CN105251433B - A kind of liquid acid alkylation reactor and its application process - Google Patents
A kind of liquid acid alkylation reactor and its application process Download PDFInfo
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Abstract
A kind of liquid acid alkylation reactor and its application process, from top to bottom include mixed zone, reaction zone and liquid collecting zone, least one set injection stream blender is set in described mixed zone, every group of injection stream blender is centrosymmetric ejector at least two same levels, the entrance of the described injection stream blender of described liquid collecting zone Jing circulating pump connections, described reaction zone arranges gas outlet, and liquid product outlet is arranged under described gas outlet.The liquid acid alkylation reactor that the present invention is provided is applied to alkylated reaction of the liquid acid for catalyst.The reactor is a kind of simple structure, compact, invests little, operates easy to maintenance, saves the alkylation reactor of power again.
Description
Technical field
The present invention relates to a kind of reactor of petrochemical industry, more particularly, it relates to a kind of isoparaffin and alkene
The reactor of reaction is alkylated under liquid acid catalysiss.
Background technology
Isoparaffin and the alkylated reaction of alkene, are primarily referred to as the alkylated reaction of isobutane and butene, its reaction
Essence is organic additive reaction alkane molecule being added on olefin hydrocarbon molecules in the presence of acidic catalyst.Alkylated reaction
It is an important technical process in petrochemical industry.Isobutane and butene reacts the isomery C of generation under strong acid catalyst effect8
Alkane, referred to as gasoline alkylate.Gasoline alkylate has high-octane rating (RON94～96) and low Reid vapour pressures, sulfur content, alkene
Hydrocarbon content is extremely low, without benzene and aromatic hydrocarbons, is excellent gasoline blend component.Using reformulated gasoline as petrolic combustion
Material, it will relax significantly the urban air pollution caused due to Extract from Gasoline-fueled Vehicle discharge.For this meaning, gasoline alkylate is one
Plant eco-friendly petrochemicals.
The at present catalyst adopted by industrial alkylated reaction is mainly the liquid strong acid such as concentrated sulphuric acid or Fluohydric acid..Typical case
Alkylation reaction technique still adopt horizontal agitated vessel reactor, and iso-butane and butene alkylation are typical Two Liquid Phases
Reaction, interphase mass transfer speed determine Global reaction Rate.In such reaction system, in the situation of biphase fully dispersed mixing
Under, alkene can be realized converting completely quickly, if the response time is long, initially form with high-octane trimethyl penta
Alkane (TMP) will continue to contact with highly acid catalyst, can cause TMP to the different of low-octane dimethylhexane (DMH)
Structure.Therefore, it is difficult to obtain high-octane product while high conversion is obtained using convention stir reactor.
Isoparaffin belongs to immiscible liquid-liquid two phase reaction with the alkylated reaction of alkene, and immiscible liquid-liquid is biphase to mix
Close effect and there is material impact to the conversion ratio and selectivity of liquid-liquid reactions.Current existing liquid-liquid two-phase mixtures reactor master
Stirred tank to be had, static mixer, impinging streams mixer and ejector mixing etc..
CN200520078557.3 discloses the horizontal reactor in a kind of sulfuric acid process alkylation process, and main body is one and crouches
Formula pressure vessel, the propeller having at an interior circulation sleeve, a shell and tube heat removing tube beam, an end socket.React into
Material and recycle acid enter the suction side of stirring paddle, and under the driving of stirring paddle, reaction mass spreads rapidly and forms emulsifying with acid
Liquid, emulsion ceaselessly high-speed circulating react in the reactor.In the discharge side of reactor, a part of emulsion is discharged
To acid settler, the separation of acid is carried out.Acid sinks to sedimentation pot bottom as proportion is larger, then returnes to the suction of stirring paddle
Side.Reactant mixed process is completed in whole horizontal reactor, and the bulk of mixing is whole reactor, and time appropriateness exists
20～30 minutes, belong to the category of micromixing.Back-mixing in this reactor is larger, is unfavorable for improving the selectivity of reaction.
