Process system for preparing gasoline from methanol
By combining a fluidized bed reactor and a regenerator, the problems of carbon buildup and high energy consumption in fixed bed reactors are solved. This enables long catalyst life and low-energy continuous production, improves gasoline yield and by-product utilization, and is suitable for large-scale production.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- SHANGHAI REZEL KEHUA ENG DESIGN CO LTD
- Filing Date
- 2025-04-27
- Publication Date
- 2026-04-21
AI Technical Summary
Existing methanol-to-gasoline processes suffer from problems such as carbon buildup in fixed-bed reactors, high energy consumption, discontinuous production, and limited scale.
The process system employs a fluidized bed reactor combined with a regenerator, separator, and stripping tower. By utilizing the heat exchange coils inside the fluidized bed reactor and the external heat exchanger outside the regenerator, along with a multi-stage cyclone separator, the regeneration of the catalyst and the effective utilization of heat are achieved, reducing energy consumption and improving reaction efficiency.
It enables long-life use of catalysts, continuous production, reduced energy consumption and production costs, improved gasoline yield and by-product utilization, and is suitable for large-scale production.
Smart Images
Figure CN224147991U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of gasoline production technology, and more specifically, to a process system for producing gasoline from methanol. Background Technology
[0002] Gasoline is currently the most widely used vehicle fuel in the world. It is a light liquid fuel mainly used in internal combustion engines (such as cars, motorcycles, and small generators). It is an important energy source for modern transportation and has the characteristics of being flammable and volatile.
[0003] Methanol-to-gasoline (MTG) is a chemical process that converts methanol (CH3OH) into high-octane gasoline, primarily used in coal chemical and renewable energy fuel sectors. my country is rich in coal but lacks oil, and MTG can serve as a substitute for imported petroleum.
[0004] Currently, methanol-to-gasoline (MTG) uses a fixed-bed reactor. Although the fixed-bed MTG technology has a high conversion rate and is technically mature, its production is discontinuous, prone to carbon buildup, has high energy consumption, and its scale is limited. Utility Model Content
[0005] The purpose of this invention is to provide a process system for producing gasoline from methanol. It has an ingenious structure and advantages such as fewer side reactions, high reaction efficiency, and high yield. In addition, the catalyst in the system has a long service life, can be used for continuous production, has low energy consumption, low production cost, high operational flexibility, and is easy to scale up.
[0006] To achieve the purpose of this utility model, the technical solution adopted is as follows: a methanol-to-gasoline process system, including a fluidized bed reactor, a regenerator, a separator, and a stripping tower. The top of the fluidized bed reactor is connected to the separator via a gas output pipeline. A liquid removal package is installed at the bottom of the separator, and the liquid removal package is connected to the lower end of the stripping tower. A first conveying pipeline and a second conveying pipeline are also connected between the bottom of the fluidized bed reactor and the bottom of the regenerator. The gas outlet of the separator and the gas outlet at the top of the stripping tower are connected in parallel to the first conveying pipeline, and a gasoline separation tower is also connected to the bottom of the separator. A methanol input pipeline is also connected to the lower end of the fluidized bed reactor.
[0007] Furthermore, the fluidized bed reactor is equipped with a heat exchange coil.
[0008] Furthermore, the heat delivery end of the heat extraction coil is installed on the methanol input pipeline.
[0009] Furthermore, both the fluidized bed reactor and the regenerator are equipped with primary and secondary cyclone separators, and are also equipped with tertiary and quaternary cyclone separators.
[0010] Furthermore, the regenerator is equipped with a regeneration external heat exchanger, and a regeneration stripping section heat exchanger is also installed at one end of the first delivery pipeline near the regenerator.
[0011] Furthermore, the heat generated by the regenerative external heat exchanger is steam.
[0012] Furthermore, the separator is a three-phase separator.
[0013] Furthermore, the regenerator is connected to an exhaust pipe at the top, the gasoline separator is connected to a crude gasoline output pipe at the top, the gasoline separator is connected to a heavy oil output pipe at the bottom, the stripper is connected to a drain pipe at the bottom, and a non-condensable gas outlet pipe is installed on the pipeline that connects the top of the separator and the top of the stripper to the first conveying pipeline.
