CN108786710A - A kind of alkylation reactor and alkylation reaction method - Google Patents
A kind of alkylation reactor and alkylation reaction method Download PDFInfo
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- CN108786710A CN108786710A CN201710299527.2A CN201710299527A CN108786710A CN 108786710 A CN108786710 A CN 108786710A CN 201710299527 A CN201710299527 A CN 201710299527A CN 108786710 A CN108786710 A CN 108786710A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/30—Loose or shaped packing elements, e.g. Raschig rings or Berl saddles, for pouring into the apparatus for mass or heat transfer
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/30—Details relating to random packing elements
- B01J2219/302—Basic shape of the elements
- B01J2219/30276—Sheet
- B01J2219/30288—Sheet folded
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/30—Details relating to random packing elements
- B01J2219/304—Composition or microstructure of the elements
- B01J2219/30483—Fibrous materials
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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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Abstract
The invention discloses a kind of alkylation reactor and alkylation reaction methods, alkylation reaction zone is set inside alkylation reactor, alkylation reaction zone includes the filler tube bank loaded vertically, filler tube bank includes external cylinder and inner stuffing, inner stuffing is regular braided packing, braided packing is that fibre bundle weaves, and fibre bundle includes at least oleophilic drainage or hydrophilic and oleophobic fibre bundle.The advantages that having when reactor of the present invention is used for alkylated reaction promotes reaction mass to be sufficiently mixed, and reaction efficiency is high, and side reaction is few.
Description
Technical field
The invention belongs to petrochemical industry, specially a kind of alkylation reactor and alkylation reaction method, especially
Using sulfuric acid as the reactor and alkylation reaction method of catalyst isoparaffin and olefin alkylation reaction.
Background technology
With the increase of car ownership, vehicle exhaust is to the pollution getting worse of environment, thus to the pungent of motor petrol
More stringent requirements are proposed for alkane value and cleannes, this makes alkylation process and alkylate oil obtain extensive concern and attention.
Alkylation process is that a kind of important clean gasoline processing technology, product alkylate oil are non-conventions in oil refining process
The gasoline blend component thought, with no aromatic hydrocarbons, without alkene, low-sulfur, low-steam pressure, high-octane rating（RON 94~96, MON 92~
94）The advantages that.Current prevailing technology is liquid acid alkylation techniques, includes mainly sulfuric acid alkylation and hydrofluoric acid alkylation two
Kind, wherein since there is hydrofluoric acid very strong volatility and toxicity, China to run at present and in all sulfuric acid alkylations built
Method.In order to reduce side reaction, product quality is improved, sulfuric acid alkylation technological requirement operates at low temperature, due to sulphur under low temperature
Sour viscosity is big, extremely difficult miscible with iso-butane, thus the mixing of sour hydrocarbon is just at the focus on research direction of sulfuric acid alkylation technique.
Traditional alkylation reactor mainly uses mechanical agitation mode, as US3759318 proposes a kind of mechanical agitation
Formula acid hydrocarbon mixing reactor, reactor are provided with blender and stir the hybrid reaction for completing sour hydrocarbon by impeller high speed rotation, should
The disadvantage of method is to need high-speed stirred in sour hydrocarbon mixed process and consume a large amount of electric energy.US5443799 proposes one
Kind injection-type reactor is alkylated the technology of reaction, and feeding manner is first mixed with sulfuric acid for iso-butane and contacted again with alkene instead
It answers, i.e., iso-butane is sprayed by injector is mixed to form emulsion with sulfuric acid, and alkene carries out reverse haptoreaction with the emulsion again,
But make reaction temperature due to contacting effect etc. at it（8~20 DEG C）Higher, side reaction is serious.CN203295447U is proposed
A kind of shell and tube alkylation reactor, tube side are conversion zone, and shell side is heat exchange area, and tube body both ends are respectively pre- distributed areas
Region is flowed out with reactant, which is suitable for isoparaffin and low-carbon alkene and generates Gaoxin under liquid acid catalyst effect
The reaction of alkane value alkylate oil, since this method is conventional shell-and-tube reactor, that there are device structures is complicated, formation efficiency is low,
The problems such as material side reaction is serious in pipe.