US6194625B1 discloses a kind of alkylation reactor of sectional feeding, and reaction zone is divided into the section of several series connection, will be new
Fresh raw material is divided into several stocks not introduce each reaction section, and the sour hydrocarbon emulsion for recycling is then series flow, and each is anti-
Answer and mixed using churned mechanically mode in section.Although this structure overcomes the larger problem of back-mixing, but structure mistake
In complexity.In addition, both reactors all employ fixed Motor drive stirring paddle, it is easy to anti-raw because poorly sealed to let out
Leakage.
CN100348559C discloses one kind and ionic liquid-catalyzed isoparaffin and alkene is completed in hypergravity rotary apparatuss
The liquid-liquid phase alkylation reaction technique method of hydrocarbon.The rotary drill reactor device that the invention is provided includes：Reactor shell, shell
There are charge door and discharging opening on body, reactor shell is built with the RPB being made up of rotor, packing layer, wherein there is charging
Pipe, feed liquid shower nozzle, RPB are located at housing upper, and lower housing portion is fluid reservoir, and the heart is equipped with agitating device in the reactor,
The reaction mass of fluid reservoir can be stirred, fluid reservoir connects and composes revolving bed recirculation reactor with feed liquid circulating pump, be circulated
The suction tube porch of pump is connected with blender, is provided with alkane alkene feed liquid suction inlet and ionic liquid import on the mixer, after reaction
Part feed liquid and ionic liquid mix in blender, the discharging opening of circulating pump connects the feed pipe of RPB, circulating pump
Mixed feed liquid is delivered to RPB and is circulated reaction, liquid level control gage is housed on fluid reservoir, feed liquid is controlled
The time of staying.The reactor of this structure can strengthen the mixing between reactant and sour hydrocarbon emulsion, but structure is still excessively complicated, no
Easily expand the scale of production.
US3281213 proposes a kind of vertical alkylation reactor, and its main body is a riser, riser and one it is sleeping
Formula tank is connected, and horizontal tank participates in the nozzle of isoparaffin and alkene by lifting bottom of the tube of reaction built with sour hydrocarbon emulsion
Spray into, spray the gravitation that causes and drive the sour hydrocarbon emulsion in horizontal tank to enter riser together, reaction is i.e. in this root riser
Carry out in reactor.Riser top is connected with a knockout drum, for the separation of product.Sour hydrocarbon emulsion after separation is followed
Ring enters the horizontal tank for lifting bottom of the tube.This structure does not adopt mechanical transmission member, solves what built-in stirring blade brought
Series of problems.But, in riser, sour hydrocarbon emulsion is not satisfactory with the mixing of other reactants, in addition, whole anti-
Device system is answered to employ a riser, two horizontal tanks and a down-comer, equipment is huge, structure is also not compact enough.
The content of the invention
One of the technical problem to be solved in the present invention be to provide a kind of liquid acid alkylation reactor for isoparaffin with
The alkylated reaction of alkene.
The two of the technical problem to be solved in the present invention are to provide a kind of application process of liquid acid alkylation reactor.
A kind of liquid acid alkylation reactor that the present invention is provided, from top to bottom including mixed zone, reaction zone and liquid collecting zone,
Least one set injection stream blender is set in described mixed zone, and every group of injection stream blender is at least two same levels
Centrosymmetric ejector, the entrance of the described injection stream blender of described liquid collecting zone Jing circulating pump connections, described reaction
Area arranges gas outlet, and liquid product outlet is arranged under described gas outlet.
In the liquid acid alkylation reactor that the present invention is provided, the height of described mixed zone is the 10% of height for reactor
～20%, the height of described liquid collecting zone is the 10%～30% of height for reactor.
In the liquid acid alkylation reactor that the present invention is provided, it is preferable that conical flow guiding cylinder is set in described reaction zone.
Described conical flow guiding cylinder is arranged on the 40%～50% of height for reactor from the bottom to top, the height of described conical flow guiding cylinder
For the 5%～10% of height for reactor.
In the liquid acid alkylation reactor that the present invention is provided, one or more groups of injection streams are set in described mixed zone and are mixed
Clutch.Multigroup injection stream blender is preferably provided with, multigroup injection stream blender can be arranged with single or multiple lift, every group of injection stream is mixed
Clutch is centrosymmetric ejector at least two same levels, and wherein ejector is provided with centering with reactor wall junction
Adjusting means, to ensure that from different ejectors the mixed material for projecting can complete head-on collision in the same area；In course of reaction, can
Select one group of injection stream blender feeding manner, it is also possible to multigroup injection stream blender is selected while charging.
In the liquid acid alkylation reactor that the present invention is provided, it is preferable that described ejector at least two-way entrance, one
Road is feed(raw material)inlet, and another road is the circulating liquid acid entrance from described reactor liquid collecting zone.Wherein, described raw material enters
Mouthful fluid flow direction it is vertical with the flow direction of sprue interior circulation liquid acid in ejector and intersect.It is highly preferred that institute
The feed(raw material)inlet stated arranges nozzle, and alkylated reaction raw material Jing nozzles spray into ejector, and with ejector sprue in from following
There is strong immixture in the circulation fluid of ring liquid acid entrance, alkylated reaction raw material is with the mixed mixed material of liquid acid again
Sprayed by ejector, the material that two ejectors in one group of injection stream blender spray occurs to hit strongly in described mixed zone
Hit, make alkene that microcosmic admixture is reached in mixed material.
In the liquid acid alkylation reactor that the present invention is provided, two ejectors in one group of described injection stream blender
Outlet at a distance of 2.0mm-50mm, be preferably 5.0mm-20mm.
In the liquid acid alkylation reactor that the present invention is provided, reactor shell can be cylinder type (as shown in Figure 1),
Can also be square tubular, the present invention is not limited in this respect.Described liquefied alkyl reactor shell top and bottom can be adopted
With plate seal or end socket sealing structure, it is preferred to use end socket sealing structure, to clean inside reactor.
In the liquid acid alkylation reactor that the present invention is provided, described gas outlet reaction zone normally control liquid level with
On, it is arranged on the 35%～45% of height for reactor from the bottom to top.On the pipeline of the described gas outlet of connection, back pressure control is set
Pressure valve.Described liquid-phase reaction product outlet is arranged on reaction zone and normally controls below liquid level, in preferably normal control liquid level
Top, is arranged on the 15%～25% of height for reactor from the bottom to top.
In the liquid acid alkylation reactor that the present invention is provided, described circulating pump is acid corrosion-resistant type centrifugal pump.
In the liquid acid alkylation reactor that the present invention is provided, the material of described reactor shell is ordinary carbon steel.
In the liquid acid alkylation reactor that the present invention is provided, it is preferable that described reactor head arranges circulation cryogen
Entrance.
In the liquid acid alkylation reactor that the present invention is provided, described liquid collecting zone arranges recycle acid emulsion outlet, liquid collecting
Recycle acid emulsion outlet, circulating pump in area described in the yogurt liquid Jing of sedimentation enrichment returns described injection stream mixer entrance.
Wherein, described recycle acid emulsion outlet can arrange one or more.Preferably, described recycle acid emulsion outlet is arranged on
Liquid collecting zone bottom.Recycle acid emulsion pipeline can arrange one or more, can adopt a circulating pump or multiple circulating pumps, follow
Endless tube road and circulating pump are typically using a set of or two sets.Above-mentioned concrete structure and quantity can be according to reactor scale and materials
Matter, is determined by the design of this area general knowledge.
In the liquid acid alkylation reactor that the present invention is provided, described reactor bottom is provided with liquidometer, for checking
Liquid level in reactor.
A kind of liquid acid alkylation that the present invention is provided, using above-mentioned liquid acid alkylation reactor, by liquid
The entrance introducing ejector of acid catalyst and alkylated reaction raw material Jing injection stream blenders, two of one group of injection stream blender
There is strong shock mix homogeneously in the material that ejector sprays in mixed zone, mixed material enters reaction zone and liquid collecting
Area, and there is alkylated reaction, after settlement, the liquid collecting zone enriched liquid acid catalyst of reactor bottom, Jing are followed reaction mass
Return in injection stream blender after the supercharging of ring pump and reuse, the hydrocarbon of vaporization flows through gas outlet's discharge, product Jing
Liquid product outlet is discharged into piece-rate system.
