CN107523328B

CN107523328B - Alkylation process using microchannel reactor

Info

Publication number: CN107523328B
Application number: CN201610452645.8A
Authority: CN
Inventors: 方向晨; 王海彦; 金月昶; 齐慧敏; 封瑞江; 付会娟; 刘平; 龙文宇; 金熙俊; 王海波; 张健; 张银龙; 白金; 李静; 许菲; 冯帅
Original assignee: LIAONING BRANCH CHINA HUANQIU ENGINEERING Co Ltd; Sinopec Fushun Research Institute of Petroleum and Petrochemicals; Liaoning Shihua University
Current assignee: LIAONING BRANCH CHINA HUANQIU ENGINEERING Co Ltd; Sinopec Fushun Research Institute of Petroleum and Petrochemicals; Liaoning Shihua University
Priority date: 2016-06-22
Filing date: 2016-06-22
Publication date: 2020-03-24
Anticipated expiration: 2036-06-22
Also published as: CN107523328A

Abstract

The invention discloses an alkylation method adopting a microchannel reactor, which takes isobutane and olefin as raw materials, takes liquid acid as a catalyst, and adds a considerable amount of propane as a refrigerant and an entrainer to carry out alkylation reaction to obtain alkylate oil; raw materials and catalysts enter a microchannel reaction zone in a microchannel reactor for alkylation reaction, and then enter a settling section for settling and layering; after the reaction materials are settled and layered, the reaction materials enter a horizontal separating tank continuously, the catalyst at the lower layer is pumped out, the gas at the upper layer is discharged, and the product at the middle layer is sent to a coalescence separator for separation. The microchannel reaction zone is composed of a tubular microchannel reaction zone and a surface microchannel reaction zone. The method has the characteristics of low temperature, no need of premixing reaction raw materials, small bed pressure drop, good energy-saving effect, high product quality and the like, and can realize high-efficiency, energy-saving, safe, low-carbon and environment-friendly continuous production.

Description

Alkylation process using microchannel reactor

Technical Field

The invention belongs to the field of petrochemical industry, and discloses an alkylation method adopting a microchannel reactor.

Background

At present, the requirements of various countries in the world on gasoline indexes are more and more strict, the production process of high-quality gasoline becomes the focus of attention at present, and the alkylation process is a conventional and mature method for producing high-quality gasoline blending components, namely alkylate. The alkylation reaction is a reaction of isobutane and C3-C5 olefin under the action of an acid catalyst to generate gasoline components with high octane number, and the reaction product has the characteristics of low sulfur, no aromatic hydrocarbon or olefin and the like.

The micro-channel reactor has extremely large specific surface area due to the microstructure of the filler in the reaction bed layer inside the micro-channel reactor, and the specific surface area of the micro-channel reactor can reach hundreds of times or even thousands of times of that of a stirring kettle. And the microchannel reactor has excellent heat transfer and mass transfer capacity, the mass transfer efficiency is 10 to 100 times of that of the kettle type reaction kettle, the mixing efficiency of reactants can be greatly improved, the instant uniform mixing and efficient heat transfer of materials can be realized, and the stable state can be quickly reached. Compared with the traditional method, the method reduces the reaction time and material consumption. Is favorable for the stable control of the strong exothermic reaction.

CN 1953804 a discloses an alkylation process and system with staged addition of olefins in microchannels. By utilizing the good heat and mass transfer of the microchannel, higher temperature control is obtained. The temperature is accurately controlled by means of microchannel reaction technology to minimize oligomerization, and the introduction of the staged olefin reduces the local olefin concentration, increases the phase interface area of the acid hydrocarbon dispersion, more accurately adjusts the temperature, increases the octane number of the alkylate product, and improves the quality of the alkylate compared with the conventional process.

However, in the above patent, the paraffin material flow is fed in a large amount, which causes poor initial distribution, the micro-channel itself has a small radial diffusion coefficient, and it is difficult to achieve natural flow distribution only by means of the micro-channel, which results in a sharp decrease in reaction efficiency, and easily causes excessive local temperature, and the reaction area generates temperature difference, so that the alkylation rate is unbalanced. Moreover, the device is filled with hydrogen, so that the separation difficulty and the operation danger are increased.

Therefore, how to upgrade a microchannel reactor, a microchannel and an alkylation process are invented to overcome the above-mentioned drawbacks, which is a technical problem to be solved by those skilled in the art.

Disclosure of Invention

Aiming at the defects of the existing alkylation process technology, the invention discloses an alkylation method adopting a microchannel reactor, which can ensure that reactants and an acid catalyst are mixed very uniformly, can reduce side reactions, improves the mass transfer efficiency of the reactants and the catalyst, further improves the quality and the yield of reaction products, and can simultaneously realize the purpose of saving energy consumption. The cost is reduced, the influence on the environment and the instability of the performance of the produced product are reduced, the traditional intermittent reaction kettle production operation with low efficiency is replaced, and the continuous production with high efficiency, energy conservation, safety, low carbon and environmental protection is realized.

To solve the above-described problems, the present invention is thus achieved.

An alkylation method adopting a microchannel reactor is adopted, wherein isobutane and olefin are used as raw materials, and liquid acid is used as a catalyst to carry out alkylation reaction to obtain alkylate oil; the raw material and the catalyst enter a microchannel reaction zone in a microchannel reactor for alkylation reaction, and then enter a settling section for settling and layering; after the reaction materials are settled and layered, the reaction materials enter a horizontal separating tank continuously, the catalyst at the lower layer is pumped out, the gas at the upper layer is discharged, and the product at the middle layer is sent to a coalescence separator for separation.

In a preferred embodiment, propane is added to the feed as a refrigerant and entrainer for the feed.

Furthermore, the microchannel reactor comprises a feeding area, a microchannel reaction area, a settling area and a separation area; the outlet of the feeding area is communicated with the inlet of the microchannel reaction area; the outlet of the microchannel reaction zone is communicated with the inlet of the settling zone; the outlet of the settling zone is communicated with the inlet of the separation zone.

Furthermore, the microchannel reaction zone is at least provided with a tubular microchannel reaction zone and a surface microchannel reaction zone.

Furthermore, the tubular microchannel reaction zone and the surface microchannel reaction zone are longitudinally and alternately arranged in series; the number of the tubular microchannel reaction zones is 2-10; the number of the surface type micro-channel reaction areas is 2-10.

Furthermore, the space volume ratio of the tubular microchannel reaction area to the surface type microchannel reaction area is 0.5-5: 1.

furthermore, the tubular microchannel reaction zone is formed by a tubular microchannel member; the diameter of the pore channel is 0.1-10 mm; the surface type micro-channel reaction area is composed of a surface type micro-channel component; the gap between the two plates is 0.1-10 mm.

The inlet of the horizontal separation tank can adopt a cyclone separation structure (of course, other structures can be adopted), and a partition plate is arranged in the middle. And the acid hydrocarbon two phases enter a suspension separator to realize the primary separation of the acid hydrocarbon. The acid phase was returned to the reactor by a circulation pump and the hydrocarbon phase overflowed to the other side of the partition and was further separated by pumping into a coalescer.

Further, the reaction pressure of the alkylation reaction is 0MPa to 1.0 MPa; the residence time of the reaction materials in the reactor is 1-200 min.

Further, the molar ratio of isobutane to olefin in the alkylation reaction is 1-50: 1; the volume ratio of acid to hydrocarbon is 0.1-5: 1; the molar ratio of isobutane to propane is 1-100: 1.

According to the alkylation process, the acid catalyst separated by reaction can be recycled, so that the loss of acid is greatly reduced. During the reaction, the acid catalyst is replenished at any time to ensure the concentration range. After the reaction is finished, flushing the device by adopting nitrogen, inert gas or carbon dioxide.

The alkylation process of the invention uses a proper microchannel reactor, the pressure drop of the bed layer of the reactor is small, which is beneficial to mass transfer and heat transfer, the reaction is more balanced, the high-efficiency separation of reactants and products can be realized, and the side reaction is less. The method has the characteristics of mild operation conditions, easy control of reaction, good raw material distribution, high product quality and the like, effectively avoids the problem of unbalanced mass and heat transfer of the microchannel reaction with a single structure, solves the problems of large equipment size, low space utilization rate and the like, and can realize high-efficiency, energy-saving, safe, low-carbon and environment-friendly continuous production. The test result shows that the tubular micro-channel component and the surface micro-channel component (plate micro-channel component) are alternately combined, so that the reaction material contact mixing effect of an immiscible alkylation reaction system is more efficient, the reaction efficiency is improved, the side reaction is reduced, and the catalyst loss is effectively reduced.

The process adopts an alkylation process of the microchannel reactor, does not need to provide extra power to pre-mix the catalyst and the production raw materials, has small bed pressure drop, is beneficial to the heat absorption and vaporization of alkane, reduces hot spots of reaction, and solves the problem of difficult separation caused by the emulsification of reaction materials. The reaction raw materials are added with a considerable amount of propane as a refrigerant and an entrainer, so that the reaction temperature is reduced, and the occurrence of side reactions is reduced. And the high-efficiency separation of acid hydrocarbon is realized through the hydrocyclone separation of the horizontal tank, so that the corrosion of equipment is reduced. The alkylate oil produced by the reaction has high octane number and low sulfur, and does not contain aromatic hydrocarbon and olefin.

Drawings

The invention is further described with reference to the following figures and detailed description. The scope of the invention is not limited to the following expressions.

FIG. 1 is a schematic diagram of a microchannel reactor used in the present invention.

FIG. 2 is a schematic process flow diagram of the alkylation reaction of the present invention.

FIG. 3 is a cross-sectional view of a tubular microchannel reaction zone according to the present invention.

FIG. 4 is a cross-sectional view of the reaction zone of the planar microchannel of the present invention.

FIG. 5 is a schematic structural diagram of another embodiment of the planar microchannel reaction zone of the present invention.

In the figure: 1. a separation tank; 2. a transition bed layer; 3. a distribution plate; 4. a microchannel bed layer; 5. a microchannel module; 6. an acid distributor; 7. a hydrocarbon distributor; 8. a nitrogen inlet pipe; 9. an acid inlet pipe; 10. a hydrocarbon inlet pipe; 11. a top distributor; 12. an interface meter; 13. a sampling tube; 14. a refrigerant inlet; 15. a thermowell; 16. a gas phase extraction port; 17. a hydrocarbon withdrawal port; 18. an acid extraction port; 19. a fibrous material; 20. supporting ribs; 21. a constraint frame; 22. a microchannel panel.

Detailed Description

The method takes isobutane and olefin as raw materials and liquid acid as a catalyst to carry out alkylation reaction to obtain alkylate oil; the alkylation reaction employs the following microchannel reactor: the microchannel reaction zone in the microchannel reactor is vertically arranged, and at least one tubular microchannel reaction zone and one surface microchannel reaction zone (plate microchannel reaction zone) are arranged in the microchannel reaction zone. The microchannel reaction zone is vertically arranged, which means that the reaction channel is vertically arranged.

The tubular microchannel reaction zone and the surface microchannel reaction zone (plate microchannel reaction zone) are longitudinally arranged in series, and preferably a plurality of tubular microchannel reaction zones and surface microchannel reaction zones (plate microchannel reaction zones) are alternately arranged in series. Generally, 2-10 tubular microchannel reaction zones and 2-10 planar microchannel reaction zones are preferably arranged alternately in series. The number of microchannel beds is determined specifically based on throughput and residence time. The serial arrangement refers to that reaction materials sequentially pass through a tubular microchannel reaction zone and a surface microchannel reaction zone. The space volume ratio occupied by the tubular microchannel reaction zone and the surface microchannel reaction zone is 0.5-5: 1, preferably 2-3: 1.

The top of the microchannel reactor is provided with a material introducing structure, the material introducing structure comprises a liquid feeding port and a gas feeding port, a feeding distributor is arranged above a microchannel reaction zone, and the lower part of the microchannel reactor is provided with a material collecting structure after reaction. The liquid feed distributor (acid distributor 6 and hydrocarbon distributor 7) ensures that the liquid feed distribution reaches 30-200 points/m²Preferably 50 to 100 dots/m². In addition, a liquid level detection control device, a temperature detection control device, a pressure detection control device, a material gasification condition detection device and the like are arranged as required.

The reactor shell is preferably cylindrical in shape, with the reactor being vertically disposed.

The microchannel reactor is a vertical reactor, and the height-diameter ratio is 2-10, preferably 4-6.

