CN107523328A - Using the alkylation of new micro passage reaction - Google Patents
Using the alkylation of new micro passage reaction Download PDFInfo
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- CN107523328A CN107523328A CN201610452645.8A CN201610452645A CN107523328A CN 107523328 A CN107523328 A CN 107523328A CN 201610452645 A CN201610452645 A CN 201610452645A CN 107523328 A CN107523328 A CN 107523328A
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- 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
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
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- 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
- C10G2300/10—Feedstock materials
- C10G2300/1081—Alkanes
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- 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
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
Abstract
The invention discloses a kind of alkylation using new micro passage reaction, is using iso-butane and alkene as raw material, using liquid acid as catalyst, adds considerable amount of propane as cryogen and entrainer, be alkylated reaction and obtain alkylate oil；After the microchannel reaction zone that raw material and catalyst enter in micro passage reaction is alkylated reaction, enters back into settling section and carry out sedimentation layering；Reaction mass continues into horizontal knockout drum after sedimentation is layered, extracts lower catalyst agent out, discharge top tank air, middle level product is delivered to coalescing separator and separated again.Microchannel reaction zone is made up of tubular type microchannel reaction zone and face the pathway reaction area two parts that decline.The features such as present invention has and can carried out at low temperature, and reaction raw materials need not be pre-mixed, and bed pressure drop is small, good energy-conserving effect, and product quality is high, can be achieved energy-efficient, safety, low-carbon and the continuous production of environmental protection.
Description
Technical field
The invention belongs to petrochemical industry, discloses a kind of alkylation using new micro passage reaction.
Background technology
Requirement of the every country to gasoline index is more and more stricter in the world at present, and the production technology of high-quality gasoline turns into current focal point, and alkylation process is production high-quality gasoline blend component, the i.e. method of the routine of alkylate oil and maturation.Alkylated reaction is the iso-butane reaction of generation with high octane gasoline component under acid catalyst effect with C3-C5 alkene, and reaction product has the characteristics that low-sulfur and aromatic-free or alkene.
Micro passage reaction is because the micro-structural of filler in its internal-response bed makes it have great specific surface area, up to even thousands of times of the hundred times of stirred tank specific surface area.And micro passage reaction has fabulous heat transfer and mass transfer ability, mass-transfer efficiency is more than 10 to 100 times of still reaction kettle, it can greatly improve the mixing efficiency of reactant, it is possible to achieve uniformly mixing and the efficient heat transfer of the moment of material, stable state can be rapidly reached.Compared with conventional method, reduce reaction time and supplies consumption.Be advantageous to the steady control of strong exothermal reaction.
CN
1953804 A disclose the alkylation and system of staged addition of olefin in microchannel.The good heat transfer and mass transfer having using microchannel, obtain higher temperature control.Oligomerization is minimized by microchannel reaction technology precise control of temperature, and the alkene introducing of classification reduces olefin partial concentration, add the boundary area of sour hydrocarbon dispersion, more accurately adjust temperature, compared with traditional handicraft, the octane number of alkylate is improved, improves the quality of alkylates.
But above-mentioned patent paraffin material flow is largely fed, bad initial distribution can be caused, microchannel has less radial diffusion coefficient in itself, rely solely on microchannel and be extremely difficult to nature flow distribution, reaction efficiency is caused drastically to decline, it is too high to easily cause local temperature, conversion zone can produce the temperature difference so that alkyl rate is unbalanced.And hydrogen is filled with a device, increase separating difficulty and operational danger.
Therefore, how micro passage reaction is lifted, invents a kind of new microchannel and alkylation process to overcome drawbacks described above, be those skilled in the art's technical issues that need to address.
The content of the invention
For the deficiency of current alkylation process technology, the invention discloses a kind of alkylation using new micro passage reaction, this method makes the mixing of reactant and acid catalyst visibly homogeneous, side reaction can be reduced, improve the mass-transfer efficiency of reactant and catalyst, and then the quality and yield of reaction product are improved, the purpose for saving energy consumption can be realized simultaneously.While cost is reduced, the unstability of the influence to environment and the properties of product produced is also reduced, substitutes the reactor production operation in traditional poorly efficient gap, realizes energy-efficient, safety, low-carbon and the continuous production of environmental protection.
In order to solve the above technical problems, what the present invention was realized in.
