CN102510849A - Method for revamping an HF or sulphuric acid alkylation unit - Google Patents
Method for revamping an 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 present invention provides HF or the unitary method of sulfuric acid alkylation transformed.
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 does not contain alkene or aromatic essence when having high-octane rating character.
Nearly all alkylate oil all is to make through Trimethylmethane and butylene are reacted in the presence of an acidic catalyst that is fit to.Using maximum catalyzer is HF (hydrofluoric acid) and sulfuric acid.Though 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, say that from economics point the mass consumption of catalyzer is disadvantageous with cooling need be provided with equipment.
Recently, as HF and sulfuric acid the substituting of catalytic alkylation process, use ionic-liquid catalyst to come the alkylation isoparaffin to cause concern with alkene.
In US7285698 for example, a kind of method of making alkylate oil is disclosed, this method uses compound ion liquid catalyst to make Trimethylmethane and butene reaction.In the method for US7285698, Trimethylmethane and butylene are supplied in the reactor unit, and form alkylate oil through reactant is contacted under alkylation conditions with compound ion liquid.Reactor effluent is separated into hydrocarbon phase and ionic liquid mutually.Ionic liquid is recycled in the reactor unit mutually, handles hydrocarbon phase simultaneously and obtain alkylate oil.
Present alkylation is custom-designed for HF catalyzer or sulfuric acid (also being called SA) catalyzer always, very is not fit to use other catalyzer, for example ionic liquid (also being called IL) catalyzer.At (Z.Liu, R.Zhang, CXu such as for example Liu; R.Xia, Ionic liquid alkylation process produces high-quality gasoline, Oil and Gas Journal; The 104th the volume, the 40th phase, 2006) in mention; In order to use the IL catalyzer, can be retrofited in the sulfuric acid alkylation unit.In Liu etc., propose to increase to be used for the compensator of recycling IL and to revise the separation that IL is strengthened in settling vessel inside.Yet Liu finds that it is best that the performance of the alkylation behind the remodeling does not reach.
Therefore, need transform HF or SA alkylation as IL alkylation improve one's methods in this area.
Have now found that,, can rise to the performance of transformed HF or SA alkylation as the IL alkylation through revising existing alkylation.
Find that also Liu etc. reported does not reach optimal results, part is to cause incomplete separation by hydrocarbon phase in the separator unit (being the settling vessel unit) and catalyzer phase at least.
Because the IL catalyzer is compared with SA or HF and had different character, be different with IL catalyzer and hydrocarbon phase separation with SA or HF and hydrocarbon phase separation.So the design of the settling vessel of HF or SA alkylation can not provide enough separating powers to separate hydrocarbon phase and catalyzer mutually.The result is, catalyzer still is retained in the hydrocarbon phase, and vice versa.So catalyst consumption increases, hydrocarbon phase is also by catalyst contamination in addition.In addition, because of the higher isoparaffin that adopted 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 that is adopted and the mol ratio of alkene are 1～10.For the IL alkylation process, the isoparaffin that is adopted and the mol ratio of alkene are preferably greater than 20 or even greater than 100.
Therefore, the present invention also provides the method that HF or sulfuric acid alkylation unit is transformed into the ionic liquid alkylation, and wherein, said HF or sulfuric acid alkylation unit comprise at least:
-reactor unit, said reactor unit are used to make catalyzer to contact with the hydrocarbon reaction thing;
-separator unit, said separator unit are used for reactor effluent is separated into catalyzer phase and the hydrocarbon phase that comprises alkylate oil;
It is at least a logistics that comprises alkylate oil that-fractionator unit, said fractionator unit are used for the said hydrocarbon phase fractionation that comprises alkylate oil;
Said method comprises:
-one or more swirler-s unit is set in the downstream of reactor unit at least a portion reactor effluent is separated into 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 is meant, existing unit or the processing unit that design is used for moving special process made amendment or changed, thereby makes it be fit to other technologies of operation.Use the IL alkylation that is obtained,, produce alkylate oil through making isoparaffin and alkene in reaction under alkylation conditions in the presence of the IL catalyzer.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 the 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 the reactor drum in order being suppressed at, under pressure, to carry out said process, the pressure in the reactor drum 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 alkene of preferred 4 or 5 carbon atoms.The instance of the alkene that is fit to 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 molar 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,, can excessive isoparaffin be recycled in the reactor unit through one or more being contained the logistics recycling of isoparaffin.
Downstream hereinafter described are meant the direction of unitary fluid flow path from the reactor unit to the fractionator.The upper reaches hereinafter described are meant opposite direction, promptly from the fractionator unit to reactor unit.
Existing HF and SA alkylation comprise at least and are used to reactor unit that reactant is contacted with catalyzer.Reactor unit preferably comprises at least one reaction-ure inlet and at least one reactor effluent outlet.Preferably, reactor unit also comprises at least one catalyst inlet.The common reactant device unit that is arranged in the sulfuric acid alkylation unit is so-called Stratco contactor.In Stratco contactor for example, the hydrocarbon reaction thing is imported in the U-shaped reactor fluid flowing-path with catalyzer.For the HF alkylation, common reactor drum comprises for example Stratco contactor, gravity recirculation reactor and emulsion reactor drum.
Usually, the heat that alkylated reaction produced that cooling tube is removed heat release is set in the reactor fluid flowing-path.As another selection, sour recirculation stream is implemented cooling.The elute 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 elute with reactor unit is supplied to separator unit, thereby reactor effluent is separated into catalyzer phase and the hydrocarbon phase that comprises alkylate oil.Preferably, separator unit comprises at least one import (said import be generally used for reactor effluent or by the logistics of its generation) and at least one catalyzer exports the outlet that contains the hydrocarbon phase of alkylate oil with at least one mutually.
The effect of separator unit be the elute with reactor unit be separated into catalyzer mutually with the hydrocarbon phase that comprises alkylate oil.Preferably, used separator unit is the settling vessel unit in HF that is transformed and SA alkylation.Because HF and SA catalyzer are lower to the avidity of hydrocarbon, these two are separated under action of gravity easily.Settling vessel as herein described unit is meant any separator unit that two kinds of liquid phases are separated.In fact, HF, SA and IL catalyst density all are higher than the density of hydrocarbon phase, thus the hydrocarbon phase of reactor effluent above in settling vessel, being separated into usually with below catalyzer mutually.
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,, part SA catalyzer is removed from technology as the catalyzer that has consumed, and add fresh SA catalyzer levels of catalysts and activity are remained unchanged in order to keep catalyst activity.
For the alkylating situation of HF, make the HF catalyst regeneration and it be recycled in the process to supply to reuse.Therefore, the HF alkylation comprises catalyzer phase recirculation unit and comes recycling HF catalyzer, and makes up with independent regenerative process.