In the method that the present invention is provided, described liquid acid catalyst is concentrated sulphuric acid, strong acidic ion liquid or contains dense
The mixed acid of sulphuric acid.Wherein, in the described mixed acid containing concentrated sulphuric acid, concentrated sulphuric acid content is 85wt%～98wt%, and remaining is
One or more in trifluoromethanesulfonic acid, phosphoric acid and formic acid.
In the method that the present invention is provided, described alkylated reaction raw material is the C containing iso-butane3～C5Olefine fraction, it is described
Alkylated reaction raw material in alkane alkene mol ratio be 5.0～15:1.0th, 6.0～12 are preferably:1.0th, more preferably 8.0～
10:1.0。
In the method that the present invention is provided, the operating condition of described liquid acid alkylation reactor is：Pressure be 0.05～
1.2MPa, preferably 0.1～0.3MPa；Temperature is -4～15 DEG C, preferably -3～7 DEG C.
In the method that the present invention is provided, it is preferable that the outlet of product Jing liquid product is discharged, into sour hydrocarbon knockout drum,
Jing after gravity settling separation, in the liquid acid catalyst Returning reactor of sour hydrocarbon knockout drum bottom, the hydrocarbon mixture isolated
Into next cleaning procedure.
In the method that the present invention is provided, the hydrocarbon of described vaporization flows through gas outlet's discharge, the vaporization alkane of discharge
Continue reaction Jing after compressor compression condensation in Returning reactor.
In the method that the present invention is provided, in alkylation reactor, exothermic heat of reaction takes thermal recovery isoparaffin spontaneous evaporation refrigeration side
Formula, discharges reactor at the top of the alkane Jing gas-liquid separations gas phase zone of vaporization, discharge, and control is anti-
Device pressure is answered in 0.05～1.2MPa, it is preferred to use 0.1～0.3MPa.The vaporization alkane of discharge is returned Jing after compressor compression condensation
Reactor is returned, circulation cryogen returns entrance and can be arranged on any position of reactor, it is preferred to use is arranged at the top of mixed zone and seals
Head middle position.
The purpose of generally majority alkylation is will be isoparaffin (or aromatic hydrocarbons) and light olefin tight with acidic catalyst
Contact, reaction generate alkylate.In petroleum refining industry, aliphatic hydrocarbon is well-known with the acid catalyzed alkyation of alkene
Method.Generally indication alkylation refers to isoparaffin and alkene under strong acid catalyst, and it is higher than raw material, boiling range to produce octane number such as
For the course of processing of gasoline-range fraction.Alkylation involved in the present invention is generally iso-butane and C3～C5Olefine fraction it is anti-
Should, it is particularly well-suited to the reaction of iso-butane and C 4 olefin.
Above-mentioned reactor is suitable for the mixed acid with concentrated sulphuric acid, strong acidic ion liquid and with concentrated sulphuric acid based on as catalyst
Liquid acid alkylation process, it is preferred to use concentration is 90%～99.2% concentrated sulphuric acid and the mixing based on concentrated sulphuric acid
Acid.
The liquid acid alkylation reactor and application process that the present invention is provided has the beneficial effect that：
Injection stream blender is set in the liquid acid alkylation reactor that the present invention is provided, is utilized in injection stream blender
Mixed intensified rapid dispersion of the alkene in sour hydrocarbon emulsion of injection, the fluid of preliminary mixing eject impingement mix once more,
The initial microcosmic mixed-level of liquid phase is improve, alkylated reaction speed macroscopically is accelerated, so as to improve reaction conversion ratio
And the selectivity of product, it is more suitable for plant-scale course of reaction.The liquid acid alkylation reactor that the present invention is provided
By the way of two-phase or multiphase injection mixing and reaction stream are directly clashed into and are combined, it is to avoid in stirred autoclave liquid and
The energy loss that wall clashes into, capacity usage ratio are high.In the liquid acid alkylation reactor that the present invention is provided, inner member is few, machinery
Simple structure, is easy to process, cleans, and equipment investment is low.The liquid acid alkylation reactor that the present invention is provided is all using quiet close
Envelope, it is to avoid rotary part weakens the shortcoming of sealing property in traditional stirred tank reactor, sealing property more preferably, is particularly well-suited to
The mixing of inflammable, explosive and corrosive materials and reaction.
