CN114479904B - Combined conversion reaction flow of methanol and light hydrocarbon components - Google Patents
Combined conversion reaction flow of methanol and light hydrocarbon components Download PDFInfo
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- CN114479904B CN114479904B CN202210217262.8A CN202210217262A CN114479904B CN 114479904 B CN114479904 B CN 114479904B CN 202210217262 A CN202210217262 A CN 202210217262A CN 114479904 B CN114479904 B CN 114479904B
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 334
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 120
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 120
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 120
- 238000006243 chemical reaction Methods 0.000 claims abstract description 71
- 239000003054 catalyst Substances 0.000 claims abstract description 33
- 239000007795 chemical reaction product Substances 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 10
- 239000003502 gasoline Substances 0.000 claims description 7
- 125000003118 aryl group Chemical group 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 5
- 229930195734 saturated hydrocarbon Natural products 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 2
- 230000018044 dehydration Effects 0.000 claims 1
- 238000006297 dehydration reaction Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 claims 1
- 230000008878 coupling Effects 0.000 abstract description 4
- 238000010168 coupling process Methods 0.000 abstract description 4
- 238000005859 coupling reaction Methods 0.000 abstract description 4
- 230000009849 deactivation Effects 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 4
- 230000002860 competitive effect Effects 0.000 abstract description 2
- 238000009826 distribution Methods 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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
- C10G3/42—Catalytic treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst 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
-
- 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
- C10G3/60—Controlling or regulating the processes
-
- 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)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention relates to a combined conversion reaction flow of methanol and light hydrocarbon components, which mainly solves the problems of side effects caused by the reaction of the methanol and the light hydrocarbon components under the same catalyst, the same reactor and the same operation condition in the prior art, such as compatibility of the catalyst components, competitive activity of active centers, hydrothermal deactivation of the catalyst and low reaction efficiency caused by uneven temperature distribution of a reaction bed. According to the invention, by adopting two parallel tubular fixed bed reactors, methanol and light hydrocarbon components are separately fed, and are independently reacted, and countercurrent heat exchange is performed, so that not only can heat coupling utilization be realized, energy sources be saved, but also the temperature of a catalyst bed layer can be maintained uniform, personalized catalyst configuration is implemented, the respective reaction performance is improved, and the problems are well solved.
Description
Technical Field
The invention relates to the technical field of petrochemical production, in particular to a methanol and light hydrocarbon component combined conversion reaction flow.
Background
Light hydrocarbon components (mainly C5-C7 saturated hydrocarbon components) such as aromatic raffinate oil, reforming topped oil and hydrogenated light petroleum oil which are byproducts of petrochemical enterprises, are light in weight and high in vapor pressure, and simultaneously are rich in normal paraffins with low octane number, and the research octane number is low, so that the petroleum extract can not be used for blending the motor gasoline. For enterprises without ethylene devices, the light hydrocarbon components have no better outlet and can only be taken as cheap fuel for take-out, if the low-value light hydrocarbon components are processed and converted into isoparaffin and aromatic hydrocarbon with higher values, the isoparaffin and aromatic hydrocarbon are converted into the high-octane blending component of the vehicle oil, so that the problem of light hydrocarbon component utilization is solved, and a new way is opened for the production of the vehicle gasoline.
On the other hand, methanol is the only chemical synthesized on a large scale from coal gasification and natural gas reforming, except for ammonia synthesis, and becomes a main product of coal chemical industry and natural gas chemical industry and a main route for clean utilization of coal. The excess capacity of methanol can be effectively digested, and the industrial chain is extended to the petrochemical field, but the independent construction investment of the device is large, the risk is high, and the economical efficiency and the competitiveness of the device are greatly limited by the market price of methanol and oil products especially when the price of crude oil is continuously low.
