CN102510849B - Method for revamping HF or sulphuric acid alkylation unit - Google Patents
Method for revamping HF or sulphuric acid alkylation unit Download PDFInfo
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Abstract
The present invention provides a method for revamping an HF or sulphuric acid alkylation unit to an ionic liquid alkylation unit, wherein the HF or sulphuric acid alkylation unit comprise at least: -a reactor unit for contacting catalyst and hydrocarbon reactants; -a separator unit for separating a reactor effluent into a catalyst phase and an alkylate-comprising hydrocarbon phase; -a fractionator unit for fractionating the alkylate- comprising hydrocarbon phase into at least one stream comprising alkylate; and which method includes: -providing one or more cyclone units downstream of the reactor unit to separate at least part of the reactor effluent in a catalyst phase and a alkylate-comprising hydrocarbon phase.
Description
The invention provides the method for transformation HF or sulfuric acid alkylation unit.
Demand to alkylate oil fuel mediation raw material constantly increases.The alkylate oil of harmonic component of acting as a fuel also has low-steam pressure and containing alkene or aromatic essence when having high-octane rating character.
Nearly all alkylate oil is all by making isobutane and butene react and make under applicable an acidic catalyst exists.Using maximum catalyzer is HF (hydrofluoric acid) and sulfuric acid.Although very ripe, these methods still have many shortcomings.For HF, must take strict healthy measure and security measures, this needs a large amount of investments.For sulfuric acid, from economics point, a large amount of consumption of catalyzer and need to provide cooling be disadvantageous with equipment.
Recently, as substituting of HF and the acid catalysed alkylation process of sulphur, with ionic-liquid catalyst, with alkene, come the alkylation isoparaffin to cause concern.
In US7285698 for example, a kind of method of manufacturing alkylate oil is disclosed, the method makes the isobutane and butene reaction with compound ion liquid catalyst.In the method for US7285698, Trimethylmethane and butylene are supplied in reactor unit, and by making reactant contact to form alkylate oil with compound ion liquid under alkylation conditions.Reactor effluent is separated into to hydrocarbon phase and ionic liquid phase.Ionic liquid is recycled in reactor unit mutually, processes hydrocarbon phase simultaneously and obtain alkylate oil.
Current alkylation be always for the HF catalyzer or sulfuric acid (also being called SA) catalyzer custom-designed, the other catalyzer of very not applicable use, for example ionic liquid (also being called IL) catalyzer.Such as (Z.Liu such as Liu, R.Zhang, CXu, R.Xia, Ionic liquid alkylation process produces high-quality gasoline, Oil and Gas Journal, the 104th volume, the 40th phase, 2006) in mention, in order to use the IL catalyzer, can be retrofited in the sulfuric acid alkylation unit.Propose to increase for the compensator of recirculation IL in Liu etc. and revise the separation that IL is strengthened in settling vessel inside.Yet, the Liu discovery, it is best that the performance of the alkylation after remodeling does not reach.
Therefore, in this area, need to transform HF or SA alkylation as IL alkylation improve one's methods.
Have now found that, by revising existing alkylation, can rise to the performance of transformed HF or SA alkylation as the IL alkylation.
It has also been found that, Liu etc. report does not reach best result, be at least partly in separator unit (being the settling vessel unit) the incomplete separation of hydrocarbon phase and catalyzer phase cause.
Because the IL catalyzer is compared and had different character from SA or HF, by IL catalyzer and hydrocarbon phase separation be different by SA or HF and hydrocarbon phase separation.So the settling vessel design of HF or SA alkylation can not provide enough separating powers to separate hydrocarbon phase and catalyzer phase.Result is, catalyzer still is retained in hydrocarbon phase, and vice versa.So catalyst consumption increases, also catalyzed dose of pollution of hydrocarbon phase in addition.In addition, because of the higher isoparaffin that adopts in the IL alkylation process and the mol ratio of alkene, the hydrocarbon recirculation volume can increase.In common HF and SA alkylation process, the isoparaffin adopted and the mol ratio of alkene are 1～10.For the IL alkylation process, the isoparaffin adopted and the mol ratio of alkene are preferably greater than 20 or even be greater than 100.
