

ID=69533791

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810888047.4A Active CN110819373B (en) 2018-08-07 2018-08-07 Device and method for preparing gasoline by using oxygen-containing compound

Country Status (1)

Country Link
CN (1) CN110819373B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114425281A (en) * 2020-10-29 2022-05-03 中国石油天然气股份有限公司 Internal circulation slurry bed reactor

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202754917U (en) * 2012-07-09 2013-02-27 中国石油化工集团公司 Device for producing low carbon olefin from oxy-compound
CN104945211A (en) * 2014-10-08 2015-09-30 青岛京润石化工程有限公司 Heat extraction and catalyst circulation method in catalytic reaction for preparing hydrocarbons from methanol
CN105018129A (en) * 2014-04-18 2015-11-04 中石化洛阳工程有限公司 Device and method for producing gasoline from methyl alcohol by fluidized bed
CN107540495A (en) * 2016-06-29 2018-01-05 中国石油化工股份有限公司 Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene
CN108017487A (en) * 2016-11-04 2018-05-11 中国石油化工股份有限公司 Method containing oxygen-containing compound material aromatic hydrocarbons two-stage reaction
CN207581697U (en) * 2017-08-31 2018-07-06 中国石油化工股份有限公司 Reaction-regenerative device

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202754917U (en) * 2012-07-09 2013-02-27 中国石油化工集团公司 Device for producing low carbon olefin from oxy-compound
CN105018129A (en) * 2014-04-18 2015-11-04 中石化洛阳工程有限公司 Device and method for producing gasoline from methyl alcohol by fluidized bed
CN104945211A (en) * 2014-10-08 2015-09-30 青岛京润石化工程有限公司 Heat extraction and catalyst circulation method in catalytic reaction for preparing hydrocarbons from methanol
CN107540495A (en) * 2016-06-29 2018-01-05 中国石油化工股份有限公司 Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene
CN108017487A (en) * 2016-11-04 2018-05-11 中国石油化工股份有限公司 Method containing oxygen-containing compound material aromatic hydrocarbons two-stage reaction
CN207581697U (en) * 2017-08-31 2018-07-06 中国石油化工股份有限公司 Reaction-regenerative device

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114425281A (en) * 2020-10-29 2022-05-03 中国石油天然气股份有限公司 Internal circulation slurry bed reactor

Also Published As

Publication number Publication date
CN110819373B (en) 2021-12-14

Similar Documents

Publication Publication Date Title
CN110818521B (en) Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound
CN108017496B (en) Apparatus for producing olefins and aromatic hydrocarbons and method thereof
CN101544529B (en) Method and equipment for pre-treatment of reaction produced gas in olefin preparation technology by oxygen-containing compounds
CN111807916B (en) Device for producing low-carbon olefin by efficient oxygen-containing compound
CN110818522B (en) Device and method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compound
CN111875465B (en) Method for producing low-carbon olefin by oxygen-containing compound
CN110819373B (en) Device and method for preparing gasoline by using oxygen-containing compound
CN102268286A (en) C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device
CN101164685B (en) Combined quickly fluidized bed reactor
CN111871343A (en) Device for producing low-carbon olefin by using oxygen-containing compound
CN110950730B (en) Method and equipment for improving selectivity of low-carbon olefin
CN110819375B (en) Device and method for preparing gasoline from oxygen-containing compound
CN110819374B (en) Device and method for preparing gasoline from oxygen-containing compound
CN111875464B (en) Method for producing low-carbon olefin by high-efficiency oxygen-containing compound
CN102276389B (en) Reaction and regeneration device for catalyzing and converting methanol and naphtha into lower olefins
CN102276391B (en) Method for catalyzing and converting methanol and naphtha into low-carbon olefins
CN110818520B (en) Device and method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compound
CN101659600B (en) Method and device of a combined process for producing dimethyl ether by methanol and catalytic cracking
CN102276399B (en) Method for producing lower olefins from methanol and naphtha
CN113509897A (en) Device of low carbon olefin of high efficiency oxygen compound production
CN115992005B (en) Reaction method and reactor for preparing low-carbon olefin and aromatic hydrocarbon by catalytic conversion of hydrocarbon raw material as reaction raw material
CN102875297B (en) The method of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha
CN113354496A (en) Device for producing low-carbon olefin by using oxygen-containing compound
CN115992004B (en) Reaction method and reactor for preparing low-carbon olefin and aromatic hydrocarbon by catalytic conversion of hydrocarbon raw material as reaction raw material
CN102875304A (en) Method for preparing low carbon olefins from methanol and naphtha

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant