CN107974280A - A kind of liquid acid alkylation reaction method - Google Patents
A kind of liquid acid alkylation reaction method Download PDFInfo
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- CN107974280A CN107974280A CN201610937335.5A CN201610937335A CN107974280A CN 107974280 A CN107974280 A CN 107974280A CN 201610937335 A CN201610937335 A CN 201610937335A CN 107974280 A CN107974280 A CN 107974280A
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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
- C10G2300/70—Catalyst aspects
Abstract
A kind of liquid acid alkylation reaction method, the alkylation reactor of use from top to bottom includes light phase Disengagement zone (I), reaction zone (III), circulating-area (II) and heavy phase decanting zone (IV), the wherein described reaction zone (III) and circulating-area (II) both ends communicates respectively, described reaction zone (III) bottom sets dispersed phase feeder (4), and continuous phase entrance (1) is set in the circulating-area (II) of sidewall of reactor；Reaction zone and the reaction mixture that circulating-area is liquid acid catalyst, the mixture of isoparaffin and alkene is dispersed through phase feeder and enters reaction zone, alkylated reaction occurs for isoparaffin and alkene under alkylation reaction condition, enter circulating-area after reaction, wherein light phase enters the light phase Disengagement zone on reactor top, heavy phase enters the heavy phase decanting zone of reactor lower part, and alkylation reaction product is produced from light phase export, and waste liquid body catalyst is produced from heavy out.The high selectivity of liquid acid alkylated reaction provided by the invention.
Description
Technical field
The present invention relates to a kind of alkylation reaction method, and new alkylation reactor is used more specifically to one kind
Liquid acid alkylation reaction method.
Technical background
With increasingly harsh, the most important thing for being produced into vast oil plant of clean fuel of environmental regulation.Although refining
There are a variety of gasoline blending components such as catalytically cracked gasoline, Reformed Gasoline, alkylate oil, isomerized oil and etherified gasoline in oily factory,
But alkylate oil is compared with other blending components, there is not olefin-containing and aromatic hydrocarbons, and the advantages such as sulfur content is extremely low, therefore obtain
Greatly pay attention to, alkylation techniques are also continued to develop.With the continuous improvement of alkylation process technology, alkyl plant exists
Status in petroleum refining industry's production also becomes more and more important.
Alkylation refers to that isoparaffin and light olefin produce alkylate, the alkyl under acidic catalyst effect
Change the product usually octane number with than raw material higher, and belong to gasoline fraction.In petroleum refining, which typically refers to
The reaction of C3-C5 alkene and iso-butane.Alkylation catalyst includes liquid acid and solid acid, wherein, liquid acid catalyst is main
Including hydrofluoric acid, sulfuric acid or ionic liquid etc..
Liquid acid catalytic alkylation reaction usually operates under cryogenic, favors low temperature in reduce side reaction generation,
And the selectivity of product can be improved.In traditional method, hydrocarbon raw material is dispersed in continuous acid solution, therefore acid is used
Measure larger.Although this method needs to use strong acid to have very strong corrosivity, the waste residue pair of generation to equipment as catalyst
Environment pollutes, and hydrofluoric acid can also damage human body, but being capable of complete generation there is presently no other effective ways
For this method, liquid acid catalytic alkylation reaction is still to be used to produce the main of high octane gasoline component on our times
Method.
Research in terms of major part liquid acid at present is focused primarily upon to liquid acid alkylation reactor and sour hydrocarbon separation
Equipment is improved and improves, to reduce its adverse effect.Specifically, include documents below in terms of reactor：
CN101104570A discloses a kind of liquid acid alkylation, and this method includes：Will be substantially by alkene, alkene
The hydrocarbon component of precursor or its mixture and isoparaffin composition is incorporated into the dirty reaction zone comprising disperser；By vaporizing zone simultaneously
Enter the container comprising the reaction zone or be incorporated in the also independent container comprising disperser；Grasped in the bubble point of the hydrocarbon component
Make vaporizing zone, so as to exported by the vaporization for adjusting the flow-rate ratio hydrocarbon of hydrocarbon/acid/steam in the vaporizing zone with stream of pulses
State or the formal operations close to pulse flow regime.