Therefore, the present invention also provides the method that HF or sulfuric acid alkylation unit is transformed into to the ionic liquid alkylation, and wherein, described HF or sulfuric acid alkylation unit at least comprise:
-reactor unit, described reactor unit is for making catalyzer contact with the hydrocarbon reaction thing;
-separator unit, the hydrocarbon phase of described separator unit for reactor effluent is separated into to the catalyzer phase and comprises alkylate oil;
-fractionator unit, it is at least one logistics that comprises alkylate oil by the described hydrocarbon phase fractionation that comprises alkylate oil that described fractionator unit is used for;
Described method comprises:
-one or more swirlers unit is set in the downstream of reactor unit at least a portion reactor effluent is separated into to catalyzer phase and the hydrocarbon phase that comprises alkylate oil.
The present invention relates to HF or SA alkylation are transform as the method for IL alkylation.Transformation as herein described refers to, the existing unit or the processing unit that design are used for moving to special process are modified or change, thereby make it be applicable to other techniques of operation.Use the IL alkylation obtained, react under alkylation conditions under the IL catalyzer exists with alkene by making isoparaffin, produce alkylate oil.Common IL alkylation conditions (or processing condition) is well known in the art, and therefore should be appreciated that, actual operation process condition especially depends on the definite composition of reactant and catalyzer.
Temperature in reactor unit is preferably-20 ℃～100 ℃, more preferably 0～50 ℃, but temperature must height to being enough to guarantee that ionic liquid is its liquid form.
To form steam in order being suppressed in reactor, carry out said process under pressure, the pressure in reactor is preferably 0.1MPa～1.6MPa.
Alkylation process can be semi-continuous process or successive processes.Usually, isoparaffin is Trimethylmethane or iso-pentane, and alkene is to contain 2～8 carbon atoms, more preferably 3～6 carbon atoms, the further preferred alkene of 4 or 5 carbon atoms.The example of applicable alkene comprises propylene, 1-butylene, 2-butylene, iso-butylene, 1-amylene, 2-amylene, 2-methyl-1-butene alkene, 3-methyl-1-butene, 2-methyl-2-butene.
In the IL alkylation process, fresh isoparaffin and alkene are fed in this process with certain mol ratio, wherein said mol ratio is preferably more than 1, is generally 1: 1 to 40: 1, more preferably 1: 1 to 20: 1.For the situation of successive reaction, by the logistics recirculation that one or more are contained to isoparaffin, excessive isoparaffin can be recycled in reactor unit.
Downstream hereinafter described refers to the direction of the fluid flow path from reactor unit to the fractionator unit.Upstream hereinafter described refers to contrary direction, from the fractionator unit to reactor unit.
Existing HF at least comprises the reactor unit for reactant is contacted with catalyzer with the SA alkylation.Reactor unit preferably comprises at least one reaction-ure inlet and the outlet of at least one reactor effluent.Preferably, reactor unit also comprises at least one catalyst inlet.The common reactant device unit be arranged in the sulfuric acid alkylation unit is so-called Stratco contactor.In Stratco contactor for example, the hydrocarbon reaction thing is imported in U-shaped reactor fluid flowing-path together with catalyzer.For the HF alkylation, common reactor comprises for example Stratco contactor, gravity recirculation reactor and emulsion reactor.
Usually, cooling tube is set in the reactor fluid flowing-path and removes the heat that the alkylated reaction of heat release produces.As another selection, to sour recirculation stream, implement cooling.The effluent of reactor unit is the mixture of catalyzer and hydrocarbon phase, and the latter comprises alkylate oil and unreacted reactant (being mainly isoparaffin).
Usually the effluent of reactor unit is supplied to separator unit, thus the hydrocarbon phase that reactor effluent is separated into to the catalyzer phase and comprises alkylate oil.Preferably, separator unit comprises at least one import (described import be generally used for reactor effluent or by the logistics of its generation) and at least one catalyzer exports mutually and at least one outlet containing the hydrocarbon phase of alkylate oil.
The effect of separator unit is the hydrocarbon phase that the effluent of reactor unit is separated into to the catalyzer phase and comprises alkylate oil.Preferably, in the HF transformed and SA alkylation, separator unit used is the settling vessel unit.Due to HF and the SA catalyzer lower to the avidity of hydrocarbon, these two are easily separated under action of gravity.Settling vessel as herein described unit refers to any separator unit that makes two kinds of liquid phases separate under action of gravity.In fact, the density of HF, SA and IL catalyzer is all higher than the density of hydrocarbon phase, thus the hydrocarbon phase of reactor effluent above usually being separated in settling vessel and below the catalyzer phase.
For the alkylating situation of SA, catalyzer phase recirculation unit is set the SA catalyzer is recycled to reactor unit from the settling vessel unit.Usually, in order to keep catalyst activity, part SA catalyzer is removed from technique as the catalyzer consumed, and add fresh SA catalyzer make levels of catalysts and activity keeping constant.
For the alkylating situation of HF, make the HF catalyst regeneration and it is recycled in process for reusing.Therefore, the HF alkylation comprises catalyzer phase recirculation unit and carrys out recirculation HF catalyzer, and combines with independent regenerative process.
In SA and HF alkylation, the hydrocarbon phase that contains alkylate oil obtained in settling vessel is provided to the fractionator unit at least in part, obtains alkylate oil.The fractionator unit preferably comprises at least one import containing the hydrocarbon phase of alkylate oil.The fractionator unit comprises one or more distillation subelements usually, for example comprises that main fractionator (also be called in the art isomer carry heat up in a steamer tower (iso-stripper)), acid carries and heat up in a steamer tower and/or depropanizing tower.
After fractionation, obtained alkylate oil can be used for prepare aviation spirit or as the gasoline harmonic component.Hydrocarbon phase also may comprise the unreacted isoparaffin of significant quantity.Preferably, it is provided for isoparaffin is recycled to the device of reactor from the fractionator unit to pass through, and at least a portion of this isoparaffin is recycled to reactor unit.By hydrocarbon phase is carried out to fractionation, can also obtain other hydrocarbon streams, for example contain the logistics of n-paraffin.
In existing HF or SA alkylation, setting device is so that reactant and catalyzer enter reactor, and the hydrocarbon phase that reactor effluent is supplied to separator unit and will contains subsequently alkylate oil is supplied to the fractionator unit.Will directly not be sent to separator unit from reactor unit by reactor effluent.Can carry out intermediate treatment to reactor effluent, for example in heat exchanger, carry out cooling or heating.This is equally applicable to just be provided to the hydrocarbon phase that contains alkylate oil of fractionator unit.Usually, by arranging the device of reactant and catalyzer importing reactor unit, produce the fluid flow path of reactant, product and catalyzer.In addition, setting device is the reactor effluent import from the reactor effluent export supply of reactor unit to separator unit by reactor effluent, and wherein said separator unit is positioned at the reactor unit downstream in fluid flow path.In addition, setting device is the import from the export supply of the hydrocarbon phase containing alkylate oil of separator unit to the hydrocarbon phase containing alkylate oil of fractionator unit by the hydrocarbon phase that contains alkylate oil, and wherein said fractionator unit is positioned at the separator unit downstream in fluid flow path; Catalyzer phase recirculation unit is set catalyzer is recycled to reactor unit from the settling vessel unit.
Ionic liquid is known because of the ability of its catalytic alkylation reaction in the art.In the present invention, catalyzer used is to contain cationic compound ion liquid, and described cationic source is from the halogen acid salt of the amine, imidazoles or the pyridine that contain alkyl.Preferably, described positively charged ion comprises by four nitrogen-atoms that substituting group is saturated, and at least one hydrogen atom and an alkyl are arranged in these substituting groups.More preferably, alkyl substituent is at least one being selected from methyl, ethyl, propyl group, butyl, amyl group and hexyl.The cationic example be applicable to comprises triethyl ammonium (NEt
3h
+) and methyl diethyl ammonium positively charged ion (MeNEt
2h
+) or
The negatively charged ion of compound ion liquid is preferably aluminium class Lewis acid, particularly aluminium halogenide, preferably aluminum chloride (III).Due to the lewis acidic peracidity of aluminum chloride, preferably aluminum chloride or other aluminium halogenides and the second or more kinds of metal halide, vitriol or nitrate are combined to form coordination anion, particularly be derived from the coordination anion of two or more metal halides, wherein at least one metal halide is aluminium halogenide.Other metal halides, vitriol or the nitrate be applicable to can be selected from halogenide, vitriol or the nitrate of following metal, the group that described metal selects IB family element, the IIB family element in periodictable and the transition element in periodictable in free periodictable to form.The example of applicable metal comprises copper, iron, zinc, nickel, cobalt, molybdenum or platinum.Preferably, described metal halide, vitriol or nitrate are metal halides, more preferably metal chloride or bromide, for example cuprous chloride (I), cupric chloride (II), nickelous chloride (II), iron protochloride (II).Preferably, the mol ratio of aluminum compound and other metallic compounds is 1: 100 to 100: 1, more preferably 1: 1 to 100: 1, and more preferably 2: 1 to 30: 1.The coordination anion that comprises aluminium and other metals by use, can obtain improved alkylate oil product.For example in US7285698, a kind of method for preparing this type of catalyzer is being described.Particularly preferred catalyzer is to contain to be derived from aluminum chloride (III) and cupric chloride (II) or to be derived from aluminum chloride (III) and the acidic ionic liquid catalysts of the coordination anion of cuprous chloride (I).
In the method for the invention, swirler is set and carrys out the separate reactor effluent.In current HF or SA alkylation, be provided with the settling vessel unit and isolate HF or SA catalyzer and hydrocarbon phase from reactor effluent.After HF or SA alkylation are transformed into to the IL alkylation, the existing settling vessel that is used for HF or SA are separated with hydrocarbon by former the design separates IL catalyzer and the hydrocarbon phase that comprises alkylate oil from reactor effluent, may produce some ill effects, comprise:
-Yin the recirculation volume of hydrocarbon more due to, need larger settling vessel volume and a large amount of undesirable liquefaction light hydrocarbons arranged;
-catalyzer is brought to the hydrocarbon processing equipment in downstream;
-the hydrocarbon phase that comprises alkylate oil is polluted, thereby produces substandard product;
-form hydrocarbon-catalyst emulsion in settling vessel, thus control and brought operation problem for the settling vessel level;
-comprise more containing due to the hydrocarbon phase of alkylate oil of vast scale in catalyzer, aspect the validity of fund cost (larger equipment) and catalyst activity recovery, the validity that catalyzer restores regeneration descends.
Therefore, in the method for the invention, the HF transformed or SA alkylation preferably comprise the settling vessel unit as separator unit.In the method for the invention, in the reactor unit downstream, be provided with the swirler unit, and be provided with at least a portion reactor unit effluent is supplied to the device of swirler unit, thereby add separating of powerful catalyst and hydrocarbon phase.By using the swirler unit, reactor effluent can be separated into the effluent that the density that mainly comprises the hydrocarbon phase that contains alkylate oil is lower and mainly comprising the higher effluent of density of acidic ionic liquid catalysts phase.The swirler unit can comprise the swirler subelement of one or more series connection.Preferably, the swirler unit comprises one or more hydrocyclones.Hydrocyclone as herein described refers to and is designed for the swirler that makes water-hydrocarbon mixture phase-splitting.More preferably, swirler or hydrocyclone that the swirler unit comprises series connection more than two, wherein, the hydrocarbon phase that take in first (waterpower) swirler contains alkylate oil is that main low density outflow thing is provided to the next one (waterpower) swirler.This makes obtain further reinforcement separating between IL catalyzer phase and hydrocarbon phase.Preferably, described one or more swirlers unit additionally is set to existing settling vessel unit.Preferably, described one or more swirlers unit is arranged on to upstream, settling vessel unit, and setting device as flowing out thing, main low density is sent to settling vessel unit from the swirler unit by the hydrocarbon phase of take containing alkylate oil.By one or more swirlers and the one or more settling vessels that are positioned at this at least one swirler downstream are combined, to take containing the hydrocarbon phase of alkylate oil, be that main low density flows out thing and carries out further physical separation processes, can further be reduced in the hydrocarbon phase of take containing alkylate oil is that main low density flows out the ionic liquid ratio in thing.Although comparing the volume of settling vessel unit with for example swirler may be relatively large, if but use the settling vessel unit in downstream, swirler unit, the present invention still has advantage, and this is because this settling vessel unit will be more much smaller than being used for the settling vessel unit of separate reactor effluent in common process.
The higher effluent of density that mainly comprises the swirler unit of catalyzer phase can be recycled to reactor unit, optionally, after itself and the catalyzer phase (if any) obtained are merged, carry out again recirculation in the settling vessel unit.Optionally, can be arranged in parallel two above swirler unit with the increase capacity.These swirler unit in parallel can combine with series system with one or more settling vessels.