Packing reactor is a kind of new alkylation reactor, as CN201410175970.5,
CN201310140601.8, CN201510738217.7, CN201210100634.5 etc..By taking CN201210100634.5 as an example,
The document discloses a kind of alkylation reactor, it is made of, fills out one section or more the structured packing with cavity structure in reactor
The cavity of material is provided at both ends with coolant distribution pipe, forms heat transfer zone in cavity, forms reaction zone between cavity and cavity, reacts
Area and heat transfer zone are arranged in reactor radially alternating, and reaction zone and heat transfer zone are not communicated with.Existing material filling type alkylation reactor
Although haveing a certain upgrade in certain sport technique segments tool, comprehensive performance still needs to further increase.
From the point of view of current technology development both at home and abroad, the research of new sulfur acid alkylation processes is sour based on improving mostly
Hydrocarbon mixability strengthens mass transfer, accelerates reaction rate, and how continuous and stable remove reaction heat, keep reaction process temperature,
The direction of side reaction is reduced, but still is had the following problems：（1）Since alkylated reaction is exothermic reaction, material is unevenly distributed
（Including radial material distribution and axial material are distributed）The side reaction that can aggravate olefinic polymerization occurs, and influences the product of alkylate oil
Quality；（2）Since sour hydrocarbon is immiscible, and the viscosity of acid is big, and the interfacial mass transfer resistance in the alkylation process for being is big, passes
Matter and reaction rate are low, it is therefore desirable to which the surface area for providing sour hydrocarbon reaction simultaneously, provides the mass transfer force of reaction mass also ten
Divide important；（3）Reaction heat in reaction process（Including radial reaction heat and Axial response heat）It needs to remove in time, otherwise can go out
Existing hot localised points occur side reaction and reduce reaction efficiency, and more satisfactory mode is that reactor maintains original state always
Isothermal reaction process, but actually can only be infinite approach and be unable to reach.
In conclusion for alkylation process, exploitation is a kind of uniform, anti-along the radial and axial temperature of reactor
Efficient, side reaction is answered to lack reaction process and equipment, with overcome the deficiencies in the prior art, for the advanced of alkylated reaction technology
Property and high efficiency are of great significance.
Invention content
In view of the deficiencies of the prior art, the present invention provides a kind of alkylation reactor, and filler is used in alkylation reactor
Tube bank improves reaction efficiency, reduces side reaction.
Alkylation reaction zone is arranged in a kind of alkylation reactor, alkylation reactor inside, and alkylation reaction zone includes perpendicular
The filler tube bank directly loaded, filler tube bank include external cylinder and inner stuffing, and inner stuffing is regular braided packing, braiding
Filler is that fibre bundle weaves, and fibre bundle includes at least oleophilic drainage or hydrophilic and oleophobic fibre bundle.
In the present invention, the filler tube bank of alkylation reaction zone is at least arranged two layers, and every layer of lower part setting takes hot arc.Take heat side
Formula preferably uses refrigerant vapor mode.The total height of filler tube bank is determining according to alkylated reaction required time, in general,
The sulfuric acid process alkylated reaction time is 5~60 minutes.
In the present invention, filler bundle diameters（Overall diameter）For 50mm~500mm, preferably 100mm~300mm.Loading pipe
The cross-sectional shape of beam can be round or square structure, and square structure is containing square, rectangle, regular polygon etc..Alkylation
The filler tube bank quantity being arranged in reactor is determined according to reactor scale.
In the present invention, inner stuffing is to be compressed or be fastened by multi-layer fiber braiding sheet folding of material and constitute densification
Stereoregular filling-material structure, eliminate material dispersion and the pockets of possibility of coalescence, pass through oleophilic drainage or hydrophilic and oleophobic filament
The effect of beam so that oiliness material and aqueous materials come into full contact under reaction condition, are formed intensive micro- logical under reactiveness
Road structure reduces liquid-drop diameter, increases mass transfer area.What the braiding of braided packing can be realized by following methods：It selects first
Select required performance（Oleophilic drainage is hydrophilic and oleophobic）Fibre bundle first carries out uniform tension through fiber tension device, and then multi beam is fine
Dimension twisting, plying, then it is that rope can in order to improve the wearability and service life of rope to carry out Split Down after multiply uniform tension
It is qualitative through surface resin coating, drying, become high strength fibre rope filler；The even more flat rope establishment machine of selection 1~10
All over knitting to obtain fibrage flaky material, braiding flower pattern can be any one in water-drop-shaped, wave linear shape, S-shaped etc..