[0014] The beneficial effects of this utility model are:
[0015] 1. This process system uses a fluidized bed reactor, which has the advantages of high operational flexibility and large-scale production capability. Simultaneously, the fluidized bed reactor is connected to a regenerator. After the reaction, the deactivated catalyst carrying coke enters the regenerator for coke burning and regeneration. The regenerated catalyst, now reactivated, re-enters the fluidized bed reactor to participate in the reaction, creating a flow between the catalyst in the fluidized bed reactor and the catalyst in the regenerator. This extends the catalyst's lifespan and enables continuous production. The methanol-to-gasoline reaction is exothermic. By installing heat extraction coils within the fluidized bed reactor, the heat released during the reaction is effectively removed, maintaining a favorable temperature within the reactor for the reaction. This promotes the reaction of methanol to gasoline, reduces side reactions, improves reaction efficiency, and results in a high gasoline yield. Furthermore, the heat extraction coils utilize methanol for heat extraction, preheating the methanol feedstock with the heat released during the reaction, saving energy, reducing consumption, and lowering production costs.
[0016] 2. Since the coke-burning regeneration catalyst is an exothermic regeneration process, an external regeneration heat exchanger is installed outside the regenerator. This external heat exchanger can remove the heat generated by the coke burning process, thus ensuring that the regenerator temperature remains at a balanced state. At the same time, the fluidization of the external regeneration heat exchanger can be achieved using factory air or nitrogen flow, and the extracted heat can be used to produce steam. Furthermore, the external regeneration heat exchanger can be used in either top-bottom fluidization or back-mixing mode, which is flexible in operation, produces by-product steam, and has low energy consumption and low production costs.
[0017] 3. The fluidized bed reactor and regenerator are equipped with primary and secondary cyclone separators, and are also equipped with tertiary and quaternary cyclone separators on the outside. The effective cyclone separation of the catalyst carried by the cyclone has obvious cyclone effect, which is conducive to gas-solid two-phase separation and is environmentally friendly.
[0018] 4. The product from the fluidized bed reactor passes through a separator, with a desliming chamber at the bottom. The water from the desliming chamber is then fed into a stripping tower. The separator employs a three-phase separation technology, with water at the bottom, oil in the middle, and gas at the top. The stripping tower removes organic matter carried in the water, purifying the wastewater and improving the utilization rate of organic matter. The gas at the top of the separator and the top of the stripping tower serves as the transport medium for the regenerated catalyst, effectively reducing the temperature at which the regenerated catalyst enters the fluidized bed reactor, reducing side reactions, improving reaction efficiency, and increasing product yield. The gas then enters the fluidized bed reactor for further reaction, and the byproducts are recycled to produce gasoline, further increasing product yield and reducing production costs.
[0019] 5. By installing a regeneration stripping section heat exchanger in the first conveying pipeline, the regeneration temperature is effectively reduced. Since the temperature of the regenerated catalyst is high and the reaction temperature is low, it is necessary to reduce the temperature of the regenerated catalyst to a state that is conducive to the reaction, reduce side reactions, improve reaction efficiency, and increase product yield. At the same time, by using boiler water to generate steam for heat extraction through the regeneration stripping section heat exchanger, not only can energy consumption be reduced, but production costs are also low. Attached Figure Description
[0020] The accompanying drawings illustrate exemplary embodiments of the present invention and, together with the description thereof, serve to explain the principles of the present invention. These drawings are included to provide a further understanding of the present invention and are incorporated in and constitute a part of this specification.
[0021] Figure 1 This is a system diagram of the methanol-to-gasoline process system provided by this utility model.
[0022] The attached diagram shows the markings and corresponding component names:
[0023] 1-Reactor; 2-Regenerator; 3-Regenerator external heat exchanger; 4-Regenerator stripping section heat exchanger; 5-Separator; 6-Stripping tower; 7-Gas separator; 8-Heat exchange coil; 9-Dehydration package; 10-First conveying pipeline; 11-Second conveying pipeline; 12-Methanol input pipeline; 13-Gas output pipeline; 14-Crude gasoline output pipeline; 15-Heavy oil output pipeline; 16-Drain pipe; 17-Non-condensable gas output pipeline; 18-Liquid phase output pipeline; 19-Exhaust pipe. Detailed Implementation
[0024] The present invention will now be described in further detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for illustrative purposes only and are not intended to limit the scope of the present invention. Furthermore, it should be noted that, for ease of description, only the parts relevant to the present invention are shown in the accompanying drawings.