In Fig. 1, the hydrocarbon mixture that comprises alkene and isoparaffin for example, is supplied to reactor unit 100 (for example Stratco contactor) via conduit (, pipeline) 105, process reaction-ure inlet 107.Catalyst S A or IL also are provided to reactor unit 100 through conduit 110 and catalyst inlet 113.In reactor unit 100, hydrocarbon mixture contacts under alkylation conditions with catalyzer.Export 114 by reactor effluent, the reactor effluent that will comprise catalyzer and hydrocarbon takes out and is supplied to settling vessel unit 120 via conduit 115, process reactor effluent import 122 from reactor unit 100.In settling vessel unit 120, the catalyzer phase is separated under action of gravity with the hydrocarbon phase containing alkylate oil.Via containing the outlet 123 of the hydrocarbon phase of alkylate oil, hydrocarbon phase being taken out from separator unit 120, and by conduit 130 with containing the hydrocarbon phase import 133 of alkylate oil, it is supplied to fractionator unit 125.From the bottom of fractionator unit 125, by conduit 135, obtain the product that contains alkylate oil.This alkylate oil product can be for for example fuel mediation purposes.In addition, from the fractionator unit, 125 obtain iso-paraffinic products, via conduit 140, its recirculation are become to the part of the hydrocarbon mixture in conduit 105.Can also obtain from fractionator 125 the logistics (not shown) that other contain hydrocarbon.
Export mutually 143 by catalyzer catalyzer is taken out from separator unit 120, and can be recirculated to reactor unit 100 via catalyzer phase recycling pipe 145.Via conduit 150, the catalyst member consumed can be taken out from this process.Other live catalyst can be supplied to reactor unit 100 via conduit 155.
In Fig. 2 A, provided the schematic representation figure that uses the described SA alkylation of the transformed Fig. 1 of method of the present invention, wherein, be provided with the swirler unit between reactor unit and separator unit.In Fig. 2 A, via conduit 115, reactor effluent is supplied to swirler unit 505.Via conduit 510, in the future the hydrocarbon of take containing alkylate oil of spin current device unit be main density lower be supplied to mutually settling vessel unit 120.Via conduit 515, the catalyzer of take be main density higher be supplied to mutually catalyst recycle conduit 145.Provided the more detailed depiction of feasible swirler unit 505 in Fig. 2 B, wherein, reactor effluent enters the first swirler subelement 550 in swirler unit 505 via conduit 115.What density was lower leaves the first swirler subelement 550 via conduit 555, and be provided to the second swirler subelement 560 with further by the catalyzer phase with containing the hydrocarbon phase separation of alkylate oil.The hydrocarbon phase containing alkylate oil that density is lower leaves the second swirler subelement 560 via conduit 565, and is provided to settling vessel unit 120.Via conduit 570 and conduit 575, obtained the higher catalyzer phase of density from the first swirler subelement 550 and the second swirler subelement 560, and this catalyzer can be supplied to catalyst recycle conduit 145 mutually respectively.
Although what Fig. 1 and Fig. 2 related to is the SA alkylation, should be appreciated that, same figure can be used for describing the HF alkylation.
Embodiment
Illustrate the present invention by following non-limiting example.
Embodiment 1
In order to show the validity of carrying out the separate reactor effluent with swirler rather than conventional settling vessel, use swirler to be separated with the reactor effluent sample of the mixture of ionic-liquid catalyst with product comprising the hydrocarbon reaction thing.
Hydrocarbon and ionic-liquid catalyst that the reactor effluent sample packages is 1: 1.05 containing volume ratio.
Make operating temperature remain on 30 ℃～50 ℃, and make operating pressure remain on 0.1MPa～0.5MPa.The maximum feed rate that the reactor effluent sample enters in swirler is 2m
3/ hour.
In test for the first time, the reactor effluent sample of 40 volume % is main lower the obtaining mutually of density as the hydrocarbon of take containing alkylate oil.
The reactor effluent sample of remaining 60 volume % is as take catalyzer as main higher the obtaining mutually of density.
Based on the described volume that to take containing the hydrocarbon of alkylate oil be the phase that main density is lower, described hydrocarbon of take containing alkylate oil is main lower the comprising mutually of density:
The hydrocarbon of-95.5 volume %; With
The ionic liquid of-4.5 volume %.
Take catalyzer and be the volume of the phase that main density is higher based on described, describedly take catalyzer as main higher the comprising mutually of density:
The hydrocarbon of-17.7 volume %; With
The ionic liquid of-82.3 volume %.
By using a separator, take containing the hydrocarbon of alkylate oil be main density lower mutually in, that has reclaimed about 79 volume % is provided at the hydrocarbon in the reactor effluent sample at first.
Further processing the hydrocarbon of take containing alkylate oil in the settling vessel unit in downstream is the main lower phase time of density, and the volume size of this settling vessel unit is only 40% of the settling vessel unit that is used for separating the total reactor effluent.