In the microchannel reactor, a microchannel reaction area is arranged below the distributor, belongs to a vertical microchannel and consists of two structural microchannel components. The tubular microchannel reaction zone is formed by a tubular microchannel member. The tubular microchannel member is made of a material with a fiber compact porous structure, and can be made of organic polymers such as glass fiber and polyethylene or inorganic substances, the cross section of a pore channel of the tubular microchannel member can be in various suitable shapes such as polygons, and the diameter (equivalent to a circle) of the pore channel can be in a micron-sized or millimeter-sized diameter, generally 0.5-10 mm, and preferably 2-5 mm. Referring to fig. 3, 19 is a fibrous material; 20 is a support rib; 21 is a constraining frame (tubesheet). The fiber material 19 has a dense porous structure, can be organic polymers such as glass fiber and polyethylene, or inorganic substances, and has corrosion resistance and long service life. The fiber material is processed into fiber cloth with a suitable shape and is filled into the tube bundle on the restraint frame, the cross section of the formed micro-channel pore channel can be in various suitable shapes, such as polygons, and the equivalent diameter of the pore channel is micron-sized or millimeter-sized, generally 0.5-10 mm, and preferably 2-5 mm.

The surface type microchannel reaction zone (plate type microchannel reaction zone) is formed by a surface type microchannel component. The surface type microchannel component consists of a plurality of groups of plates which are vertically installed, and can be of specific structures such as annular plates and folded plates, the surface type channel gap between the two plates is in a micron-sized or millimeter-sized range, generally 0.1-10 mm, preferably 0.5-2 mm, and the gap between the two plates forms a surface type microchannel reaction space. When the folded plate structure is adopted, the angle a between the two plates is between 5 and 180 degrees, preferably between 10 and 60 degrees. Referring to fig. 4, preferably, the surface type microchannel member is configured to have an indirect heat exchange type structure, i.e., a structure similar to a conventional plate type heat exchanger type structure, but the reaction channel is a surface type microchannel structure, and the introduction of the cooling medium facilitates the extraction of reaction heat.

The bottom of the microchannel reactor is communicated with the horizontal separation tank. The material inlet of the horizontal separation tank is preferably arranged to be of a cyclone separation structure.

And a liquid level meter is arranged on the outer wall of the shell between the distributor of the microchannel reactor and the reaction bed layer to detect whether the acid-hydrocarbon mixed liquid has a liquid layer on the surface of the filler or not, and the acid feeding amount is adjusted.

And a gas phase sampling device is arranged on the outer wall of the shell between the reaction beds of the microchannel reactor to judge whether gas resistance occurs.

The height of each section of microchannel bed layer of the microchannel reactor is 30-200 cm, preferably 50-150 cm.

The upper end and the lower end of each section of the microchannel reactor are isolated by a porous steel plate, and the aperture ratio (the proportion of the aperture area of the steel plate in the steel plate) of the steel plate is 10-60%, preferably 15-30%.

The alkylation process used by the invention is to use the microchannel reactor of the invention to carry out alkylation reaction by taking isobutane and olefin as raw materials, propane as a refrigerant and an entrainer and liquid acid as a catalyst to obtain alkylate. The olefin is C3-C5 olefin, preferably butylene.

The alkylation process reduces acid consumption, improves selectivity and yield of the reaction process, and improves the octane number of the alkylate oil. The reaction pressure (gauge pressure) is maintained at 0MPa to 1.0MPa, preferably 0MPa to 0.5 MPa. The residence time of the reaction materials in the reactor is 1-200 min, preferably 30-90 min.

In the alkylation process, the molar ratio of isobutane to olefin (alkane-alkene molar ratio) is 1-50: 1, and preferably 5-20: 1.

In the alkylation reaction method, the volume ratio of the acid hydrocarbon is 0.1-5: 1, preferably 0.5-3: 1. Acid refers to a liquid catalyst comprising various acids and ionic liquids.

According to the alkylation process, the molar ratio of isobutane to propane is 1-100: 1, and preferably 10-30: 1. The microchannel reactor has the advantages that the pressure drop of the bed layer of the microchannel alkylation reactor is small, the heat absorption vaporization of propane is facilitated, and the hot spots of the reaction are reduced.

As shown in fig. 1 and 2, the microchannel reactor comprises a feed zone, a microchannel reaction zone, a settling zone, and a separation zone; the outlet of the feeding area is communicated with the inlet of the microchannel reaction area; the outlet of the microchannel reaction zone is communicated with the inlet of the settling zone; the outlet of the settling zone is communicated with the inlet of the separation zone.