[0025] It should be noted that, where there is no conflict, the embodiments and features described in these embodiments can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.
[0026] like Figure 1 As shown, the present invention provides a methanol-to-gasoline process system, including a fluidized bed reactor 1, a regenerator 2, a separator 5, and a stripping tower 6. A methanol input pipeline 12 is connected to the side wall of the fluidized bed reactor 1, and the methanol feed into the fluidized bed reactor 1 via the methanol input pipeline 12 is a gas-phase feed. The fluidized bed reactor 1 can produce continuously, has high operational flexibility, and can be used for large-scale production. The regenerator 2 is used to regenerate the deactivated catalyst after the reaction in the fluidized bed reactor 1. The separator 5 is used to separate the gas generated after the reaction in the fluidized bed reactor 1. The stripping tower 6 is used to refine the organic matter and unreacted methanol carried in the water separated in the reactor 1, purifying wastewater while improving the utilization rate of organic matter.
[0027] In this embodiment, the top of the fluidized bed reactor 1 is connected to the separator 5 via a gas output pipe 13, allowing the gas generated in the fluidized bed reactor 1 to be transported to the separator 5 for separation via the gas output pipe 13. The separator 5 is a three-phase separator, which separates the gas generated in the fluidized bed reactor 1 into water, oil, and gas phases. A desliming chamber 9 is provided at the bottom of the separator 5, allowing the water separated by the separator 5 to enter the desliming chamber 9, the gas separated by the separator 5 to enter the top of the separator 5, and the oil separated by the separator 5 to be in the middle of the separator 5. At the same time, the desliming chamber 9 is connected to the lower end of the stripping tower 6 via a liquid phase output pipe 18, allowing the water separated by the separator 5 to be sent into the stripping tower 6 for refining.
[0028] A first conveying pipeline 10 and a second conveying pipeline 11 are connected between the bottom of the fluidized bed reactor 1 and the bottom of the regenerator 2. The first conveying pipeline 10 is used to send the catalyst regenerated in the regenerator 2 into the fluidized bed reactor 1, and the second conveying pipeline 11 is used to send the deactivated catalyst after reaction in the fluidized bed reactor 1 into the regenerator 2 for regeneration. The gas outlet of the separator 5 and the gas outlet at the top of the stripping tower 6 are connected in parallel to the first conveying pipeline 10 through pipelines, so that the gas separated by the separator 5 and the gas refined by the stripping tower 6 are sent into the first conveying pipeline 10 together. The gas entering the first conveying pipeline 10 pushes the catalyst in the first conveying pipeline 10, so that the catalyst regenerated by the regenerator 2 can smoothly enter the fluidized bed reactor 1. This can effectively reduce the temperature of the regenerated catalyst entering the fluidized bed reactor 1, reduce side reactions, improve reaction efficiency, and increase product yield. It can also enable the gas separated by the separator 5 and the gas refined by the stripping tower 6 to enter the reactor 1 for reaction, improve the gasoline product yield, and increase the utilization rate of by-products.
[0029] The bottom of the separator 5 is also connected to a gasoline separation tower 7, which is used to further separate the oil separated by the separator 5 to obtain heavy oil and crude gasoline.
[0030] In this embodiment, since the reaction in the fluidized bed reactor 1 is exothermic, in order to make reasonable use of the heat generated during the reaction process in the fluidized bed reactor 1 and keep the temperature inside the reactor 1 in a favorable reaction state, a heat exchange coil 8 is also installed inside the fluidized bed reactor 1. The medium flowing in the heat exchange coil 8 carries away the heat in the fluidized bed reactor 1, which is more conducive to the reaction of methanol to produce gasoline, reduces the occurrence of side reactions, improves reaction efficiency, and results in a high gasoline yield. At the same time, the heat output end of the heat exchange coil 8 is installed on the methanol input pipeline 12 to preheat the methanol feedstock transported through the methanol input pipeline 12, thereby eliminating the need for additional heat to preheat the methanol feedstock, achieving energy saving and consumption reduction, and making the entire reaction process low in energy consumption and low in production cost.