The existing refining device and public engineering are used for co-converting methanol and light hydrocarbon components, and a series of complex chemical reactions (such as cracking, polymerization, dehydrogenation, cyclization, aromatization and the like) are used for producing a high-octane gasoline component or an aromatic chemical component, so that raw materials for producing aromatic chemical industry can be widened, the quality of gasoline is improved, and reasonable utilization of resources is realized; in the existing methanol and light hydrocarbon component co-conversion technology, the light hydrocarbon component and methanol carry out chemical reaction by using the same acidic molecular sieve catalyst, on one hand, the heat released by the conversion of the methanol is provided for the conversion of the light hydrocarbon component by the co-reaction of the methanol and the light hydrocarbon component, so that the heat coupling is realized, the total heat effect of a system can be reduced, and the energy is saved; on the other hand, the co-reaction of the methanol and the light hydrocarbon component can realize the organic combination of coal chemical industry, natural gas chemical industry and petrochemical industry, and the reaction product can be used as a high-octane gasoline blending component or an aromatic hydrocarbon chemical raw material, but in the prior conversion technology, the mixed feeding of the methanol and the light hydrocarbon component is carried out under the same reactor, the same catalyst and the same operation condition (reaction temperature, reaction pressure and reaction airspeed), and at least has the following problems:
(1) The methanol conversion is a strong exothermic reaction, heat needs to be removed in time to maintain the reaction temperature, the light hydrocarbon component conversion is an endothermic reaction, heat needs to be continuously supplemented to maintain the reaction temperature, the methanol conversion amount and the light hydrocarbon conversion amount are necessarily influenced by heat balance to be mutually restricted, and the feeding proportion of the two components is difficult to reasonably control;
(2) The chemical reaction mechanism and reaction process of the conversion of methanol and the conversion of light hydrocarbon components are not completely the same, and in order to maintain the respective high reactivity and selectivity, the requirements of the two components on the active components and the functional modification components in the catalyst are different, so that the compatibility of the catalyst is a problem;
(3) The methanol is chemically converted at high temperature to generate a large amount of water, the catalyst is in environments such as high temperature, high water vapor partial pressure and the like, and has the problem of hydrothermal deactivation, so that the catalyst is required to have strong water-heat deactivation resistance, the chemical conversion of light hydrocarbon components is a strong endothermic reaction, and no water is generated in the reaction process;
(4) The reaction conditions of methanol conversion and light hydrocarbon component conversion are obviously unsuitable due to different reaction mechanisms and reaction courses, and the problem of synergetic reaction conditions exists due to the adoption of the same operation conditions;
(5) Methanol and light hydrocarbon components are mixed into the same reactor to react, share the same type of active center, inevitably have a competitive problem, and influence the reaction efficiency.
Disclosure of Invention
The invention aims to solve the technical problems of low reaction efficiency caused by the compatibility of the components of the catalyst, the competition of the active center, the hydrothermal deactivation of the catalyst and the uneven temperature distribution of a reaction bed, which are caused by the same catalyst, the same reactor and the same operation condition in the prior art, and provides a new methanol and light hydrocarbon component combined conversion reaction flow. The process is used for producing the high-octane gasoline component or the chemical aromatic component by the combined conversion of the high-methanol and the light component, and has the advantages of realizing heat energy coupling, saving energy, reducing consumption, realizing personalized configuration of the catalyst, prolonging the service life of the catalyst and ensuring uniform temperature of a reaction bed.