The feed zone comprises a top distributor 11; an acid inlet pipe 9, a nitrogen inlet pipe 8 and a hydrocarbon inlet pipe 10 are arranged on the top distributor 11; an acid distributor 6 and a hydrocarbon distributor 7 are arranged in the inner cavity of the top distributor 11; the outlet of the acid inlet pipe 9 is communicated with the inlet of the acid distributor 6; the outlet of the hydrocarbon inlet pipe 10 communicates with the inlet of the hydrocarbon distributor 7. An interface meter 12 is arranged on the top distributor 11.

The microchannel reaction zone comprises a five-section structure which is formed by longitudinally and alternately connecting a tubular microchannel reaction zone, a surface type microchannel reaction zone, a tubular microchannel reaction zone, a surface type microchannel reaction zone and a tubular microchannel reaction zone in series. 13 is a sampling tube; 14 is a refrigerant inlet; 15 is a thermowell; 3 is a distribution plate; 4 is a microchannel bed layer; and 5 is a micro-channel module. The settling zone is a transition bed layer 2. The separation area is a separation tank 1. The separation tank 1 is provided with a gas phase extraction port 16, an acid extraction port 18, and a hydrocarbon extraction port 17.

After the raw materials enter the reactor, the raw materials pass through acidThe distributor 6 and the hydrocarbon distributor 7 realize uniform distribution, and the distributor ensures that the liquid feeding distribution reaches 30-200 points/m²Preferably 50 to 100 dots/m². A microchannel reaction area is arranged below the distributor, the microchannel reaction area belongs to a vertical microchannel and consists of two parts, the upper end of the microchannel belongs to a tubular microchannel and is made of materials with fiber compact pore structures, the lower end of the microchannel belongs to a surface microchannel and consists of vertically installed folded plates, and the angle a between the two plates is 10-60 degrees. Has the effects of redistribution, mixing, reaction and the like.

Referring to fig. 2, fig. 2 is a schematic view of an alkylation process flow using a microchannel reactor according to an embodiment of the present invention.

The microchannel reactor is adopted, isobutane and olefin are used as alkylation reaction raw materials, the catalyst is a liquid acid catalyst, the reaction raw materials enter a distributor (a hydrocarbon distributor 7) of a reaction device through a liquid feed inlet after passing through a buffer tank, the acid catalyst enters an acid distributor 6 of the reaction device through the liquid feed inlet, a considerable amount of propane is added into the raw materials and used as a refrigerant and an entrainer of the raw materials, the vaporization and heat removal of the raw materials are realized, the reaction temperature is ensured to be low, the raw material amount and the acid catalyst amount are regulated and given and controlled by flow regulation, and after primary distribution of the liquid distributor, the raw materials uniformly flow down in a trickle state according to a certain liquid hourly space velocity and enter a reaction bed layer. After the reaction raw materials can uniformly enter the microchannel reaction zone, the reaction is firstly carried out in the tubular microchannel reaction zone at the upper end of the microchannel, and the extremely large specific surface area provided by the tubular microchannel reaction zone is favorable for alkylation reaction and simultaneously does not generate a channeling phenomenon. Then, the fluid is mixed, redistributed and reacted through the surface type micro-channel reaction area at the lower end of the micro-channel. The raw materials are mixed well in the micro-channel, the temperature in the reaction process is accurately controlled, the raw material ratio is accurately controlled, and the yield of the product is obviously improved.

After the materials react in the microchannel reaction zone, the materials enter a settling section, the reaction materials are settled and layered, the propane in the middle of the settling section is heated and gradually vaporized along with the change of pressure due to the different boiling points of the propane and the isobutane, the propane is vaporized to the lower part of the settling section, part of the isobutane is vaporized, the reaction materials are settled and layered and enter a horizontal separation tank (for enhancing the separation effect, the horizontal separation tank with the cyclone separation function can be adopted in the specific design), the lower layer acid catalyst is pumped out by a circulating pump for circulation, the upper layer gas is discharged by a compressor, the middle layer product is pumped out by a pump and enters a coalescence separator, the separated product is sent to a separation section or a storage tank, and a small amount of acid returns to the reactor.

The liquid catalyst used in the alkylation reaction can be any liquid acid catalyst capable of catalyzing isobutane and olefin to carry out alkylation reaction, and specifically HF and H₂SO₄One or more of liquid catalysts such as phosphoric acid, boric acid, acetic acid or ionic liquid.

The following examples are given to illustrate the reaction effects of the present invention, but do not limit the scope of the present invention.

Examples 1 to 3.