In the present invention, on the inner stuffing of loading pipe beam inner barrel, material premix section can be set.Material premixes
It closes section and corrugated plate packing is set.Corrugated plate packing is multilayer, is generally horizontally disposed, the phase of corrugated plate packing in a state of use
Adjacent bed is made of the different material of surface hydrophilic oleophilic properties, i.e., odd-level loads the corrugated plating that hydrophilic oleophobic material is prepared into and fills out
Material, then even level load oleophilic drainage material preparation at filler；Conversely, odd-level filling surface is processed through oleophilic drainage
Filler, then even level load hydrophilic oleophobic material and be prepared into.It can be led in this way to avoid different due to the polarity between raw material
The short-circuit flow and mixing problem of non-uniform of cause.The trepanning of suitable number is set on corrugated plate packing, packing layer is passed through convenient for material
Flowing.The height ratio generally 1 of material premix section and inner stuffing section：3~1：20, preferably 1：5~1：15.
In the present invention, alkylation reactor inner top is normally arranged feed distributor, the normal arranging thing in bottom in reactor
Material collects discharge structure.Reactor bottom is connected to three phase separator, and reacting rear material is detached in three phase separator.Into
Expect that distributor can be in sprinkle nozzle, porous calandria, porous coiled, vertical tube type, overflow disc type, overflow groove type etc.
Any one.
In the present invention, the control pressurer system on refrigerant lines and pipeline can be set, for controlling refrigerant vapor
Pressure and amount of vaporization, and then controlling reaction temperature.
Alkylation reaction method of the present invention, alkylation reactor using the present invention, with the concentrated sulfuric acid, strong acidic ion liquid
Or the mixed acid based on the concentrated sulfuric acid is catalyst, with iso-butane and C3~C5Alkene is raw material, is alkylated reaction and obtains alkane
Base gasoline fraction.
Alkylation reactor of the present invention is used to, using sulfuric acid as the alkylation process of catalyst agent, have and promote reactant
The advantages that material is sufficiently mixed, and reaction efficiency is high, and side reaction is few.The advantages of alkylation reactor of the present invention is restrained using filler, matches
Refrigeration system is closed, realizes that reaction temperature radially reaches that temperature is uniform along reactor, improves the concentration motive force of reaction process, improve
Alkylated reaction rate takes reaction heat away, it is ensured that reactor exists in such a way that pressure control makes some refrigerant gasify
Temperature on axial direction is uniform, to reduce the side reaction of alkylation process.In short, the present invention is reacted with conventional alkylation
System is compared, and can not only substitute complicated stirred reactor structure, and can with simplification of flowsheet, reduce energy and material consumption,
And can ensure that radial and axial realization temperature is uniform in alkylation process, increase substantially reaction rate and product selection
Property, play an important roll for improving alkylation generation technique.It is mixed with material compared with conventional fillers formula alkylation reactor
The advantages that conjunction is abundant, and reaction speed is fast, and side reaction is few.
Specific implementation mode
Oleophilic drainage material involved in the present invention can select polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoro
One or more compositions in ethylene, acrylic compounds, nylon etc. use, and are to calculate every gram by its weight to inhale to its performance requirement
Receive 20mL~100mL oil；The hydrophilic oleophobic material being related to can be main chain or side chain with the natural of carboxyl, amino or hydroxyl
High molecular polymer, such as polypropylene fiber.Can also be that material surface carries out oleophilic drainage processing or hydrophilic and oleophobic processing.Filament
Beam includes at least oleophilic drainage or hydrophilic and oleophobic fibre bundle, while can also increase some materials for improving intensity, such as gold
Belong to material, ceramic material etc..
The alkylation reactor of the present invention is suitable for the concentrated sulfuric acid, strong acidic ion liquid and mixing based on the concentrated sulfuric acid
Close the liquefied alkyl reaction process that acid is catalyst, the mixed acid preferably based on the concentrated sulfuric acid.Wherein, described with the concentrated sulfuric acid
Based on mixed acid in concentrated sulfuric acid content be generally the wt% of 85wt%~98；The sour hydrocarbon volume ratio is 0.1:1~5:1, preferably
It is 0.5:1~3:1.
The present invention alkylation reactor, applicable alkylated reaction raw material be contain iso-butane, C3~C5Alkene evaporates
Point, the alkane alkene molar ratio in the alkylated reaction raw material is 1:1~20:1, preferably 5:1~15:1.