The liquid acid alkylation reactor that the present invention is provided is particularly well-suited to sulphuric acid, ionic liquid and with sulphuric acid
Alkylated reaction of the main mixed acid for catalyst.
Description of the drawings
The liquid acid alkylation reactor structural representation that accompanying drawing 1 is provided for the present invention；
The liquid acid alkylation reactor A-A ' profiles that accompanying drawing 2 is provided for the present invention.
Wherein：1- reactor shells；2- liquid collecting zones；3- injection stream blenders；4- circulating pumps；5- gas outlets；6- liquid phases
Product exit；7- mixed zones；8- reaction zones；9- circulates cryogen entrance；10- recycle acids are exported；11- recycle acids unload outlet；12- is former
Material entrance；13- ejector guide shells；14- conical flow guiding cylinders.
Specific embodiment
The specific embodiment of the present invention is described in detail below in conjunction with accompanying drawing, but therefore the present invention is not subject to any limit
System.
The liquid acid alkylation reactor structural representation that accompanying drawing 1 is provided for the present invention, as shown in Figure 1, described liquid
Body acid alkylation reactor from top to bottom includes mixed zone 7, reaction zone 8 and liquid collecting zone 2, arranging at least in described mixed zone 7
One group of injection stream blender 3, every group of injection stream blender 3 are centrosymmetric ejector (ratio at least two same levels
Venturi type jet mixer can such as be adopted), it is to strengthen mixed effect, described ejector outlet is preferably provided with ejector and leads
Flow cartridge 13；Described 2 Jing circulating pumps 4 of liquid collecting zone connect the entrance of described jet mixer 3, and described reaction zone arranges gas
Outlet 5, arranges liquid product outlet 6 under described gas outlet 5.It is preferred that arranging conical flow guiding cylinder in described reaction zone 8
14。
A-A ' profile of the accompanying drawing 2 for liquid acid alkylation reactor, such as accompanying drawing 2 are visible, and every group of injection stream blender 3 is
Centrosymmetric ejector at least two same levels.
Diameter is identical to be distributed in the middle part of mixed zone with length identical injection stream blender is coaxial two-by-two, symmetrical, sprays
Stream blender can be arranged with multilamellar, and injection stream blender is provided with centering adjusting device with reactor wall junction, never to ensure
The mixed material projected with ejector can complete head-on collision in the same area.Described mixed zone top is ellipse end socket, is adopted
Bolt presses structure is used, to clean inside reactor ejector.Connection safety valve at ellipse end socket, thermocouple thermometer,
The adnexaes such as pressure gauge.It is preferred that circulation cryogen entrance 9, described circulation cryogen entrance are arranged at the top of liquid acid alkylation reactor
9 by reactor is entered at the top of ellipse end socket, to control temperature of reactor.Reaction zone barrel arranges gas outlet 5.In gas
Outlet bottom is provided with liquid product outlet 6.The bottom of the liquid collecting zone 2 of liquid acid alkylation reactor bottom is provided with liquidometer, uses
In checking liquid level in kettle.Liquid acid alkylation reactor bottommost is provided with recycle acid outlet 10 and is connected with circulating pump 4, and pump discharge is followed
Naphthenic acid hydrocarbon emulsion Jing pipelines return to the sprue of injection stream blender 3.