Using the alkylation of new micro passage reaction, it is using iso-butane and alkene as raw material, using liquid acid as catalyst, is alkylated reaction and obtains alkylate oil；After the microchannel reaction zone that the raw material and catalyst enter in micro passage reaction is alkylated reaction, enters back into settling section and carry out sedimentation layering；Reaction mass continues into horizontal knockout drum after sedimentation is layered, extracts lower catalyst agent out, discharge top tank air, middle level product is delivered to coalescing separator and separated again.
As a kind of preferred scheme, the present invention adds propane in the raw material, cryogen and entrainer as raw material.
Further, micro passage reaction of the present invention includes feed zone, microchannel reaction zone, decanting zone and Disengagement zone；The outlet of the feed zone communicates with the entrance of microchannel reaction zone；The outlet of the microchannel reaction zone communicates with the entrance of decanting zone；The outlet of the decanting zone communicates with the entrance of Disengagement zone.
Further, microchannel reaction zone of the present invention declines pathway reaction area at least provided with a tubular type microchannel reaction zone and a face.
Further, tubular type microchannel of the present invention reaction zone and face are declined, and longitudinally alternating is arranged in series in pathway reaction area；The number of tubular type microchannel reaction zone is 2~10；The face decline pathway reaction area number be 2~10.
Further, tubular type microchannel of the present invention reaction zone and face the spatial volume ratio that pathway reaction area occupies that declines are 0.5~5：1.
Further, tubular type microchannel of the present invention reaction zone is made up of tubular type microchannel component；Channel diameter is 0.1~10mm；The face pathway reaction area that declines is made up of the face channel component that declines；Path clearance is 0.1~10mm between two plates.
The entrance of horizontal knockout drum of the present invention can use hydrocyclone separation structure（Certainly other structures also can be selected）, centre sets dividing plate.Sour hydrocarbon two-phase enters suspension separator, realizes the initial gross separation of sour hydrocarbon.Sour mutually to return to reactor by circulating pump, hydrocarbon mutually overflows to dividing plate opposite side, is further separated by being pumped into coalescer.
Further, the reaction pressure of alkylated reaction of the present invention is 0MPa~1.0MPa；Residence time of the reaction mass in reactor is 1~200min.
Further, the mol ratio of the iso-butane of alkylated reaction of the present invention and alkene is 1~50:1；Sour hydrocarbon volume ratio is 0.1~5:1；Iso-butane is 1~100 with propane mol ratio:1.
Alkylation process of the present invention, the acid catalyst of Reaction Separation can be recycled, and greatly reduce the loss of acid.During the course of the reaction, supplement acid catalyst ensures concentration range at any time.Reaction uses nitrogen, inert gas or carbon dioxide to carry out device flushing after terminating.
Alkylation process of the present invention is by using suitable micro passage reaction, and reactor bed pressure drop is smaller, is advantageous to mass transfer and heat transfer, makes reaction more balanced, it is possible to achieve reactant and product efficiently separate, and side reaction is few.The present invention has operating condition gentle, react easily controllable, feed distribution is good, the features such as product quality is high, it effectively prevent the single microchannel plate of structure and answer the unbalanced problem of mass-and heat-transfer, it is huge to solve equipment size simultaneously, the problems such as low space utilization, energy-efficient, safety, low-carbon and the continuous production of environmental protection can be achieved.Result of the test shows, tubular type microchannel component and face decline channel component（Board-like microchannel component）Alternately combine and set, for immiscible alkylation reaction system there is more efficient reaction mass to contact mixed effect, be advantageous to improve reaction efficiency, reduce side reaction, effectively reduce catalyst attrition amount.
Present invention process uses the alkylation process of micro passage reaction, extra power need not be provided to be pre-mixed catalyst and raw materials for production, bed pressure drop is smaller, is advantageous to the heat absorption vaporization of alkane, the focus of reaction is reduced, solves and is difficult to separation problem caused by reaction mass emulsification.Considerable amount of propane is added in reaction raw materials as cryogen and entrainer, reaction temperature is reduced, reduces side reaction.By the rotary filter press of horizontal tank, efficiently separating for sour hydrocarbon is realized, reduces equipment corrosion.React the alkylate oil octane number height of generation, low-sulfur, aromatic-free and alkene.
Brief description of the drawings
The invention will be further described with reference to the accompanying drawings and detailed description.Protection scope of the present invention is not only limited to the statement of following content.
Fig. 1 is the micro passage reaction structural representation that the present invention uses.