In SA and HF alkylation, the hydrocarbon phase that contains alkylate oil that in settling vessel, obtains is provided to the fractionator unit at least in part, obtains alkylate oil.The fractionator unit preferably comprises at least one import that contains 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, can the alkylate oil that obtained be used for preparing aviation spirit or use harmonic component as gasoline.Hydrocarbon phase also possibly comprise the unreacted isoparaffin of significant quantity.Preferably, the device that is used for isoparaffin is recycled to from the fractionator unit reactor drum that passes through to be provided is recycled to reactor unit with at least a portion of this isoparaffin.Through hydrocarbon phase is carried out 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 get into reactor drum, and the hydrocarbon phase that reactor effluent is supplied to separator unit and will contains alkylate oil subsequently 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, cool off or heat.This is equally applicable to just be provided to the unitary hydrocarbon phase that contains alkylate oil of fractionator.Usually, through the device with reactant and catalyzer importing reactor unit is set, produce the fluid flow path of reactant, product and catalyzer.In addition, setting device is with the reactor effluent import of reactor effluent from reactor effluent export supply to the separator unit of reactor unit, and wherein said separator unit is positioned at the reactor unit downstream in fluid flow path.In addition; From the unitary import that contains the hydrocarbon phase of alkylate oil of export supply to the fractionator of the hydrocarbon phase that contains alkylate oil of separator unit, wherein said fractionator unit is positioned at the separator unit downstream to setting device in fluid flow path with the hydrocarbon phase that contains alkylate oil; 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.Used catalyzer is to contain cationic compound ion liquid among the present invention, and said cationic source is from the halogen acid salt that contains amine, imidazoles or the pyridine of alkyl.Preferably, said positively charged ion comprises by four nitrogen-atoms that substituting group is saturated, and at least one Wasserstoffatoms and an alkyl are arranged in these substituting groups.More preferably, alkyl substituent is to be selected from least a in methyl, ethyl, propyl group, butyl, amyl group and the hexyl.The cationic instance that is fit 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, preferred aluminum chloride (III).Because the lewis acidic peracidity of aluminum chloride; Preferably aluminum chloride or other aluminium halogenides and second kind or more kinds of metal halide, vitriol or nitrate salt are made up and form coordination anion; Particularly be derived from the coordination anion of two or more metal halides, wherein at least a metal halide is an aluminium halogenide.Other metal halides, vitriol or the nitrate salt that is fit to can be selected from halogenide, vitriol or the nitrate salt of following metal, and said metal is selected from the group of being made up of the IB family element in the periodictable, IIB family element and the transition element in the periodictable in the periodictable.The instance of the metal that is fit to comprises copper, iron, zinc, nickel, cobalt, molybdenum or platinum.Preferably, said metal halide, vitriol or nitrate salt 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, further is preferably 2: 1 to 30: 1.Comprise the coordination anion of aluminium and other metals through use, can obtain improved alkylate oil product.For example among the US7285698 a kind of method for preparing this type of catalyzer is being described.Preferred especially catalyzer is to contain the acidic ionic liquid catalysts that is derived from aluminum chloride (III) and cupric chloride (II) or is derived from the coordination anion of aluminum chloride (III) and cuprous chloride (I).
In the method for the invention, swirler-is set and comes the separate reactor elute.In present HF or SA alkylation, be provided with the settling vessel unit and come from reactor effluent, to isolate HF or SA catalyzer and hydrocarbon phase.After HF or SA alkylation are transformed into the IL alkylation; Use former the design to be used for making HF or SA to come from reactor effluent, to separate the IL catalyzer and the hydrocarbon phase that comprises alkylate oil with the isolating existing settling vessel of hydrocarbon; Possibly produce some ill effects, comprise:
-Yin the recirculation volume of hydrocarbon more due to, need bigger 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;
-in settling vessel, form hydrocarbon-catalyst emulsion, thus operation problem brought for the control of settling vessel level;
-in catalyzer, comprising due to the hydrocarbon phase that contains alkylate oil of vast scale more, aspect the validity of recovering at fund cost (bigger equipment) and catalyst activity, catalyzer restores regenerated validity and descends.