The liquid acid alkylation reaction method that the present invention is provided, using above-mentioned liquid acid alkylation reactor, by liquid
Acid catalyst and alkylated reaction raw material Jing circulating pumps squeeze into one group of injection stream blender sprue, the mixing of Jing injection streams blender
Reactor mixed zone 7 being entered afterwards, strong shock mix homogeneously occurring in mixed zone 7, mixed material enters reaction zone
8, and the liquid collecting zone 2 Jing after conical flow guiding cylinder water conservancy diversion into reactor bottom, beat again by Jing circulating pumps for the mixed material in liquid collecting zone 2
Enter injection stream blender, so circulation a period of time material mixing is complete；Another strand of alkane alkene ratio is 8：1 carbon 4 liquid gas reaction
Material is shouted cervical region and is provided with one group of 4 homodisperse aperture vertically into throat of injector cervical region, and alkene Jing apertures spray into ejector
There is strong immixture with recycle acid emulsion in sprue, the mixed material of ejection occurs to clash into strongly in head-on collision area again, makes alkene
Hydrocarbon reaches microcosmic admixture in mixed material and alkylated reaction occurs.Reacted material enters liquid collecting zone 2, vaporization
Hydrocarbon material flow (predominantly iso-butane) Jing gas outlets 5 discharge, and control reactor pressure is in 0.12MPa or so, gas phase iso-butane
9 Returning reactor of Jing circulation cryogens entrance Jing after compressor compression condensation；Alkylation liquid product Jing liquid products outlet 6 is entered
Into piece-rate system.It is preferred that alkylation liquid product is discharged into sour hydrocarbon knockout drum, Jing after gravity settling separation, the liquid of bottom
Reuse in yogurt liquid Returning reactor, the hydrocarbon mixture isolated enters next cleaning procedure.
As seen from the above technical solution provided by the invention, alkylation reactor proposed by the present invention is using multigroup right
The reacted material of setting of push-style jet mixer and sour hydrocarbon emulsion circulating pump is circulated reaction again, enhances alkene and is following
Initial microcosmic mixing dispersion effect in naphthenic acid hydrocarbon emulsion, suppresses the carrying out of alkylation side reaction, so as to the product after reaction is ensured
The circulating load into the iso-butane in material is reduced on the premise of with high-octane rating, the energy consumption of device is reduced, with very strong
Industrial applicibility.
The above, the only present invention preferably specific embodiment, but protection scope of the present invention is not limited thereto,
Any those familiar with the art in the technical scope of present disclosure, the change or replacement that can be readily occurred in,
Should all cover within the scope of the present invention.Therefore, protection scope of the present invention with scope of the claims should be
It is accurate.
The concrete structure and application effect of the liquid acid alkylation reactor of present invention offer are provided by embodiment below
Really, but the present invention is not therefore subject to any restriction.
Embodiment 1
The structure of liquid acid alkylation reactor as shown in Figure 1, wherein, reactor diameter is 2m, is highly 15m, mix
It is highly 2m to close area, 2 groups of injection stream blenders of setting in mixed zone, the position of gas outlet away from reactor bottom 5m, liquid
Away from reactor bottom 1.5m, the height of conical flow guiding cylinder is away from reactor bottom 6.5m for the position of phase product exit.
Reaction is alkylated using aforesaid liquid acid alkylation reactor, reaction raw materials are carbon 4 liquid gas, take from stone
Village oil-refining chemical limited company of family.Mass percent is consisted of：Propane 0.098%, iso-butane 39.36%, normal butane
13.51%, isobutene. 1.39%, 1-butylene 14.70%, maleic 14.92%, anti-butylene 16.0%, pentane 0.022%.With
Recycle isobutane is made into alkane alkene ratio for 8：1 reaction feed, concentrated sulphuric acid of the catalyst for concentration 98.5%, concentrated sulphuric acid and iso-butane
Jing circulating pumps squeeze into injection stream blender sprue, and carbon 4 liquid gas are shouted cervical region and are provided with 4 vertically into throat of injector cervical region
Even scattered aperture, carbon 4 liquid gas Jing apertures spray into ejector sprue, concentrated sulphuric acid and iso-butane Jing ejector mixings with
Enter in liquid acid alkylation reactor after carbon 4 liquid gas mixing, Jing circulating pumps squeeze into spray to the mixed emulsion of reactor bottom again
Jet mixer, so circulation a period of time mix complete；In the mixed zone on reactor top, it is mixed that injection stream blender sprays
There is strong shock in head-on collision area in compound material, make alkene that microcosmic admixture is reached in mixed material again.Reacted material
Into liquid collecting zone 2, the hydrocarbon of vaporization flows through gas outlet 5 and discharges reactor, controls reactor pressure in 0.12MPa or so,
Gas phase iso-butane 9 Returning reactor of Jing circulation cryogens entrance Jing after compressor compression condensation；The alkylation liquid product Jing of discharge
Liquid product outlet 6 enters sour hydrocarbon knockout drum, the concentrated sulphuric acid Returning reactor Jing after gravity settling separation, the hydro carbons mixing isolated
Thing enters next cleaning procedure, obtains alkylate oil, the alkylate oil for obtaining after distillation removing four component of most of carbon
Do as 190 DEG C, it is 94.1 that RON values are 96.4, MON values.