In order to solve the technical problems, the invention adopts the following technical scheme: a combined conversion reaction process of methanol and light hydrocarbon components comprises the steps of feeding the light hydrocarbon components (mainly C5-C7 saturated hydrocarbon) and methanol into a light hydrocarbon buffer tank 2 in two paths, pumping the light hydrocarbon components from the light hydrocarbon feed pipeline 1 into the light hydrocarbon buffer tank 2 by a light hydrocarbon pump 3, pressurizing the light hydrocarbon components, conducting heat exchange through a tube pass of a light hydrocarbon preheater 4, heating the light hydrocarbon components to a required temperature by a light hydrocarbon heating furnace 5, feeding the light hydrocarbon components from one end of the tube pass of the light hydrocarbon converter 7, conducting chemical reaction, discharging the light hydrocarbon reaction products from the other end of the tube pass of the light hydrocarbon converter 7, feeding the light hydrocarbon reaction products from one end of a shell pass of the methanol converter 6, conducting heat exchange, discharging the light hydrocarbon reaction products from the other end of the shell pass of the methanol converter 6, feeding the methanol into a methanol buffer tank 10 from a methanol feed pipeline 9, pumping the methanol pump 11 from the bottom of the methanol buffer tank 10, pressurizing the methanol preheater 12, conducting heat exchange through the tube pass of the methanol preheater 13, heating the light hydrocarbon heater to the required temperature, feeding the methanol components from one end of the methanol converter 6, conducting chemical reaction, discharging the other end of the methanol converter 6, discharging the methanol reaction products from the other end of the light hydrocarbon converter after the chemical reaction products, discharging the light hydrocarbon reaction products from one end of the shell pass through the methanol converter 6, the other end of the heat exchanger, discharging the two heat-pass through the methanol heater 6, and then discharging the two heat-pass through the two-pass heater, and then the two-pass through the two-pass heater, and is mixed layers of the two-channel is separated.
In the above technical scheme, preferably, the methanol converter 6 is a tubular fixed bed reactor, the tube is filled with a methanol conversion catalyst, and the light hydrocarbon reaction product is removed from the tube; the light hydrocarbon converter 7 is a tube type fixed bed reactor, a light hydrocarbon conversion catalyst is filled in the tube, and a methanol reaction product is taken out of the tube.
In the above technical scheme, preferably, the methanol converter 6 and the light hydrocarbon converter 7 are arranged in parallel in two groups, one on each other and one on each other, and if the catalyst is coked and deactivated, the regeneration can be switched, and the operation is switched.
In the above technical solution, preferably, the methanol converter 6 and the light hydrocarbon converter 7 are both countercurrent heat exchange.
In the above technical scheme, preferably, the bed reaction temperature of the methanol converter is 350-450 ℃, and the bed reaction temperature of the light hydrocarbon converter is 350-450 ℃.
According to the invention, as methanol reacts in the methanol converter, light hydrocarbon components react in the light hydrocarbon converter, the reactions can be carried out separately and independently, more personalized catalyst configuration can be realized according to different reaction mechanism and different reaction atmosphere, so that high reactivity and high reaction selectivity are respectively exerted, the service life of the catalyst is prolonged, meanwhile, a tubular fixed bed reactor is adopted for countercurrent heat extraction, the heat generated by the reaction is coupled and utilized, the heat generated by the conversion of the methanol can be timely removed to supplement the heat required by the conversion of the light hydrocarbon components, so that the temperature of a catalyst bed layer in each reactor from an inlet to an outlet is kept uniform, the control of the reaction at the optimal reaction temperature is facilitated, the local temperature of the catalyst bed layer is prevented from being too high or too low, and a better technical effect is achieved for improving the reactivity of the catalyst and the yield of target products.
Drawings
Fig. 1 is a schematic structural diagram of the flow of the present invention.
In fig. 1: 1 is a light hydrocarbon feeding pipeline; 2 is a light hydrocarbon buffer tank; 3 is a light hydrocarbon pump; 4. is a light hydrocarbon preheater; 5 is a light hydrocarbon heating furnace; 6 is a methanol converter; 7 is a light hydrocarbon converter; 8 is a reaction product discharge pipeline; 9 is a methanol feed line; 10 is a methanol buffer tank; 11 is a methanol pump; 12 is a methanol preheater; 13 is a methanol heating furnace; 141 is a light hydrocarbon heating furnace outlet temperature display, 142 is a methanol heating furnace outlet temperature display, 143 is a methanol converter outlet temperature display, and 144 is a light hydrocarbon converter outlet temperature display.
The present invention is further illustrated by, but not limited to, the following examples.