Therefore, in the method for the invention, HF or the SA alkylation transformed preferably comprise the settling vessel unit as separator unit.In the method for the invention, be provided with the swirler-unit, and be provided with at least a portion reactor unit elute is supplied to the unitary device of swirler-, thereby add separating of powerful catalyst and hydrocarbon phase in the reactor unit downstream.Through using the swirler-unit, can reactor effluent be separated into the lower elute of the density that mainly comprises the hydrocarbon phase that contains alkylate oil and mainly comprise the higher elute of acidic ionic liquid catalysts density mutually.The swirler-unit can comprise one or more placed in-line swirler-subelements.Preferably, the swirler-unit comprises one or more hydrocyclones.Hydrocyclone as herein described is meant and is designed for the swirler-that makes water-hydrocarbon mixture phase-splitting.More preferably, the swirler-unit comprises placed in-line swirler-or hydrocyclone more than two, and wherein, the hydrocarbon phase to contain alkylate oil in first (waterpower) swirler-is that master's low density outflow thing is provided to the next one (waterpower) swirler-.This make the IL catalyzer mutually with hydrocarbon phase between separate and obtained further reinforcement.Preferably, said one or more swirler-s unit additionally is set to existing settling vessel unit.Preferably, said one or more swirler-s unit is arranged on the upper reaches, settling vessel unit, and setting device is sent to the settling vessel unit with the low density outflow thing that with the hydrocarbon phase that contains alkylate oil is the master from the swirler-unit.Through one or more swirler-s and the one or more settling vessels that are positioned at these at least one swirler-downstream are made up; To being that master's low density flows out thing and carries out further physical separation processes with the hydrocarbon phase that contains alkylate oil, can further be reduced in the hydrocarbon phase that contains alkylate oil is the ionic liquid ratio in the master's low density outflow thing.Though comparing the unitary volume of settling vessel with for example swirler-maybe 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 much littler than being used for the settling vessel unit of separate reactor elute in the common process.
Can the higher elute of the unitary density of the swirler-that mainly comprises the catalyzer phase be recycled to reactor unit, optional is that it is carried out recycling after (if any) merging mutually again with the catalyzer that in the settling vessel unit, obtains.Optional is parallel connection two above swirler-unit to be set with the increase capacity.These parallelly connected swirler-unit can make up with series system with one or more settling vessels.
In Fig. 1, the hydrocarbon mixture that comprises alkene and isoparaffin is supplied to reactor unit 100 (for example Stratco contactor) via conduit (for example, 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.Through reactor effluent outlet 114, the reactor effluent that will comprise catalyzer and hydrocarbon is supplied to settling vessel unit 120 from reactor unit 100 taking-ups and via conduit 115, process reactor effluent import 122.In settling vessel unit 120, catalyzer separates under action of gravity with the hydrocarbon phase that contains alkylate oil mutually.Hydrocarbon phase outlet 123 via containing alkylate oil is taken out hydrocarbon phase from separator unit 120, and through conduit 130 and the hydrocarbon phase import 133 that contains alkylate oil it is supplied to fractionator unit 125.From the bottom of fractionator unit 125, obtain to contain the product of alkylate oil through conduit 135.This alkylate oil product can be used for for example fuel mediation purposes.In addition, 125 obtain iso-paraffinic products from the fractionator unit, its recycling are become the part of the hydrocarbon mixture in the conduit 105 via conduit 140.Can also obtain the logistics (not shown) that other contain hydrocarbon from fractionator 125.
Export 143 mutually through catalyzer catalyzer taken out from separator unit 120, and can be recirculated to reactor unit 100 via catalyzer phase recycling pipe 145.Can the catalyst member that consume be taken out from this process via conduit 150.Can other live catalyst 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, between reactor unit and separator unit, be provided with the swirler-unit.In Fig. 2 A, reactor effluent is supplied to swirler-unit 505 via conduit 115.Via conduit 510, in the future the spin current device unitary with the hydrocarbon that contains alkylate oil be master's density lower be supplied to settling vessel unit 120 mutually.Via conduit 515, will be with the catalyzer main density higher be supplied to catalyst recycle conduit 145 mutually.Provided the more detailed depiction of feasible swirler-unit 505 among Fig. 2 B, wherein, the first swirler-subelement 550 that reactor effluent gets in the swirler-unit 505 via conduit 115.What density was lower leaves the first swirler-subelement 550 via conduit 555, and is provided to the second swirler-subelement 560 with further with catalyzer and the hydrocarbon phase separation that contains alkylate oil.The hydrocarbon phase that contains alkylate oil that density is lower leaves the second swirler-subelement 560 via conduit 565, and is provided to settling vessel unit 120.Respectively via conduit 570 and conduit 575, obtained the higher catalyzer of density mutually from the first swirler-subelement 550 and the second swirler-subelement 560, and can this catalyzer be supplied to catalyst recycle conduit 145 mutually.