Fig. 2 is alkylation reaction technique schematic flow sheet of the present invention.
Fig. 3 is tubular type microchannel reaction zone sectional view of the present invention.
Fig. 4 is that face of the present invention declines pathway reaction area sectional view.
Fig. 5 is that face of the present invention declines pathway reaction area another embodiment structural representation.
In figure：1st, knockout drum；2nd, transition bed；3rd, distribution grid；4th, microchannel bed；5th, microchannel module；6th, acid spreader；7th, hydrocarbon distributor；8th, nitrogen inlet tube；9th, sour inlet tube；10th, hydrocarbon inlet tube；11st, top distributor；12nd, level meters；13rd, sampling pipe；14th, cryogen entrance；15th, thermocouple sheath；16th, gas phase outlet port；17th, hydrocarbon outlet port；18th, sour outlet port；19th, fibrous material；20th, brace rod；21st, framework is constrained；22nd, microchannel panel.
Embodiment
The present invention, using liquid acid as catalyst, is alkylated reaction and obtains alkylate oil using iso-butane and alkene as raw material；Alkylated reaction uses following micro passage reaction：Microchannel reaction zone in micro passage reaction is vertical to be vertically arranged, and microchannel reaction zone declines pathway reaction area at least provided with a tubular type microchannel reaction zone and a face（Board-like microchannel reaction zone）.Described microchannel reaction zone is vertical to be vertically arranged, and is referred to that reaction channel is vertical and is vertically arranged.
Tubular type microchannel reaction zone and face decline pathway reaction area（Board-like microchannel reaction zone）Lontitudinal series are set, and preferably multiple tubular type microchannel reaction zones and face decline pathway reaction area（Board-like microchannel reaction zone）Alternating is arranged in series.As a rule, preferably 2~10 tubular type microchannel reaction zones and 2~10 faces decline pathway reaction area alternately be arranged in series.The quantity of microchannel bed is determined with specific reference to treating capacity and residence time.Described is arranged in series, and refers to that reaction mass passes sequentially through tubular type microchannel reaction zone and face declines pathway reaction area.Tubular type microchannel reaction zone and face the spatial volume ratio that pathway reaction area occupies that declines are 0.5~5:1, preferably 2~3:1.
Material is set to introduce structure at the top of micro passage reaction, material, which introduces structure, includes liquid inlet opening and gas charging aperture, and feed distributor is set on the reaction zone of microchannel, and micro passage reaction bottom sets reacting rear material collection structure.Liquid feed distributor（Acid spreader 6 and hydrocarbon distributor 7）Ensure that liquid feedstock is distributed and reach 30 ~ 200 points/m2, preferably 50 ~ 100 points/m2.In addition, it is arranged as required to level sensing control device, temp detecting controller, pressure detection control device, material gasification situation detection means etc..
Reactor shell profile is preferably cylinder, and reactor is disposed vertically.
Micro passage reaction is vertical reactor, and ratio of height to diameter is 2 ~ 10, preferably 4 ~ 6.
In micro passage reaction, microchannel reaction zone is set, microchannel reaction zone belongs to vertical microchannel, is made up of two kinds of structure microchannel components below distributor.Tubular type microchannel reaction zone is made up of tubular type microchannel component.Tubular type microchannel component is made up of the material with fiber densification hole shape structure, can be the materials such as the organic polymers such as glass fibre, polyethylene or inorganic matter, the opening cross-sectional face of tubular type microchannel component can be various suitable shapes, such as polygon, channel diameter（It is equivalent to justify）Can be micron order or grade, generally 0.5 ~ 10mm, preferably 2 ~ 5mm.Shown in Figure 3,19 be fibrous material；20 be brace rod；21 be constraint framework（Tube sheet）.Fibrous material 19 has fine and close hole shape structure, can be the organic polymers such as glass fibre, polyethylene or inorganic matter etc., have corrosion-resistant, it is ensured that service life.Fibrous material is processed into the fiber cloth of suitable shape, is loaded into the tube bank on constraint framework, the microchannel duct cross section of composition can be various suitable shapes, such as polygon, duct equivalent diameter is micron order or grade, generally 0.5 ~ 10mm, preferably 2 ~ 5mm.