Embodiment 2
Reaction is alkylated using the liquid acid alkylation reactor in embodiment 1, reaction process and reaction raw materials are same
Embodiment 1, except that liquid acid catalyst is 99.5% highly acid AlCl3Type ionic liquid (AlCl3:(C2H5)3NHCl
=0.67) (Chinese Academy of Sciences's Lanzhou Chemical Physics institute production), reaction raw materials are carbon 4 liquid gas, originate and constitute same embodiment
1.Alkane alkene ratio is made into for 6 with iso-butane：1 reaction feed, reactor pressure are controlled to 0.25MPa, and temperature is：-3℃.Alkyl
Changing product and alkylate oil being obtained through most of four component of carbon of distillation removing, the alkylate oil for obtaining is done as 189 DEG C,
It is 93.9 that RON values are 96.2, MON values.
Claims (16)
1. a kind of liquid acid alkylation reaction method, it is characterised in that the reactor of employing from top to bottom includes mixed zone, reaction
Area and liquid collecting zone, arrange least one set injection stream blender in described mixed zone, every group of injection stream blender is at least two
Centrosymmetric ejector in same level, described liquid collecting zone Jing circulating pumps connect entering for described injection stream blender
Mouthful, described reaction zone arranges gas outlet, and liquid product outlet is arranged under described gas outlet；By liquid acid catalyst
Ejector, two ejector sprays of one group of injection stream blender are introduced with the entrance of alkylated reaction raw material Jing injection stream blenders
There is strong shock mix homogeneously in the material for going out in mixed zone, mixed material enters reaction zone and liquid collecting zone, concurrently
Raw alkylated reaction, after settlement, the liquid collecting zone enriched liquid acid catalyst of reactor bottom, Jing circulating pumps are pressurized reaction mass
Return in injection stream blender afterwards and reuse, the hydrocarbon of vaporization flows through gas outlet's discharge, product hydrocarbon mixture
The outlet of Jing liquid products is discharged into piece-rate system.
2. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that the height of described mixed zone is reaction
The 10%～20% of device height, the height of described liquid collecting zone is the 10%～30% of height for reactor.
3. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that described reaction zone arranges conical flow guiding
Cylinder.
4. according to the liquid acid alkylation reaction method of claim 3, it is characterised in that described conical flow guiding cylinder is arranged on
The 40%～50% of height for reactor from the bottom to top, the height of described conical flow guiding cylinder is the 5%～10% of height for reactor.
5. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that described ejector at least two-way enters
Mouthful, wherein be feed(raw material)inlet all the way, another road is circulating liquid acid entrance, the flow direction and ejector of described feed(raw material)inlet
Middle circulating liquid acid liquid flow path direction vertically and intersects.
6. according to the liquid acid alkylation reaction method of claim 5, it is characterised in that described feed(raw material)inlet arranges nozzle,
Reaction raw materials Jing nozzle Jing feed(raw material)inlets are sprayed in ejector, and with ejector sprue in following from circulating liquid acid entrance
Ring liquid acid mixes strongly.
7. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that in one group of described injection stream blender
The outlet of a pair of ejectors at a distance of 2.0mm-50mm.
8. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that described gas outlet is arranged on by under
The 35%～45% of supreme height for reactor, described liquid product outlet be arranged on height for reactor from the bottom to top 15%～
25%.
9. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that described circulating pump is acid corrosion-resistant type
Centrifugal pump.
10. according to the liquid acid alkylation reaction method of claim 1, it is characterised in that described reactor head is arranged and followed
Ring cryogen entrance.