Though 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 through following non-limiting example.
In order to show the validity of using swirler-rather than conventional settling vessel to come the separate reactor elute, use swirler-to separate with the reactor effluent sample of the mixture of ionic-liquid catalyst with product to comprising the hydrocarbon reaction thing.
It is 1: 1.05 hydrocarbon and ionic-liquid catalyst that the reactor effluent sample comprises 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 gets in the swirler-is 2m
3/ hour.
In test for the first time, the reactor effluent sample conduct of 40 volume % is master's lower the obtaining mutually of density with the hydrocarbon that contains alkylate oil.
The reactor effluent sample of remaining 60 volume % is as with the catalyzer being main higher the obtaining mutually of density.
Based on said be the volume of the lower phase of master's density with the hydrocarbon that contains alkylate oil, said is master's lower the comprising mutually of density with the hydrocarbon that contains alkylate oil:
The hydrocarbon of-95.5 volume %; With
The ionic liquid of-4.5 volume %.
Based on said be the volume of the higher phase of main density with the catalyzer, said is main higher the comprising mutually of density with the catalyzer:
The hydrocarbon of-17.7 volume %; With
The ionic liquid of-82.3 volume %.
Through using a separator, the density that with the hydrocarbon that contains alkylate oil is the master lower mutually in, that has reclaimed about 79 volume % is provided at the hydrocarbon in the reactor effluent sample at first.
In the settling vessel unit in downstream, further handling with the hydrocarbon that contains alkylate oil is master's the lower phase time of density, and the unitary volume size of this settling vessel is merely the settling vessel unitary 40% that is used for separating the total reactor elute.
In test for the second time, using two separating steps is to be that the lower phase of master's density is mutually higher with the density that is the master with the catalyzer with the hydrocarbon that contains alkylate oil with the reactor effluent sample separation.The separating resulting that is obtained is following.
The charging of the entering whizzer of 50 volume % (being the reactor effluent sample) obtains as the lower intermediate phase of density; Remaining 50 volume % obtain as the higher ionic liquid phase elute of density.
Based on the volume of said intermediate phase, said intermediate phase comprises:
The hydrocarbon of-98.3 volume %; With
The ionic liquid of-6.2 volume %.
Based on said be the volume of the higher phase of main density with the catalyzer, said is main higher the comprising mutually of density with the catalyzer:
The hydrocarbon of-90.0 volume %; With
The ionic liquid of-10.0 volume %.
The intermediate phase that is obtained is obtained as intermediate product, and it is carried out second swirler-separating step.In second swirler-separating step process, the intermediate phase of from swirler-, obtaining 85 volume % is as the lower hydrocarbon phase elute of density, and the intermediate phase that remains 15 volume % is obtained as the higher phase elute of density (also being called other elutes).
Based on the volume of the lower phase of the density that with the hydrocarbon that contains alkylate oil is the master, said is master's lower the comprising mutually of density with the hydrocarbon that contains alkylate oil:
The hydrocarbon of-98.5 volume %; With
The ionic liquid of-1.5 volume %.
Based on the volume of said other elutes, said other elutes comprise:
The hydrocarbon of-68.7 volume %; With
The ionic liquid of-31.3 volume %.
Through using two separators, the density that with the hydrocarbon that contains alkylate oil is the master lower mutually in, that has reclaimed about 86 volume % is provided at the hydrocarbon in the reactor effluent sample at first.