Detailed Description
[ example 1 ]
As shown in FIG. 1, in a combined conversion reaction process of methanol and light hydrocarbon components, the methanol and the light hydrocarbon components are fed independently, the light hydrocarbon components (mainly referred to as C5-C7 saturated hydrocarbon) from outside the boundary region are fed into a light hydrocarbon buffer tank 2 through a light hydrocarbon feeding pipeline 1, are boosted to 1.6MPa by a light hydrocarbon pump 3 and then are sent out, a reaction product (mixed) with the temperature of about 400 ℃ from a methanol converter 6 and a light hydrocarbon converter 7 is subjected to heat exchange with a light hydrocarbon reactant of the pipe pass through a light hydrocarbon preheater 4 (the light hydrocarbon components are led to the pipe pass of the light hydrocarbon preheater 4), the light hydrocarbon components are heated to about 200 ℃, then are fed into a light hydrocarbon heating furnace 5 to be heated to about 380-410 ℃ (observed through a light hydrocarbon heating furnace outlet temperature display 141), a series of complex chemical reactions are carried out by the light hydrocarbon reaction product (about 380 ℃) from the light hydrocarbon converter 7, the reaction product is fed into the methanol reactor 6 through the shell pass through the light hydrocarbon reactor through the light hydrocarbon converter outlet temperature display 144, the heat exchange is maintained, the methanol reactor 6 is subjected to the heat exchange with the methanol reactant of the pipe pass along the axial direction, the methanol converter 6 is uniformly heated along the axial temperature, the heat is not generated, and the heat is further heat is recovered along the axial direction of the heat exchange layer of the catalyst is not heated along the heat exchange layer, and the heat is further heat is partially and the heat is recovered because the heat is partially and the heat is caused by the heat difference of the heat generated.
Methanol (purity 95%) from outside the boundary area is fed into a methanol buffer tank 10 from a methanol feed line 9, is boosted to about 1.6MPa by a methanol pump 11 and then is fed out, and is preheated (after mixing) by a methanol preheater 12 with the other path of reaction products (the temperature of the methanol products from the methanol converter 6 and the light hydrocarbon converter 7 is about 400 ℃), the methanol is heated to about 200 ℃, then is heated to about 380-410 ℃ by a methanol heating furnace 13 (observed by a methanol heating furnace outlet temperature display 142), a plurality of complicated chemical reactions are carried out in the methanol converter 6, the methanol reaction products (about 380 ℃ and observed by the methanol converter outlet temperature display 143) from the methanol converter 6 are fed into a shell side of the light hydrocarbon converter 7 and are reversely heat-exchanged with the light hydrocarbon reactants in the tube side, the uniformity of the light hydrocarbon converter 7 along the axial temperature is maintained, the catalyst bed layer in the light hydrocarbon converter 7 is not generated to be too high in the axial direction or too low due to the strong endothermic effect of the light hydrocarbon component conversion, the methanol reaction products after heat exchange and the light hydrocarbon components are mixed with the light hydrocarbon reaction products along the two paths, the heat exchange is carried out again, and the two paths are further heat exchanged and the two paths are further processed and the heat exchange is carried out, and the heat exchange is carried out again.
The methanol converter 6 is a tubular fixed bed reactor, a methanol conversion catalyst is filled in a tube, and light hydrocarbon reaction products are discharged outside the tube; the light hydrocarbon converter 7 is a tube type fixed bed reactor, a light hydrocarbon conversion catalyst is filled in the tube, and a methanol reaction product is taken out of the tube.
The methanol converter 6 and the light hydrocarbon converter 7 are connected in parallel, and the two groups are provided with one group and one group, and the two groups can be switched to regenerate and operate in a switching way if the catalyst is coked and deactivated.
The methanol converter 6 and the light hydrocarbon converter 7 are both in countercurrent heat exchange.
Obviously, by adopting the flow of the invention, two groups of parallel tubular fixed bed reactors are adopted, methanol and light hydrocarbon components are separately fed, the reaction is independently carried out, and the reverse heat exchange is carried out, so that the heat coupling utilization can be realized, the energy is saved, the temperature of the catalyst bed layer can be maintained to be uniform, the personalized configuration of the catalyst is implemented, and the respective reaction performance is improved.