US5785933 discloses a kind of sulfuric acid alkylation reactor, which includes：Reactor vessel, the reactor
Container has the baffle of vertical cylindrical wall, top, inverted conical lower section and inner perforated；Sedimentation vessel, this is heavy
Drop container is used to separate sulfuric acid catalyst from alkylates；Delivery pipe, which, which has, is suspended in the reaction
The vertical component effect at the middle part of device, the cylindrical wall of reactor described in hermetically passing and the horizontal part connected with the sedimentation vessel, should
Delivery pipe, which has, is provided towards the first end of the inverted conical base and the second end at the top of the sedimentation vessel；
And multiple lotion ascending pipes that are tangentially-arranged and being connected with the inside of the reactor, the lotion ascending pipe are used for reactant
Inject in the reaction vessel.
US4075258 discloses a kind of improved alkylation reaction method, and this method, which is based on the discovery that, to be alkylated medium
The motor octane number for the alkylates that can be improved, therefore this method institute are stirred under higher than critical mixing intensity
Hybrid element is provided with the reactor used.
CN101679143A discloses a kind of be used for hydrocarbon containing at least one isoparaffin and at least one alkene
The system that compound is alkylated, the system include：At least one external high shear mixing arrangement, it contains at least one
Rotor and at least one stator, between be separated with shear gap, wherein shear gap is at least one rotor and at least one stator
Between minimum range, wherein high shear device can be produced more than 22.9m/s at the tip of at least one rotor
Blade tip speed；It is configured to the pressurization liquid stream containing liquid acid catalyst being shipped at least one shearing force mixing arrangement
Pump；And it is configured to receive the container of emulsion from high shear device.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of liquefied alkyl reaction method using novel reactor.
A kind of liquid acid alkylation reaction method, the alkylation reactor of use from top to bottom include light phase Disengagement zone I, anti-
Area III, circulating-area II and heavy phase decanting zone IV are answered, wherein the reaction zone III and circulating-area II both ends is communicated respectively, it is described
Reaction zone III bottoms dispersed phase feeder 4, the dispersed phase entrance 3 of the dispersed phase feeder 4 and reactor bottom are set
Connection, sets continuous phase entrance 1 in the circulating-area II of sidewall of reactor, light phase export 2, heavy phase is equipped with the top of the I of light phase Disengagement zone
Decanting zone IV bottoms are equipped with heavy out 5；Reaction zone and circulating-area are full of the reaction mixture containing liquid acid catalyst, isomery
The mixture of alkane and alkene is dispersed through phase feeder and enters reaction zone, isoparaffin and alkene hair under alkylation reaction condition
Raw alkylated reaction, reaction stream enter circulating-area, and light phase therein enters the light phase Disengagement zone on reactor top, and heavy phase enters
The heavy phase decanting zone of reactor lower part, alkylation reaction product is produced from light phase export, from heavy out extraction waste liq catalysis
Agent.
Liquid acid alkylation reaction method provided by the invention has the beneficial effect that：
Liquid acid alkylation reaction method provided by the invention uses new alkylation reactor, including light phase separation
Area, reaction zone, circulating-area and heavy phase decanting zone, reaction zone bottom set dispersed phase feeder, and alkylated reaction raw material is with small
Droplet distribution improves alkylated reaction raw material and liquid acid catalyst phase in the reaction mixture containing liquid acid catalyst
Between mass transfer surfaces, be conducive to improve reaction efficiency；Circulated by setting circulating-area to realize in the device of liquid acid catalyst, with by means of
Help the reactor that mechanical pump carries out outer circulation to compare, advantageously reduce plant energy consumption.
Brief description of the drawings
Attached drawing 1 calculates the flow diagram of alkylation reaction method for liquid provided by the invention.
Attached drawing 2 is reaction zone, circulating-area layout in alkylation reactor.
Attached drawing 3 is the schematic diagram that filler is loaded in alkylation reactor light phase Disengagement zone.
Attached drawing 4 is the schematic diagram that baffle is set in alkylation reactor light phase Disengagement zone.
Reference numeral：
1- continuous phase entrances, 2- light phase exports, 3- dispersed phase entrances, 4- dispersed phase feeders, 5- heavy outs；I-light phase
Disengagement zone, II-circulating-area, III-reaction zone, IV-heavy phase decanting zone.
Embodiment
Alkylation reactor is calculated to liquid provided by the invention with concrete technical scheme below in conjunction with the accompanying drawings to further illustrate,
But content not thereby limiting the invention.