Face declines pathway reaction area（Board-like microchannel reaction zone）It is made up of the face channel component that declines.The face channel component that declines is made up of multigroup plate of vertical installation, can be the concrete structure such as ring-plate, folded plate type, face formula path clearance is micron order or grade between two plates, generally 0.1~10mm, it is preferred that 0.5~2mm, the gap between two plates forms face and declined pathway reaction space.During using folded structure, the angle a between two plates is between 5 ° ~ 180 °, between preferably 10 ° ~ 60 °.It is shown in Figure 4, it is preferable that the face channel component that declines is arranged to indirect heat exchange type structure, i.e. structure is similar to conventional board-like heat exchanger type structure, but reaction channel is that face declines channel design, introduces the taking-up that cooling medium is advantageous to reaction heat.
Micro passage reaction bottom connects with horizontal knockout drum.The material inlet of horizontal knockout drum is preferably arranged to hydrocyclone separation structure.
Liquid level gauge is installed at the housing exterior walls between micro passage reaction distributor and reaction bed, detects whether sour hydrocarbon mixed liquor has liquid layer on filler surface, with the sour inlet amount of adjustment.
Gas phase sampler is installed at the housing exterior walls between micro passage reaction reaction bed, determines whether to have vapour lock.
Every section of microchannel bed height of micro passage reaction is 30 ~ 200cm, preferably 50 ~ 150cm.
Isolated between every section of microchannel top and bottom of micro passage reaction with stephanoporate steel plate, steel plate percent opening（Steel plate perforated area accounts for the ratio of steel plate）For 10% ~ 60%, preferably 15% ~ 30%.
The alkylation process that the present invention uses, it is that, using iso-butane and alkene as raw material, propane is cryogen and entrainer, using liquid acid as catalyst, is alkylated reaction and obtains alkylate oil using the micro passage reaction of the present invention.Alkene is C3 ~ C5 alkene, preferably butylene.
Alkylation process of the present invention, sour consumption is reduced, improve the selectivity and yield of course of reaction, while alkylate oil octane number gets a promotion.Reaction pressure（Gauge pressure）Maintain 0MPa ~ 1.0MPa, preferably 0MPa ~ 0.5MPa.Residence time of the reaction mass in reactor is 1 ~ 200min, preferably 30 ~ 90min.
The mol ratio of alkylation process of the present invention, iso-butane and alkene（Alkane alkene mol ratio）For 1 ~ 50:1, preferably 5 ~ 20:1.
In alkylation reaction method of the present invention, sour hydrocarbon volume ratio is 0.1 ~ 5:1, preferably 0.5 ~ 3:1.Acid refers to the liquid catalyst including various acid and ionic liquid.
Alkylation process of the present invention, iso-butane are 1 ~ 100 with propane mol ratio:1, preferably 10 ~ 30:1.Micro passage reaction of the present invention, the bed pressure drop of microchannel alkylation reactor is smaller, is advantageous to the heat absorption vaporization of propane, reduces the focus of reaction.
As shown in Figures 1 and 2, micro passage reaction includes feed zone, microchannel reaction zone, decanting zone and Disengagement zone；The outlet of the feed zone communicates with the entrance of microchannel reaction zone；The outlet of the microchannel reaction zone communicates with the entrance of decanting zone；The outlet of the decanting zone communicates with the entrance of Disengagement zone.
Feed zone includes top distributor 11；Sour inlet tube 9, nitrogen inlet tube 8 and hydrocarbon inlet tube 10 are provided with the top distributor 11；Acid spreader 6 and hydrocarbon distributor 7 are provided with the inner chamber of top distributor 11；The outlet of the sour inlet tube 9 communicates with the entrance of acid spreader 6；The outlet of the hydrocarbon inlet tube 10 communicates with the entrance of hydrocarbon distributor 7.Level meters 12 are provided with the top distributor 11.
Microchannel reaction zone includes tubular type microchannel reaction zone, face and declined five segment structures that pathway reaction area, tubular type microchannel reaction zone, face decline pathway reaction area and tubular type microchannel reaction zone is longitudinally alternately arranged in series.13 be sampling pipe；14 be cryogen entrance；15 be thermocouple sheath；3 be distribution grid；4 be microchannel bed；5 be microchannel module.Decanting zone is transition bed 2.Disengagement zone is knockout drum 1.Gas phase outlet port 16, sour outlet port 18 and hydrocarbon outlet port 17 are provided with knockout drum 1.