11. according to any one in claim 1-10 liquid acid alkylation reaction method, it is characterised in that described liquid acid
Catalyst is concentrated sulphuric acid, strong acidic ion liquid or the mixed acid containing concentrated sulphuric acid.
12. according to claim 11 liquid acid alkylation reaction method, it is characterised in that the described mixed acid containing concentrated sulphuric acid
The content of middle concentrated sulphuric acid is 85wt%～98wt%, and remaining is one or more in trifluoromethanesulfonic acid, phosphoric acid and formic acid.
13. according to any one in claim 1-10 liquid acid alkylation reaction method, it is characterised in that described alkylation
Reaction raw materials are the C containing iso-butane3～C5Olefine fraction.
14. according to the claim 1-10 liquid acid alkylation reaction method of any one, it is characterised in that described liquid acid alkane
The operating condition of glycosylation reaction device is：Pressure is 0.05～1.2MPa；Temperature is -4～15 DEG C.
15. according to any one in claim 1-10 liquid acid alkylation reaction method, it is characterised in that product hydro carbons
The outlet of mixture Jing liquid products is discharged into sour hydrocarbon knockout drum, and Jing after settlement separate, the liquid acid of sour hydrocarbon knockout drum bottom is urged
In agent Returning reactor, the hydrocarbon mixture isolated enters next cleaning procedure.
16. according to any one in claim 1-10 liquid acid alkylation reaction method, it is characterised in that described vaporization
Hydrocarbon flows through gas outlet's discharge, and the vaporization alkane of discharge continues reaction Jing after compressor compression condensation in Returning reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410342373.7A CN105251433B (en) | 2014-07-17 | 2014-07-17 | A kind of liquid acid alkylation reactor and its application process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410342373.7A CN105251433B (en) | 2014-07-17 | 2014-07-17 | A kind of liquid acid alkylation reactor and its application process |
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| Publication Number | Publication Date |
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| CN105251433A CN105251433A (en) | 2016-01-20 |
| CN105251433B true CN105251433B (en) | 2017-03-29 |
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| CN107974280B (en) * | 2016-10-25 | 2020-05-19 | 中国石油化工股份有限公司 | Liquid acid alkylation reaction method |
| CN108325493A (en) * | 2018-03-28 | 2018-07-27 | 中国矿业大学 | A kind of granular medicine action system and method based on strong turbulence cycle |
| CN108283996B (en) * | 2018-03-28 | 2024-04-30 | 中国矿业大学 | Multiphase mixing mineralizing device and mixing method |
| CN108273668B (en) * | 2018-03-28 | 2024-03-01 | 中国矿业大学 | Rapid flotation system and flotation method based on high-turbulence mixed mineralization |
| CN108246515B (en) * | 2018-03-28 | 2024-03-01 | 中国矿业大学 | Pulping and flotation integrated system with internal circulation function and pulping and flotation method |
| CN114432976B (en) * | 2020-10-31 | 2023-11-07 | 中国石油化工股份有限公司 | Alkylated gasoline production device and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6194625B1 (en) * | 1994-09-30 | 2001-02-27 | Stratco, Inc. | Alkylation by controlling olefin ratios |
| CN2790575Y (en) * | 2005-03-24 | 2006-06-28 | 兰州炼油化工设计院 | Horizontal allkylation reactor |
| CN203329731U (en) * | 2013-02-06 | 2013-12-11 | 武汉工程大学 | Vertical impinging stream reactor |
| CN103611487A (en) * | 2013-12-18 | 2014-03-05 | 华东理工大学 | Impinging stream reactor |
-
2014
- 2014-07-17 CN CN201410342373.7A patent/CN105251433B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6194625B1 (en) * | 1994-09-30 | 2001-02-27 | Stratco, Inc. | Alkylation by controlling olefin ratios |
| CN2790575Y (en) * | 2005-03-24 | 2006-06-28 | 兰州炼油化工设计院 | Horizontal allkylation reactor |
| CN203329731U (en) * | 2013-02-06 | 2013-12-11 | 武汉工程大学 | Vertical impinging stream reactor |
| CN103611487A (en) * | 2013-12-18 | 2014-03-05 | 华东理工大学 | Impinging stream reactor |
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