A kind of liquid acid alkylation reaction method, the alkylation reactor of use from top to bottom include light phase Disengagement zone I, anti-
Area III, circulating-area II and heavy phase decanting zone IV are answered, wherein the reaction zone III and circulating-area II both ends is communicated respectively, it is described
Reaction zone III bottoms dispersed phase feeder 4, the dispersed phase entrance 3 of the dispersed phase feeder 4 and reactor bottom are set
Connection, sets continuous phase entrance 1 in the circulating-area II of sidewall of reactor, light phase export 2, heavy phase is equipped with the top of the I of light phase Disengagement zone
Decanting zone IV bottoms are equipped with heavy out 5；Reaction zone and circulating-area are full of the reaction mixture containing liquid acid catalyst, isomery
The mixture of alkane and alkene is dispersed through phase feeder and enters reaction zone, isoparaffin and alkene hair under alkylation reaction condition
Raw alkylated reaction, enters circulating-area after reaction, wherein light phase enters the light phase Disengagement zone on reactor top, and heavy phase enters reaction
The heavy phase decanting zone of device lower part, alkylation reaction product is produced from light phase export, and waste liquid body catalyst is produced from heavy out.
In liquid acid alkylation reaction method provided by the invention, the dispersed phase feeder uses pressure type feeding
The mixture of device, the isoparaffin and alkene in the dispersed phase feeder with there are certain pressure in reactor
Difference, by the way that pressure difference potential energy to be transformed into the kinetic energy and surface energy of dispersed phase fluid, makes fluid dispersion into small drop.It is preferred that
Pressure difference is 0.02-3.0MPa before and after the mixture charging of ground, the isoparaffin and alkene, the isoparaffin and alkene
Mixture into dispersed phase feeder outlets initial flow rate be 2-40m/s, the dispersed phase feeder outlets isoparaffin
Mixture droplets diameter range with alkene is 0.1-1000 μm.
In liquid acid alkylation provided by the invention, the hydrocarbon raw material and liquid acid catalyst of alkylated reaction are alkane
The convenient source and catalyst of glycosylation reaction.Preferably, the liquid acid catalyst is selected from hydrofluoric acid, sulfuric acid trifluoromethanesulfonic acid
With the one or more in ionic liquid；The isoparaffin is the one or more in the isoparaffin of C3-C7；The alkene
Hydrocarbon is the monoolefine of C3-C5；The molar ratio of isoparaffin and alkene is 100- in the mixture of the isoparaffin and alkene
500:1。
Preferably, the alkylation reaction condition is：Temperature is -20 DEG C -100 DEG C, reaction pressure 0.1MPa-
2MPa。
Preferably, the dispersed phase feeder 4 is antipriming pipe, sintered metal tube or atomizer.
The reaction zone III arranges for single reaction tube or multiple reaction tubes, wherein each reaction bottom of the tube setting pair
The dispersed phase feeder 4 answered.Preferably, multiple reaction tubes arrange in the reaction zone.
Preferably, the circulating-area II sectional areas are 0.8-4.0 times, more preferably 1.0- of reaction zone III total sectional areas
3.5 again.
Preferably, the light phase Disengagement zone I is 1.0-3.0 times of circulating-area II outside diameters.The heavy phase decanting zone IV
For 1.0-3.0 times of circulating-area II outside diameters.
Preferably, filler or baffle are set in the light phase Disengagement zone I and/or heavy phase decanting zone IV, for improve liquid-
Liquid separative efficiency.
Preferably, baffle is set in the light phase Disengagement zone I, and the baffle slant setting, is staggered, angle of inclination beta
For 5-30 °.Aperture, bore dia 1-10mm are provided with more preferably described baffle.
Liquid acid alkylation provided by the invention, alkane and olefin feedstock are passed through as dispersed phase from reaction zone bottom
Dispersed phase feeder adds, and is highly dispersed in the form of fine droplet in the reaction mixture containing liquid acid catalyst.Newly
Continuous phase entrance of the fresh liquid acid catalyst in the middle part of circulating-area adds, and flows to reaction zone with circulating liquid acid catalyst
The arrival end of bottom, and the raw material for alkylation flowed up at a high speed is carried along into reaction zone, is catalyzed alkane and alkane occurs for alkene
Glycosylation reaction.Exported in reaction zone, since fluid velocity drastically declines, reaction mixture rapid realization body due to density contrast
Split-phase, wherein alkylation reaction product and unreacted alkane flow up into light phase Disengagement zone, and liquid acid catalyst enters
Circulating-area simultaneously flows downward.In light phase Disengagement zone and heavy phase decanting zone, the weight component of entrainment is further separated out coming, hydrocarbon phase
Produced from reactor head, spent acid catalyst is discharged from reactor bottom.