The alkylation reactor of the present invention, applicable alkylated reaction operating condition are：Pressure is 0.05~1.0MPaG,
It is preferred that 0.1~0.5MPaG；Temperature is -4~15 DEG C, preferably -3~7 DEG C.
The alkylation reactor of the present invention, iso-butane and propane molar ratio are 5 in applicable alkylation process:1~
50:1, preferably 15:1~30:1.
The process and effect of method are further illustrated the present invention by the following examples.
In embodiment, filler restrains the rounded cylindrical structure for a diameter of 300mm；Wherein material premix section is provided that
The corrugated plate packings of two kinds of horizontal superpositions, the corrugated plate packing of odd-level are that the surface punching crossed by hydrophilic material treatment is stainless
The corrugated plate packing of steel, even level is that polypropylene is punched on surface；Wherein inner stuffing section is to weave flaky material by multi-layer fiber
It folds and compresses and constitute fine and close structured packing structure, it is polytetrafluoroethylene (PTFE), nylon, metal fiber wire three which, which knits piece,
Kind material mixing（Examples 1 and 2）And polypropylene fiber（Embodiment 3）It is water-drop-shaped decorative pattern to be woven to water-drop-shaped decorative pattern.Reaction
Residence time reaches 100% determination with butene conversion.
Comparative example 1
Using sulfuric acid process stirring-type alkylation reactor, bundled tube heat collector, reaction condition and reaction knot is arranged in inside reactor
Fruit sees Tables 1 and 2 respectively.
Comparative example 2
Using sulfuric acid process material filling type alkylation reactor, the ceramic Pall ring filler of inside reactor filling, the interior setting pipe of reactor
Beam formula heat collector, reaction condition and reaction result are shown in Tables 1 and 2 respectively.
Comparative example 3
Using sulfuric acid process material filling type alkylation reactor, inside reactor integrally loads the braiding of the polypropylene fiber used in embodiment 3
Filler, bundled tube heat collector is set in reactor, and reaction condition and reaction result are shown in Tables 1 and 2 respectively.
Embodiment 1
Using the method for the present invention, it is provided with the three phase separator of three groups of alkylation reaction zones and bottom, alkylated reaction therein
Section by filler tube bundle region and hot-zone being taken to form, filler tube bank be only in a manner of setting inner stuffing in filler of the present invention is restrained,
Hot-zone is taken to take heat, reactor bottom to connect three phase separator using heat exchange tube structure, to isolate gasification cryogen, thick alkylate oil
With mixing sulfuric acid, reaction condition and reaction result are shown in Tables 1 and 2 respectively.
Embodiment 2
Using the method for the present invention, it is provided with the three phase separator of three groups of alkylation reaction zones and bottom, alkylated reaction therein
Section is by filler tube bundle region and refrigerant vapor district's groups at the structure of filler tube bank is used by material premix section and inner stuffing section
Composition（Height ratio 1：12）, setting refrigerant vapor section, cryogen gasification pipeline and corresponding in the lower part of every group of alkylation reaction zone
Voltage-controlled system, reactor bottom connect three phase separator, with isolate vaporised refrigerant, thick alkylate oil and mixing sulfuric acid,
Reaction condition and reaction result are shown in Tables 1 and 2 respectively.
Embodiment 3
Using the method for the present invention, it is provided with the three phase separator of three groups of alkylation reaction zones and bottom, alkylated reaction therein
Section is made of filler tube bundle region and cryogen gasification zone, and filler tube bank is made of material premix section and inner stuffing section（Height ratio
1：8）, setting refrigerant vapor section, refrigerant vapor pipeline and corresponding voltage-controlled system in the lower part of every group of alkylation reaction zone,
Reactor bottom is connect with three phase separator, to isolate the refrigerant, thick alkylate oil and mixing sulfuric acid of gasification, reaction condition
And reaction result is shown in Tables 1 and 2 respectively.
The alkylation reaction condition of table 1 embodiment and comparative example
2 embodiment of table and comparative example alkylated reaction result
Alkylation reaction technique using the present invention and system are can be seen that from the present embodiment and comparative example result, on the one hand may be used
To realize that axially and radially to reach temperature in alkylation reactor uniform, to which side reaction be greatly reduced, selecting response is improved
Property and product octane number, on the other hand can increase substantially reaction rate, reduce the residence time, reduce acid consumption, have notable
Economy.