[0031] In this embodiment, the fluidized bed reactor 1 is equipped with a primary and secondary cyclone separator 5, and is also equipped with a tertiary and quaternary cyclone separator 5. The catalyst carried by the cyclone reaction products is beneficial to the separation of gas and solid phases. At the same time, the regenerator 2 is also equipped with a primary and secondary cyclone separator 5, and is also equipped with a tertiary and quaternary cyclone separator 5. The catalyst carried by the cyclone flue gas is beneficial to the separation of gas and solid phases.
[0032] In this embodiment, since the regeneration catalyst in the regenerator 2 is regenerated exothermically, in order to make reasonable use of the heat generated during the regeneration process of the catalyst in the regenerator 2, an external regeneration heat exchanger 3 is provided on the regenerator 2. The flowing medium in the external regeneration heat exchanger 3 is boiler water. The heat generated during the regeneration process is exchanged between the flowing medium in the external regeneration heat exchanger 3 and the catalyst, so that the flowing medium in the external regeneration heat exchanger 3 forms steam, which can effectively reduce energy consumption and make production costs lower.
[0033] Since the regenerated catalyst in regenerator 2 undergoes exothermic regeneration, in order to make reasonable use of the heat generated during the regeneration process, a regeneration stripping section heat exchanger 4 is installed at one end of the first conveying pipeline 10 near regenerator 2. The flowing medium in the regeneration stripping section heat exchanger 4 is boiler water. When the regenerated catalyst in regenerator 2 flows through the first conveying pipeline 10, the regenerated catalyst exchanges heat with the flowing medium in the regeneration stripping section heat exchanger 4. The flowing medium in the regeneration stripping section heat exchanger 4 forms steam, which can effectively reduce the temperature of the regenerated catalyst, reduce side reactions, improve reaction efficiency, increase product yield, and effectively reduce energy consumption, thus lowering production costs.
[0034] In this embodiment, to facilitate the discharge of gas generated during catalyst regeneration in regenerator 2, an exhaust pipe 19 is connected to the top of regenerator 2; to facilitate the transport of crude gasoline separated by gasoline separator 7 to downstream processing to produce qualified product gasoline, a crude gasoline output pipe 14 is connected to the top of gasoline separator 7; to facilitate the transport of heavy oil separated by gasoline separator 7 to downstream recycling, thereby improving by-product utilization and increasing added value, a heavy oil output pipe 15 is connected to the bottom of gasoline separator 7; to facilitate the recycling of excess gas separated by separator 5 and excess gas refined by stripper 6, a non-condensable gas outlet pipe 17 is installed on the pipeline connecting the top of separator 5 and the top of stripper 6 to the first conveying pipeline 10; to facilitate the discharge of liquid refined in stripper 6, a drain pipe 16 is connected to the bottom of stripper 6.
[0035] During operation, methanol gas is fed into fluidized bed reactor 1. After reacting with the catalyst in fluidized bed reactor 1, the methanol gas is transported to separator 5 through gas output pipeline 13 for separation. The oil separated by separator 5 is sent to gasoline separator 7 for further separation. After separation by gasoline separator 7, the crude gasoline is transported to downstream processing through crude gasoline output pipeline 14, and the heavy oil is sent to downstream for recycling through heavy oil output pipeline 15. The liquid separated by separator 5 enters deliquescence chamber 9, and the liquid in deliquescence chamber 9 is sent to stripping tower 6. After refining by stripping tower 6, the refined liquid is sent out through drain pipe 16. The gas separated by separator 5 and the gas refined by stripping tower 6 are sent to the first conveying pipeline 10.