After raw material enters reactor, it can be realized and be uniformly distributed by acid spreader 6 and hydrocarbon distributor 7, distributor ensures that liquid feedstock is distributed and reaches 30 ~ 200 points/m2, preferably 50 ~ 100 points/m2.Microchannel reaction zone is set below distributor, microchannel reaction zone belongs to vertical microchannel, it is made up of two parts, upper end belongs to tubular type microchannel, it is made up of the material with fiber densification hole shape structure, lower end belongs to face and declined passage, is made up of the folded plate of vertical installation, the angle a between two plates is between 10 ° ~ 60 °.Redistribution is served, is mixed, reaction and other effects.
Reference picture 2, Fig. 2 are the alkylation process schematic flow sheets provided in an embodiment of the present invention using micro passage reaction.
Using the micro passage reaction of the present invention, using iso-butane and alkene as alkylated reaction raw material, catalyst uses liquid acid catalyst, enters the distributor of reaction unit after the buffered tank of reaction raw materials by liquid inlet opening（Hydrocarbon distributor 7）It is central, acid catalyst is entered among the acid spreader 6 of reaction unit by liquid inlet opening, considerable amount of propane is added in the feed, as the cryogen and entrainer of raw material, realizes that the vaporization of raw material takes heat, ensure that reaction temperature is relatively low, material quantity and acid catalysis dosage are by the given control of Flow-rate adjustment, after the first distribution of liquid distribution trough, according to certain liquid hourly space velocity (LHSV), with drip state uniform flow, into reaction bed.Reaction raw materials can be uniformly entered to after the reaction zone of microchannel, and the tubular type microchannel reaction zone in microchannel upper end is reacted first, the great specific surface area provided by tubular type microchannel reaction zone, be advantageous to alkylated reaction, while will not produce channeling.Then, mixed, redistributed, and reacted by the face of the microchannel lower end pathway reaction area convection body that declines.Raw material mixes splendid in microchannel, and temperature accurately controls in course of reaction, and raw material proportioning accurately controls, and the yield of product significantly improves.
Material is after microchannel reaction zone reacts, into settling section, reaction mass is layered through sedimentation, because propane is different with the boiling point of iso-butane, with pressure change, propane takes hot gradually vaporization in the middle part of settling section, to sedimentation pars infrasegmentalis propane vaporization, part iso-butane also realizes vaporization, and reaction mass is layered through sedimentation, into horizontal knockout drum（For idetified separation effect, the horizontal knockout drum with rotary filter press function can be used in specific design）, lower floor's acid catalyst circulates by circulating pumped, and top tank air discharges through compressor, and middle level product enters coalescing separator by pumped, and the product after separation sends to centrifugal station or storage tank, and a small amount of acid returns to reactor.
Liquid catalyst used in alkylated reaction can be that one or more in the liquid catalyst such as liquid acid catalyst, specially HF, H2SO4, phosphoric acid, boric acid, acetic acid or ionic liquid of reaction can be arbitrarily alkylated with catalyzing iso-butane alkane and alkene.
Illustrate the reaction effect of the present invention with reference to example, but therefore do not limit the scope of the invention.
Embodiment 1 ~ 3.
Using the alkylated reaction flow shown in the reactor and Fig. 2 of structure as shown in Figure 1, the bed pressure drop of microchannel reaction zone is 0.1 ~ 1.0MPa, preferably 0 ~ 0.5MPa.Using iso-butane and butylene as raw material, using sulfuric acid as catalyst, reaction is alkylated using propane as cryogen.
It is 0.1 ~ 5 that sulfuric acid, which feeds the sour hydrocarbon volume ratio fed with iso-butane and butene mixture,:1, preferably 0.5 ~ 3:1.Alkane alkene mol ratio is 1 ~ 50:1, preferably 5 ~ 20:1.Iso-butane is 1 ~ 100 with propane mol ratio:1, preferably 10 ~ 30:1, reaction pressure maintains 0MPa ~ 1.0MPa, preferably 0MPa ~ 0.5MPa.Side reaction is inhibited, reduces sour consumption, improves the selectivity and yield of course of reaction, while alkylate oil octane number gets a promotion.Residence time of the reaction mass in reactor is 1 ~ 200min, preferably 30 ~ 90min.
Structure of reactor is：" tubular type microchannel reaction zone-face decline pathway reaction area-tubular type microchannel reaction zone-face decline pathway reaction area-tubular type microchannel reaction zone " five segment structures, the volume of every section of microchannel conversion zone are identical.The pore size of tubular type microchannel component is 3mm, and gap of the angle that face declines between the plate of channel component two between 45 °, two plates is 1mm.