In test for the second time, use two separating steps that the reactor effluent sample separation is the phase that main density is lower and take catalyzer as the main higher phase of density containing the hydrocarbon of alkylate oil for take.The separating resulting obtained is as follows.
The charging that enters whizzer of 50 volume % (the being the reactor effluent sample) centre lower as density obtained mutually; The ionic liquid phase effluent that remaining 50 volume % are higher as density is obtained.
Volume based on phase in the middle of described, described centre comprises mutually:
The hydrocarbon of-98.3 volume %; With
The ionic liquid of-6.2 volume %.
Take catalyzer and be the volume of the phase that main density is higher based on described, describedly take catalyzer as main higher the comprising mutually of density:
The hydrocarbon of-90.0 volume %; With
The ionic liquid of-10.0 volume %.
Obtain as intermediate product in the middle of obtaining, and it is carried out to second swirler separating step.In second swirler separating step process, obtain the middle hydrocarbon phase effluent lower as density of 85 volume % from swirler, remain the middle of 15 volume % and obtain as the higher phase effluent of density (also being called other effluents).
Volume based on to take containing the hydrocarbon of alkylate oil be the phase that main density is lower, described hydrocarbon of take containing alkylate oil is main lower the comprising mutually of density:
The hydrocarbon of-98.5 volume %; With
The ionic liquid of-1.5 volume %.
Volume based on described other effluents, described other effluents comprise:
The hydrocarbon of-68.7 volume %; With
The ionic liquid of-31.3 volume %.
By using two separators, take containing the hydrocarbon of alkylate oil be main density lower mutually in, that has reclaimed about 86 volume % is provided at the hydrocarbon in the reactor effluent sample at first.
It is the lower phase of density of leading that separator by using two series connection (being swirler in the case) separates the hydrocarbon of take containing alkylate oil from the reactor effluent sample, can obtain the hydrocarbon in the reactor effluent sample of vast scale more and it is transported to fractionator.This is because obtained the reactor effluent of vast scale more as middle phase from the first separator.Although will be more the reactor effluent sample of vast scale become lighter centre and meet and cause the increase of this heterogeneous effluent intermediate ion liquid fraction, but due to second separator step being arranged, resulting take containing the hydrocarbon of alkylate oil be main density lower mutually in final ionic liquid ratio much lower.So, the hydrocarbon in the reactor effluent of vast scale more can be separated with ionic liquid.In the situation that only use a separator, the hydrocarbon of take containing alkylate oil be main density lower comprise mutually 79 volume % only be present at first hydrocarbon in reactor effluent.Yet, in embodiment 1b, in the hydrocarbon effluent that comprises ionic liquid still less, obtained the hydrocarbon in the reactor effluent of 86 volume %.
In addition, with the situation of only using a separator, compare, the catalyzer of take be main density higher comprise mutually hydrocarbon still less, even in the situation that be also like this by its and other effluent merging.
In the settling vessel unit in downstream to take containing the hydrocarbon of alkylate oil be main density lower do mutually further processings the time, the volume size of this settling vessel unit be only be used for separating the total reactor effluent the settling vessel unit 42.5%.
Claims (6)
1. a method that HF or sulfuric acid alkylation unit is transform as to the ionic liquid alkylation, wherein, described HF or sulfuric acid alkylation unit at least comprise:
-reactor unit, described reactor unit is for making catalyzer contact with the hydrocarbon reaction thing;
-separator unit, the hydrocarbon phase of described separator unit for reactor effluent is separated into to the catalyzer phase and comprises alkylate oil;
-fractionator unit, it is at least one logistics that comprises alkylate oil by the described hydrocarbon phase fractionation that comprises alkylate oil that described fractionator unit is used for; And
Described method comprises:
-one or more swirlers unit is set in the downstream of described reactor unit the described reactor effluent of at least a portion is separated into to catalyzer phase and the hydrocarbon phase that comprises alkylate oil.
2. the method for claim 1, wherein described one or more swirlers unit is positioned at the upstream of described separator unit.
3. the method for claim 1, wherein described separator unit is substituted by described one or more swirlers unit.
4. method as described as any one in claim 1～3, wherein, the swirler subelement that the swirler unit comprises one or more series connection.
5. method as described as any one in claim 1～3, wherein, described swirler unit comprises one or more hydrocyclones.
6. method as claimed in claim 4, wherein, described swirler unit comprises one or more hydrocyclones.
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| GB647155A (en) * | 1941-04-24 | 1950-12-06 | Standard Oil Co | Improvements in or relating to a process of synthesizing hydrocarbons |
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