The liquid acid catalyst can be that the various alkylated reactions to isoparaffin and alkene have catalytic action
Liquid acid, preferred one or more therein such as hydrofluoric acid, sulfuric acid trifluoromethanesulfonic acid and ionic liquid, more preferably sulfuric acid
Or hydrofluoric acid.The alkane refers to isoparaffin, be preferably C3-C7 isoparaffin in one or more, such as can be with
For iso-butane and/or isopentane, more preferably iso-butane.The alkene refers to contain carbon-carbon double bond (- C=in molecular structure
C- organic compound), be preferably C3-C5 monoolefine, such as can be propylene, C 4 olefin C_5 olefins, in one kind
Or it is a variety of, it is more preferably C 4 olefin.Relative scale between the isoparaffin and alkene can be conventional selection.Generally
Ground, the molar ratio of isoparaffin and the alkene can be 50-600 in the reaction zone:1, it is preferably 100-500:1.
In liquid acid alkylation provided by the invention, the alkylation reaction condition reacts bar for conventional alkylation
Part, wherein -100 DEG C of reaction temperature -20 DEG C, preferably -10 DEG C -50 DEG C, more preferably -5 DEG C -40 DEG C；Reaction pressure is to maintain to react
System is advisable for liquid phase, and optional pressure is 0.1MPa-2MPa, preferably 0.3MPa-0.6MPa.
In liquid acid alkylation provided by the invention, the dispersed phase feeder uses pressure type feeding device, into
One or more of combinations of the glassware in antipriming pipe, sintered metal tube and atomizer.Dispersed phase main fluid and reactor
Between there are certain pressure differential, by the way that pressure difference potential energy to be transformed into the kinetic energy and surface energy of dispersed phase fluid, by fluid dispersion
Into small drop.The drop, which enters after reactor, to be occurred mutually shearing between continuous phase fluid and is crushed again,
Drop size is set further to diminish.
Isoparaffin and alkene are dispersed through phase feeder and enter reaction zone bottom, main fluid in the dispersed phase feeder
Pressure differential range is 0.02-3.0MPa between reactor, and dispersed phase feeder fluid outlet initial flow rate is 2-40m/s, as
The isoparaffin and alkene liquid-drop diameter scope of dispersed phase are 0.1-1000 μm.
In the reaction zone, the liquid acid that isoparaffin and alkene are dispersed in the form of microlayer model as continuous phase is urged
In agent, great mass transfer surfaces are conducive to strengthen mass transfer and reaction, simultaneously because dispersed phase flow velocity is very fast, drive continuous phase one
Rise by whole reaction zone in the form of laminar flow, in favor of reducing local back-mixing.
In the circulating-area, raw material for alkylation and liquid acid catalyst are mainly realized by density contrast and separated, wherein gently
Phase main body enters the light phase Disengagement zone of reactor head, and heavy phase main body enters the heavy phase decanting zone of reactor bottom.
1.0-3.0 times of a diameter of circulating-area diameter in light phase Disengagement zone and heavy phase decanting zone, changeover portion vertical angle
0-60 ° of degree.In light phase Disengagement zone and heavy phase decanting zone, two-phase is separated by density contrast, can also be coalesced by adding
Material accelerates split-phase, and coalescence material can use two kinds of forms of filler and baffle.Wherein baffle uses slant setting, staggered row
Row, angle of inclination beta scope are 5-30 °, and aperture, bore dia 1-10mm are provided with baffle.In use, fluid is separated in light phase
When residence time in area and heavy phase decanting zone is 0.1-2 small.
Attached drawing 1 is the flow diagram of liquid acid alkylation reaction method provided by the invention.By attached drawing 1 as it can be seen that liquid
Acid catalyst enters circulating-area II from continuous phase entrance 1, and the entrance of reaction zone III is downwardly towards after being mixed with reaction mixture.
Alkylated reaction raw material is introduced from dispersed phase entrance 3, is dispersed through entering reaction zone III after phase feeder 4 is dispersed into fine droplet.