Claims (3)
1. A methanol and light hydrocarbon component combined conversion reaction flow is used for producing a high-octane gasoline component or a chemical aromatic component by combining the methanol and the light hydrocarbon component, the light hydrocarbon component and the methanol are fed separately in two paths, the light hydrocarbon component enters a light hydrocarbon buffer tank from a light hydrocarbon feeding pipeline, is pumped out from the bottom of the light hydrocarbon buffer tank by a light hydrocarbon pump and is boosted, exchanges heat through a light hydrocarbon preheater tube pass, enters a light hydrocarbon heating furnace to a required temperature, enters from one end of the light hydrocarbon converter tube pass, exits from the other end of the light hydrocarbon converter tube pass after undergoing chemical reaction, and light hydrocarbon reaction products enter from one end of a methanol converter shell, and exit from the other end of the methanol converter shell after exchanging heat; methanol enters a methanol buffer tank from a methanol feeding pipeline, is pumped out from the bottom of the methanol buffer tank by a methanol pump and is boosted, heat is exchanged by a methanol preheater tube side, the methanol enters a methanol heating furnace to a required temperature, enters from one end of a methanol converter tube side, enters from the other end of the methanol converter tube side after chemical reaction, enters from one end of a light hydrocarbon converter shell, enters from the other end of the light hydrocarbon converter shell after heat exchange, is mixed with a light hydrocarbon reaction product exiting from the methanol converter shell, and is then divided into two paths, one path enters a light hydrocarbon component of the light hydrocarbon preheater tube side, the other path enters the methanol of the methanol preheater tube side, and the two paths after heat exchange are mixed again to enter the subsequent dehydration and product separation procedures;
the methanol converter is a tube type fixed bed reactor, a methanol conversion catalyst is filled in the tube, and a light hydrocarbon reaction product is discharged outside the tube; the light hydrocarbon converter is a tube type fixed bed reactor, a light hydrocarbon conversion catalyst is filled in the tube, and a methanol reaction product is taken out of the tube;
the methanol converter and the light hydrocarbon converter are subjected to countercurrent heat exchange;
wherein the light hydrocarbon component is C5-C7 saturated hydrocarbon.
2. The combined conversion reaction flow of methanol and light hydrocarbon components as claimed in claim 1, wherein the methanol converter and the light hydrocarbon converter are arranged in parallel in two groups, one on each other and one on each other, and are operated in a switching manner.
3. The combined conversion reaction scheme of methanol and light hydrocarbon components according to claim 1, wherein the reaction temperature of the bed layer of the methanol converter is 350-450 ℃ and the reaction temperature of the bed layer of the light hydrocarbon converter is 350-450 ℃.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746880A (en) * | 2011-04-20 | 2012-10-24 | 中国石油化工股份有限公司 | Method for preparing gasoline, diesel oil, ethylene and propylene through coupled catalytic cracking of light hydrocarbons and heavy oil |
| CN107777663A (en) * | 2016-08-29 | 2018-03-09 | 四川天采科技有限责任公司 | A kind of lighter hydrocarbons hydrogen manufacturing and the coupling process of hydrogen from methyl alcohol |
| CN208661079U (en) * | 2018-06-20 | 2019-03-29 | 中国石化工程建设有限公司 | The reactor of thermal coupling catalysis processing hydro carbons |
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| US11220429B2 (en) * | 2019-08-26 | 2022-01-11 | Exxonmobil Research And Engineering Company | Process intensification for reverse flow reactors |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746880A (en) * | 2011-04-20 | 2012-10-24 | 中国石油化工股份有限公司 | Method for preparing gasoline, diesel oil, ethylene and propylene through coupled catalytic cracking of light hydrocarbons and heavy oil |
| CN107777663A (en) * | 2016-08-29 | 2018-03-09 | 四川天采科技有限责任公司 | A kind of lighter hydrocarbons hydrogen manufacturing and the coupling process of hydrogen from methyl alcohol |
| CN208661079U (en) * | 2018-06-20 | 2019-03-29 | 中国石化工程建设有限公司 | The reactor of thermal coupling catalysis processing hydro carbons |
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