[0036] During the reaction process in fluidized bed reactor 1, the deactivated catalyst in the fluidized bed is sent to regenerator 2 through second conveying pipeline 11 for regeneration. After regeneration, the catalyst is sent to first conveying pipeline 10. The catalyst entering first conveying pipeline 10 is propelled by the gas separated by separator 5 and the gas refined by stripping tower 6, so that the regenerated catalyst in regenerator 2 enters fluidized bed reactor 1.
[0037] During the reaction of methanol gas in the fluidized bed reactor 1, the medium flowing in the heat exchange coil 8 carries away the heat from the fluidized bed reactor 1, and the heat carried away by the heat exchange coil 8 preheats the methanol feedstock in the methanol input pipeline 12. During the regeneration of the catalyst in the regenerator 2, the flowing medium in the external regeneration heat exchanger 3 exchanges with the heat generated during the regeneration of the catalyst, causing the flowing medium in the external regeneration heat exchanger 3 to form steam and be sent out. At the same time, the flowing medium in the regeneration stripping section heat exchanger 4 exchanges with the heat generated during the regeneration of the catalyst, causing the flowing medium in the external regeneration heat exchanger 3 to form steam and be sent out.
[0038] In the description of this specification, the references to terms such as "one embodiment / mode," "some embodiments / modes," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment / mode or example is included in at least one embodiment / mode or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment / mode or example. Moreover, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments / modes or examples. Furthermore, without contradiction, those skilled in the art can combine and integrate the different embodiments / modes or examples described in this specification, as well as the features of different embodiments / modes or examples.
[0039] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise explicitly specified.
[0040] Those skilled in the art should understand that the above embodiments are merely for clearly illustrating the present invention and are not intended to limit the scope of the present invention. Those skilled in the art can make other changes or modifications based on the above disclosure, and these changes or modifications still fall within the scope of the present invention.
Claims
1. A process system for methanol to gasoline, characterized by, The system includes a fluidized bed reactor (1), a regenerator (2), a separator (5), and a stripper (6). The top of the fluidized bed reactor (1) is connected to the separator (5) via a gas output pipeline (13). A liquid removal package (9) is installed at the bottom of the separator (5), and the liquid removal package (9) is connected to the lower end of the stripper (6). A first conveying pipeline (10) and a second conveying pipeline (11) are also connected between the bottom of the fluidized bed reactor (1) and the bottom of the regenerator (2). The gas outlet of the separator (5) and the gas outlet at the top of the stripper (6) are connected in parallel to the first conveying pipeline (10). A gasoline separation tower is also connected to the bottom of the separator (5). A methanol input pipeline (12) is also connected to the lower end of the fluidized bed reactor (1).
2. The process system for the production of methanol to gasoline according to claim 1, characterized in that, The fluidized bed reactor (1) is equipped with a heat exchange coil (8).
3. The process system for the production of methanol to gasoline according to claim 2, characterized in that, The heat output end of the heat extraction coil (8) is installed on the methanol input pipeline (12).
4. The process system for producing methanol gasoline according to claim 1, wherein, The fluidized bed reactor (1) and regenerator (2) are each equipped with a first- or second-stage cyclone separator (5), and are also equipped with a third- or fourth-stage cyclone separator (5).
5. The process system for the production of methanol to gasoline according to claim 1, wherein, The regenerator (2) is equipped with a regenerating external heat exchanger (3), and a regenerating stripping section heat exchanger (4) is also installed at one end of the first conveying pipeline (10) near the regenerator (2).
6. The process system for producing methanol gasoline according to claim 5, wherein, The heat generated by the regenerated external heat exchanger (3) is steam.
7. The process system for the production of methanol to gasoline according to claim 1, wherein, The separator (5) is a three-phase separator (5).
8. The process system for the production of methanol to gasoline according to claim 1, wherein, The regenerator (2) is connected to an exhaust pipe (19) at the top, a crude gasoline output pipe (14) is connected to the top of the gasoline separator, a heavy oil output pipe (15) is connected to the bottom of the gasoline separator, a drain pipe (16) is connected to the bottom of the stripping tower (6), and a non-condensable gas outlet pipe (17) is also installed on the pipeline that connects the top of the separator (5) and the top of the stripping tower (6) to the first conveying pipeline (10).