By adopting the reactor with the structure shown in figure 1 and the alkylation reaction process shown in figure 2, the bed pressure drop of the microchannel reaction zone is 0.1-1.0 MPa, preferably 0-0.5 MPa. Isobutane and butylene are used as raw materials, sulfuric acid is used as a catalyst, and propane is used as a refrigerant to carry out alkylation reaction.

The volume ratio of the sulfuric acid feed to the isobutane and butene mixture feed is 0.1-5: 1, preferably 0.5-3: 1. The molar ratio of the alkane to the alkene is 1-50: 1, preferably 5-20: 1. The molar ratio of the isobutane to the propane is 1-100: 1, preferably 10-30: 1, and the reaction pressure is maintained at 0-1.0 MPa, preferably 0-0.5 MPa. The side reaction is inhibited, the acid consumption is reduced, the selectivity and the yield of the reaction process are improved, and the octane number of the alkylate oil is improved. The residence time of the reaction materials in the reactor is 1-200 min, preferably 30-90 min.

The reactor structure is as follows: the structure comprises five sections of a tubular microchannel reaction area, a surface type microchannel reaction area, a tubular microchannel reaction area, a surface type microchannel reaction area and a tubular microchannel reaction area, wherein the volumes of the microchannel reaction sections are the same. The pore size of the tubular microchannel component is 3mm, the angle between two plates of the surface microchannel component is 45 degrees, and the gap between the two plates is 1 mm.

The specific reaction conditions are shown in Table 1, and the reaction results are shown in Table 2.

Comparative examples 1 to 2.

Comparative example 1 used a conventional horizontal mechanically-stirred reactor with a refrigerant tube bundle disposed inside, and comparative example 2 used a microchannel reactor consisting of only tubular microchannel structures (same as in example 1), with the reaction conditions shown in Table 1 and the reaction results shown in Table 2.

Table 1 examples and comparative examples alkylation reaction conditions.

Table 2 results of alkylation reactions of examples and comparative examples.

It should be understood that the detailed description of the present invention is only for illustrating the present invention and is not limited by the technical solutions described in the embodiments of the present invention, and those skilled in the art should understand that the present invention can be modified or substituted equally to achieve the same technical effects; as long as the use requirements are met, the method is within the protection scope of the invention.

Claims

1. An alkylation method adopting a microchannel reactor, which takes isobutane and olefin as raw materials and liquid acid as a catalyst to carry out alkylation reaction to obtain alkylate oil; the method is characterized in that: the raw material and the catalyst enter a microchannel reaction zone in a microchannel reactor for alkylation reaction, and then enter a settling zone for settling and layering; after settling and layering, the reaction materials enter a horizontal separation tank continuously, a lower-layer catalyst is pumped out, an upper-layer gas is discharged, and a middle-layer product is sent to a coalescence separator for separation; adding propane into the raw material to be used as a refrigerant and an entrainer of the raw material; the microchannel reactor comprises a feeding area, a microchannel reaction area, a settling area and a separation area; the outlet of the feeding area is communicated with the inlet of the microchannel reaction area; the outlet of the microchannel reaction zone is communicated with the inlet of the settling zone; the outlet of the settling zone is communicated with the inlet of the separation zone; the microchannel reaction zone is at least provided with a tubular microchannel reaction zone and a surface microchannel reaction zone.

2. The alkylation process using a microchannel reactor of claim 1, wherein: the tubular microchannel reaction zone and the surface microchannel reaction zone are longitudinally and alternately arranged in series; the number of the tubular microchannel reaction zones is 2-10; the number of the surface type micro-channel reaction areas is 2-10.

3. The alkylation process using a microchannel reactor of claim 2, wherein: the space volume ratio of the tubular microchannel reaction area to the surface type microchannel reaction area is 0.5-5: 1.

4. the alkylation process using a microchannel reactor of claim 3, wherein: the tubular microchannel reaction zone is formed by a tubular microchannel member; the surface type micro-channel reaction area is composed of a surface type micro-channel component.

5. The alkylation process using a microchannel reactor of claim 4, wherein: the reaction pressure of the alkylation reaction is 0MPa to 1.0 MPa; the residence time of the reaction materials in the reactor is 1-200 min.

6. The alkylation process using a microchannel reactor of claim 5, wherein: the molar ratio of isobutane to olefin in the alkylation reaction is 1-50: 1; the volume ratio of acid to hydrocarbon is 0.1-5: 1; the molar ratio of isobutane to propane is 1-100: 1.