Claims (10)
1. a kind of alkylation reactor, alkylation reaction zone is arranged in alkylation reactor inside, it is characterised in that：Alkylated reaction
Area includes the filler tube bank loaded vertically, and filler tube bank includes external cylinder and inner stuffing, and inner stuffing is regular braiding
Filler, braided packing are that fibre bundle weaves, and fibre bundle includes at least oleophilic drainage or hydrophilic and oleophobic fibre bundle.
2. alkylation reactor described in accordance with the claim 1, it is characterised in that：Filler tube bank is at least arranged under two layers, every layer
Portion's setting takes hot arc.
3. alkylation reactor described in accordance with the claim 1, it is characterised in that：Filler bundle diameters are 50mm~500mm, excellent
It is selected as 100mm~300mm.
4. alkylation reactor described in accordance with the claim 1, it is characterised in that：It is round or side that filler, which restrains cross-sectional shape,
Shape structure.
5. alkylation reactor described in accordance with the claim 1, it is characterised in that：The inner stuffing of loading pipe beam inner barrel it
On, material premix section is set.
6. alkylation reactor according to claim 5, it is characterised in that：Corrugated plate packing is arranged in material premix section.
7. alkylation reactor according to claim 6, it is characterised in that：Corrugated plate packing is multilayer, in use state
Lower is horizontally disposed, and the adjacent layer of corrugated plate packing is made of the different material of surface hydrophilic oleophilic properties, i.e., odd-level loads
The corrugated plate packing that hydrophilic oleophobic material is prepared into, then even level load oleophilic drainage material preparation at filler；Conversely, odd number
Layer filling surface loads what hydrophilic oleophobic material was prepared into through the processed filler of oleophilic drainage, then even level.
8. alkylation reactor according to claim 7, it is characterised in that：Opening for suitable number is set on corrugated plate packing
Hole.
9. alkylation reactor according to claim 5, it is characterised in that：The height of material premix section and inner stuffing section
Degree is than being 1：3~1：20.
10. a kind of alkylation reaction method is catalysis with the concentrated sulfuric acid, strong acidic ion liquid or the mixed acid based on the concentrated sulfuric acid
Agent, with iso-butane and C3~C5Alkene is raw material, is alkylated reaction and obtains gasoline alkylate fraction, it is characterised in that uses
Alkylation reactor described in claim 1 to 9 any claim.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114425260A (en) * | 2020-10-29 | 2022-05-03 | 中国石油化工股份有限公司 | Liquid-liquid mixing device and mixing method |
| 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 |
| CN114471300A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Micro-channel assembly, micro-channel mixing equipment, mixing system and application |
| CN114507116A (en) * | 2020-10-28 | 2022-05-17 | 中国石油化工股份有限公司 | Olefin hydration reaction method |
| CN114505017A (en) * | 2020-10-28 | 2022-05-17 | 中国石油化工股份有限公司 | Olefin hydration reaction device and olefin hydration method |
| CN115350508A (en) * | 2022-08-02 | 2022-11-18 | 中国石化集团金陵石油化工有限责任公司 | Hydrogen fluoride and alkylate oil separator and separation method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR19980029862A (en) * | 1996-10-28 | 1998-07-25 | 김성년 | Manufacturing method and contact method for high density fiber bundles and apparatus thereof |
| CN101402881A (en) * | 2008-07-09 | 2009-04-08 | 彭鸽威 | Method stabilizing color of prime city naphtha |
| CN103980934A (en) * | 2014-05-19 | 2014-08-13 | 华东理工大学 | Deep dehydrating method and device for oil product |
| CN104587926A (en) * | 2013-10-31 | 2015-05-06 | 中国石油化工股份有限公司 | Microfilament contact reactor and alkylation reaction method |
| CN105944652A (en) * | 2016-06-22 | 2016-09-21 | 辽宁石油化工大学 | Tubular micro-channel alkylation reactor and application method thereof |
| CN106390881A (en) * | 2016-10-10 | 2017-02-15 | 辽宁石油化工大学 | Microchannel reactor internal component module for liquid acid alkylation reaction and filling method of microchannel reactor internal component module |
-
2017
- 2017-05-02 CN CN201710299527.2A patent/CN108786710A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR19980029862A (en) * | 1996-10-28 | 1998-07-25 | 김성년 | Manufacturing method and contact method for high density fiber bundles and apparatus thereof |
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