Pressure differential range is 0.02-3.0MPa before and after dispersed phase feeder, and dispersed phase fluid outlet initial flow rate is 2-40m/s.Reacting
Area's III arrival ends, occur mutually shearing collision and complete second-time breakage, make drop size into one between drop and continuous phase fluid
Step diminishes, while most of continuous phase fluid is carried and into reaction zone III and completes the mass transfer of active component by high velocity flow of droplets
And reaction.In the reaction zone III ports of export, since reaction stream fluid velocity reduces, two phase factor density contrast realization body point of weight
From realizing the further separation of weight two-phase in circulating-area II, wherein light phase is enriched with upwards, and heavy phase flows downward.Light phase master
Body carries a small amount of heavy phase and enters light phase Disengagement zone I, and heavy phase fluid carries part light phase and enters heavy phase decanting zone IV.Complete separated
Light phase is produced from the outlet 2 of reactor head, and the heavy phase after sedimentation is produced from the heavy out 5 of reactor bottom.
In order to accelerate two-phase laminated flow, coalescence material, coalescence are optionally placed in light phase Disengagement zone I and heavy phase decanting zone IV
Material can use two kinds of forms of filler and baffle, it is preferred to use baffle, wherein baffle use slant setting, are staggered, and tilt
Angle beta scope is 5-30 °, and aperture, bore dia 1-10mm are provided with baffle.
A kind of application for the alkylated reactor of liquid acid provided by the invention is illustrated by embodiment below to imitate
Fruit.
Embodiment 1
As shown in Figure 1, wherein reaction zone is single reaction pipe to the alkylation reactor used, diameter 22mm, and reaction zone is total
High 1600mm, circulating-area diameter 40mm, circulating-area net sectional area are 2.3 times of reaction zone total sectional area, and light phase Disengagement zone is straight
Footpath is 2.0 times of circulating-area outside diameter, 30 ° of changeover portion vertical angle, 1.2 times of a diameter of circulating-area outside diameter in heavy phase Disengagement zone, weight
Mutually settled by free gravity, residence time of material 40min wherein in light phase Disengagement zone, residence time of material in heavy phase decanting zone
1h。
Raw material as isoparaffin is based on iso-butane, and purchased from Beijing Hua Yuan gases Chemical Co., Ltd., it is formed
Listed in table 1；Carbon four is derived from Yanshan Mountain branch company of China Petrochemical Corp. oil plant as the raw material of alkene using after ether
MTBE devices, its composition are listed in table 1.It is anti-using entering as the concentrated sulfuric acid of catalyst (mass concentration 94%) through entrance 1
Answer device circulating-area, the mixed material of isoparaffin and alkene is dispersed through phase feeder and enters reaction zone bottom, with catalyst together
Flowed up in reaction tube and alkylated reaction occurs, dispersed phase feeder is atomizer, front and rear pressure difference 1.0MPa, and nozzle goes out
Mouth flow velocity 25m/s.The volume ratio of isoparaffin and alkene is 300 in raw material:1；Reaction temperature is controlled at 6~10 DEG C；Reactor
Interior apparent pressure is 0.5MPa.
Using the composition of gas chromatography analysis alkylate (see RIPP 80-90, Petrochemical Engineering Analysis method, Yang Cui
Fixed wait is compiled, nineteen ninety), as a result listed in table 2.Using the trimethylpentane (TMP) and dimethylhexane as alkylate
(DMH) molar ratio TMP/DMH carrys out the selectivity of evaluation response.Since trimethylpentane has higher octane number,
The ratio of TMP/DMH is bigger, illustrates that selectivity is better.
Embodiment 2
Multiple reaction tubes are equipped with the reaction zone of the alkylation reactor used in embodiment 2, it is laid out such as the institute of attached drawing 2
Show, reaction zone single tube diameter 30mm, always high 2400m, circulating-area diameter 120mm, circulating-area net sectional area are reaction to reaction zone
1.3 times of area's total sectional area, 1.5 times of a diameter of circulating-area outside diameter in light phase Disengagement zone, 45 ° of changeover portion vertical angle, heavy phase point
It is identical with circulating-area outside diameter from area's diameter, residence time of material 1h in light phase Disengagement zone, residence time of material in heavy phase decanting zone
1.5h, heavy phase Disengagement zone are filled with filler.
Raw material for alkylation isoparaffin and alkene used are the same as embodiment 1.Using as the hydrofluoric acid of catalyst, (mass concentration is
88%) reactor loop area is sent into through continuous phase entrance, the reacted bottom of the tube of mixed material of isoparaffin and alkene is disperseed
Phase feeder enters reaction zone, is together flowed up with catalyst in reaction tube and alkylated reaction occurs, dispersed phase feeder
For metal sintering pipe, front and rear pressure difference 0.4MPa.The volume ratio of isoparaffin and alkene is 200 in raw material:1；Reaction temperature is 35
~40 DEG C；Apparent pressure in reactor is 0.6MPa.The composition result of alkylate is listed in table 2.