Through using two placed in-line separators (being swirler-in the case) to come from the reactor effluent sample to separate with the hydrocarbon that contains alkylate oil is master's the lower phase of density, can obtain the hydrocarbon in the reactor effluent sample of vast scale more and it is transported to fractionator.This be because the reactor effluent that has obtained vast scale more from first separator as intermediate phase.Though more the reactor effluent sample of vast scale becomes the increase that lighter intermediate phase can cause this heterogeneous elute intermediate ion liquid fraction; But because second separator step arranged, resulting with the hydrocarbon that contains alkylate oil be master's density lower mutually in final ionic liquid ratio much lower.So, can the hydrocarbon in the reactor effluent of vast scale more be separated with ionic liquid.Under the situation of only using a separator, with the hydrocarbon that contains alkylate oil be master's density lower comprise 79 volume % only mutually be present in hydrocarbon in the reactor effluent at first.Yet, in embodiment 1b, in the ion liquid hydrocarbon elute that comprises still less, obtained the hydrocarbon in the reactor effluent of 86 volume %.
In addition, compare with the situation of only using a separator, with the catalyzer be main density higher comprise hydrocarbon still less mutually, even under situation, also be like this with its and other elute merging.
When in the settling vessel unit in downstream to the hydrocarbon that contains alkylate oil be master's density lower do further processing mutually the time, the unitary volume size of this settling vessel is merely the settling vessel unitary 42.5% that is used for separating the total reactor elute.
Claims (5)
1. one kind transform HF or sulfuric acid alkylation unit the method for ionic liquid alkylation as, and wherein, said HF or sulfuric acid alkylation unit comprise at least:
-reactor unit, said reactor unit are used to make catalyzer to contact with the hydrocarbon reaction thing;
-separator unit, said separator unit are used for reactor effluent is separated into catalyzer phase and the hydrocarbon phase that comprises alkylate oil;
It is at least a logistics that comprises alkylate oil that-fractionator unit, said fractionator unit are used for the said hydrocarbon phase fractionation that comprises alkylate oil; And
Said method comprises:
-be provided with in the downstream of said reactor unit one or more swirler-s unit with the said reactor effluent of at least a portion be separated into catalyzer mutually with the hydrocarbon phase that comprises alkylate oil.
2. the method for claim 1, wherein said one or more swirler-s unit is positioned at the upper reaches of said separator unit.
3. the method for claim 1, wherein said separator unit is substituted by said one or more swirler-s unit.
4. like each described method in the aforementioned claim, wherein, the swirler-unit comprises one or more placed in-line swirler-subelements.
5. like each described method in the aforementioned claim, wherein, said swirler-unit comprises one or more hydrocyclones.
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|---|---|---|---|
| CN201080034574.0A CN102510849B (en) | 2009-08-06 | 2010-08-06 | Method for revamping HF or sulphuric acid alkylation unit |
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|---|---|---|---|
| CN2009000886 | 2009-08-06 | ||
| CNPCT/CN2009/000886 | 2009-08-06 | ||
| PCT/EP2010/061515 WO2011015664A2 (en) | 2009-08-06 | 2010-08-06 | Method for revamping an hf or sulphuric acid alkylation unit |
| CN201080034574.0A CN102510849B (en) | 2009-08-06 | 2010-08-06 | Method for revamping HF or sulphuric acid alkylation unit |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB647155A (en) * | 1941-04-24 | 1950-12-06 | Standard Oil Co | Improvements in or relating to a process of synthesizing hydrocarbons |
| US20040133056A1 (en) * | 2002-11-12 | 2004-07-08 | Zhichang Liu | Method for manufacturing alkylate oil with composite ionic liquid used as catalyst |
-
2010
- 2010-08-06 CN CN201080034574.0A patent/CN102510849B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB647155A (en) * | 1941-04-24 | 1950-12-06 | Standard Oil Co | Improvements in or relating to a process of synthesizing hydrocarbons |
| US20040133056A1 (en) * | 2002-11-12 | 2004-07-08 | Zhichang Liu | Method for manufacturing alkylate oil with composite ionic liquid used as catalyst |
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