Specific reaction condition is shown in Table 1, and reaction result is shown in Table 2.
Comparative example 1 ~ 2.
Comparative example 1 sets the horizontal mechanical stirred reactor of refrigeration tube bank using conventional inside, and comparative example 2 is using only tubular type microchannel component（With embodiment 1）The micro passage reaction of composition, reaction condition is referring to table 1, and reaction result is referring to table 2.
The embodiment of table 1 and comparative example alkylated reaction essential condition.
The embodiment of table 2 and comparative example alkylated reaction result.
It is appreciated that, above with respect to the specific descriptions of the present invention, it is merely to illustrate the present invention and is not limited to the technical scheme described by the embodiment of the present invention, it will be understood by those within the art that, still the present invention can be modified or equivalent substitution, to reach identical technique effect；As long as satisfaction uses needs, all within protection scope of the present invention.
Claims (9)
1. a kind of alkylation using new micro passage reaction, using iso-butane and alkene as raw material, using liquid acid as catalyst, it is alkylated reaction and obtains alkylate oil；It is characterized in that：After the microchannel reaction zone that the raw material and catalyst enter in micro passage reaction is alkylated reaction, enters back into settling section and carry out sedimentation layering；Reaction mass continues into horizontal knockout drum after sedimentation is layered, extracts lower catalyst agent out, discharge top tank air, middle level product is delivered to coalescing separator and separated again.
2. the alkylation according to claim 1 using new micro passage reaction, it is characterised in that：Propane is added in the raw material, cryogen and entrainer as raw material.
3. the alkylation according to claim 2 using new micro passage reaction, it is characterised in that：The micro passage reaction includes feed zone, microchannel reaction zone, decanting zone and Disengagement zone；The outlet of the feed zone communicates with the entrance of microchannel reaction zone；The outlet of the microchannel reaction zone communicates with the entrance of decanting zone；The outlet of the decanting zone communicates with the entrance of Disengagement zone.
4. the alkylation according to claim 3 using new micro passage reaction, it is characterised in that：The microchannel reaction zone declines pathway reaction area at least provided with a tubular type microchannel reaction zone and a face.
5. the alkylation according to claim 4 using new micro passage reaction, it is characterised in that：Tubular type microchannel reaction zone and face are declined, and longitudinally alternating is arranged in series in pathway reaction area；The number of tubular type microchannel reaction zone is 2~10；The face decline pathway reaction area number be 2~10.
6. the alkylation according to claim 5 using new micro passage reaction, it is characterised in that：Tubular type microchannel reaction zone and face the spatial volume ratio that pathway reaction area occupies that declines are 0.5~5：1.
7. the alkylation according to claim 6 using new micro passage reaction, it is characterised in that：Tubular type microchannel reaction zone is made up of tubular type microchannel component；Channel diameter is 0.1~10mm；The face pathway reaction area that declines is made up of the face channel component that declines；Path clearance is 0.1~10mm between two plates.
8. the alkylation according to claim 7 using new micro passage reaction, it is characterised in that：The reaction pressure of alkylated reaction is 0MPa~1.0MPa；Residence time of the reaction mass in reactor is 1~200min.
9. according to any described alkylation using new micro passage reaction of claim 2~8, it is characterised in that：The iso-butane of alkylated reaction and the mol ratio of alkene are 1~50:1；Sour hydrocarbon volume ratio is 0.1~5:1；Iso-butane is 1~100 with propane mol ratio:1.
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| CN108126637B (en) * | 2018-01-11 | 2023-10-13 | 辽宁石油化工大学 | Silicon carbide microchannel alkylation reactor and application method thereof |
| CN113522192A (en) * | 2020-04-20 | 2021-10-22 | 中国石油化工股份有限公司 | Apparatus and method for producing polyalphaolefins |
| CN114471378A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Olefin hydration reactor and olefin hydration method |
| CN115231984A (en) * | 2022-08-02 | 2022-10-25 | 中国石化集团金陵石油化工有限责任公司 | Alkylbenzene production process and device with efficient catalysis and rapid separation of hydrogen fluoride |
| CN115231984B (en) * | 2022-08-02 | 2023-12-19 | 中国石化集团金陵石油化工有限责任公司 | Process and device for producing alkylbenzene by high-efficiency catalysis and rapid separation of hydrogen fluoride |
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