Table 1
Table 2
Claims (12)
1. a kind of liquid acid alkylation reaction method, it is characterised in that the alkylation reactor of use from top to bottom includes light phase
Disengagement zone (I), reaction zone (III), circulating-area (II) and heavy phase decanting zone (IV), wherein the reaction zone (III) and circulation
Area (II) both ends communicate respectively, and the reaction zone (III) bottom sets dispersed phase feeder (4), dispersed phase charging
Device (4) is connected with the dispersed phase entrance (3) of reactor bottom, and continuous phase entrance is set in the circulating-area (II) of sidewall of reactor
(1), light phase export (2) is equipped with the top of light phase Disengagement zone (I), heavy phase decanting zone (IV) bottom is equipped with heavy out (5)；Reaction zone
The reaction mixture containing liquid acid catalyst is full of with circulating-area, and the mixture of isoparaffin and alkene is dispersed through phase feeder
Into reaction zone, alkylated reaction occurs for isoparaffin and alkene under alkylation reaction condition, and reaction stream enters circulating-area,
Light phase therein enters the light phase Disengagement zone on reactor top, and heavy phase enters the heavy phase decanting zone of reactor lower part, goes out from light phase
Mouth extraction alkylation reaction product, waste liquid body catalyst is produced from heavy out.
2. liquid acid alkylation reaction method described in accordance with the claim 1, it is characterised in that the isoparaffin and alkene
Mixture charging before and after pressure difference be 0.02-3.0MPa, the mixture of the isoparaffin and alkene is into dispersed phase charging
Device outlet initial flow rate is the mixture droplets diameter of 2-40m/s, the dispersed phase feeder outlets isoparaffin and alkene
Scope is 0.1-1000 μm.
3. liquid acid alkylation described in accordance with the claim 1, it is characterised in that the liquid acid catalyst is selected from hydrogen
One or more in fluoric acid, sulfuric acid trifluoromethanesulfonic acid and ionic liquid；The isoparaffin is in the isoparaffin of C3-C7
One or more；The alkene is the monoolefine of C3-C5；Isoparaffin and alkene in the mixture of the isoparaffin and alkene
The molar ratio of hydrocarbon is 100-500:1.
4. liquid acid alkylation described in accordance with the claim 1, it is characterised in that the alkylation reaction condition is：
Temperature is -20 DEG C -100 DEG C, reaction pressure 0.1MPa-2MPa.
5. liquid acid alkylation reaction method described in accordance with the claim 1, it is characterised in that the dispersed phase feeder
(4) it is antipriming pipe, sintered metal tube or atomizer.
6. liquid acid alkylation reaction method described in accordance with the claim 1, it is characterised in that described circulating-area (II) section
Product is 0.8-4.0 times of reaction zone (III) total sectional area.
7. according to the liquid acid alkylation reaction method described in claim 6, it is characterised in that described circulating-area (II) section
Product is 1.0-3.5 times of reaction zone (III) total sectional area.
8. the liquid acid alkylation reaction method described in accordance with the claim 1, it is characterised in that the light phase separation
Area (I) is 1.0-3.0 times of circulating-area (II) outside diameter.
9. liquid acid alkylation reaction method described in accordance with the claim 1, it is characterised in that the heavy phase decanting zone (IV)
For 1.0-3.0 times of circulating-area (II) outside diameter.
10. according to any liquid acid alkylation reaction method in claim 1-9, it is characterised in that described is light
Filler or baffle are set in phase separation region (I) and/or heavy phase decanting zone (IV).
11. according to the liquid acid alkylation reaction method described in claim 10, it is characterised in that the light phase Disengagement zone
(I) baffle is set in, and the baffle slant setting, is staggered, and angle of inclination beta is 5-30 °.
12. according to the liquid acid alkylation reaction method described in claim 11, it is characterised in that be provided with the baffle straight
Footpath is the aperture hole of 1-10mm.
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| CN115197171A (en) * | 2021-04-13 | 2022-10-18 | 中国石油化工股份有限公司 | Method and system for producing propylene oxide |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115197171A (en) * | 2021-04-13 | 2022-10-18 | 中国石油化工股份有限公司 | Method and system for producing propylene oxide |
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