CN105233784A - Alkylation reactor and alkylation method - Google Patents
Alkylation reactor and alkylation method Download PDFInfo
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- CN105233784A CN105233784A CN201410335877.6A CN201410335877A CN105233784A CN 105233784 A CN105233784 A CN 105233784A CN 201410335877 A CN201410335877 A CN 201410335877A CN 105233784 A CN105233784 A CN 105233784A
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Abstract
The invention discloses an alkylation reactor and an alkylation method. The alkylation reactor comprises a settling area, a reaction area and a mixing area, wherein the mixing area consists of a cylindrical mixing chamber, charging pipes and outlet nozzles, the mixing area communicates with the reaction area through the outlet nozzles, the reaction area is provided with alkene charging pipes, a cylindrical partition plate, a heat exchange pipe bundle and deflection baffles and is divided into two portions by the cylindrical partition plate, a central cylindrical space serves as a fluid rising zone, an external annular space serves as a fluid backflow zone, the rising zone and the backflow zone communicate with each other at the top parts and the bottom parts, the settling area is provided with a liquid rising pipe, a swirling component and a cylindrical baffle and is divided into two portions, i.e., a central cylindrical space and an external annular space by the cylindrical baffle, the spaces of the two portions communicate with each other at the top parts and the bottom parts, the liquid rising pipe and the swirling component are located in the central cylindrical space of the settling area, the bottom of the liquid rising pipe communicates with the rising zone of the reaction area, the top of the liquid rising pipe is connected with the swirling component, and the external annular space of the settling area is connected with a liquid acid outlet pipe and a hydrocarbon mixture outlet pipe. By using the alkylation reactor and the alkylation method, a liquid acid catalyst and alkane can be adequately mixed in the mixing area of the reactor, and polymerization among alkenes is reduced; and the reaction temperature is low, the acid-hydrocarbon separation is rapid, and the acid consumption is low.
Description
Technical field
The invention belongs to petroleum refining field, relate to a kind of for liquid acid catalysis C
4alkylation production method.More particularly, invention further provides a kind ofly realize alkane, alkene mixes fully with liquid acid catalyst, react and alkylation reactor that sour hydrocarbon is separated.
Background technology
Alkylation be isoparaffin under strongly acidic catalyst existent condition, react with alkene and generate the process of alkylate.In petroleum refining field, alkylation is iso-butane and C
3~ C
5the reaction of alkene under strong acid existence condition, the alkylate oil that described reaction generates has the octane number higher than raw material, and boiling spread is the component of gasoline.Alkylate oil has without aromatic hydrocarbons, without characteristics such as alkene, low-sulfur, low-steam pressure, high-octane ratings (RON94 ~ 96, MON92 ~ 94).Industrial conventional catalyst is the concentrated sulfuric acid and hydrofluoric acid, and in order to reduce side reaction, alkylated reaction carries out usually under cryogenic.Because liquid acid system is one of main method of producing high-knock rating gasoline at present, for this reason, proposed kinds of schemes both at home and abroad and improved the mixing of sour hydrocarbon, and decreased bad effect to a certain extent.
In traditional method, adopt static mixer or turbomachine to stir and reactant is distributed in continuous print acid mutually.The most widely used mixed catalyst and the method for reactant be by together with its component by the stirring that impeller is violent, such as US Patent No. 3759318; A kind of horizontal reactor disclosed in US4075258 and US5785933.Reaction raw materials enters the suction side of the impeller of reactor, under the strong stirring of impeller, reaction mass spreads rapidly and forms emulsion with acid, emulsion constantly circulates and reacts in reactor, alkylated reaction heat is removed by heat-exchanging tube bundle, part emulsion enters settler through tedge, carries out sour hydrocarbon separation.The acid consumption of Horizontal stirring reactor is higher, and a large amount of spent acid of generation bring huge environmental protection pressure; Product need through subtractive processes such as pickling, alkali cleaning and washings, and technological process is too complicated.
US Patent No. 6194625B1 discloses a kind of alkylation reactor of sectional feeding, reaction zone is separated into the section of multiple series connection, fresh feed is divided into multiply and introduces each reaction section, the sulfuric acid recycled is then series flow, adopts churned mechanically mode to mix in each reaction section.Although this structure overcomes the larger problem of back-mixing, structure is too complicated.In addition, the paddle that this employing fixed rotating speed motor drives, easily leaks because of poorly sealed under middle high-pressure operating condition.
US Patent No. 8461408 discloses a kind of high shear mixing method, and this patent includes a reactor with High shear device.Sulfuric acid and hydrocarbon material form mix emulsion fluid under the effect of High shear device, the emulsion formed enters reactor at impeller eye, under the strong stirring of impeller, complete alkylated reaction, reaction effluent enters acid settler and carries out sour hydrocarbon separation, the acid circulation Returning reactor be separated, the alkylate oil of generation then enters subsequent processing units.But High shear device power is comparatively large, and energy consumption is higher.
US Patent No. 7319180B2 discloses a kind of alkylation reactor, and reactor is static mixing reactor.In static mixer, filling woven wire and void space are greater than the filler of the contact structure of 50% volume.The hydrocarbon mixture that alkene and iso-butane form enters reactor, contacts, emulsion reaction with sulfuric acid catalyst.Reaction mass relies on filler self pressure drop to make light hydrocarbon component gasification absorption reaction heat.It is light hydrocarbon that the reaction heat of this patent reactor removes mode, and for maintaining lower reaction temperature, reactor needs a large amount of gasification spaces.In addition, also there is the shortcomings such as pressure drop is excessive in static mixer.
US Patent No. 5443799 discloses a kind of alkylation reactor, and this reactor is divided into premixed district and reaction zone.In premixed district, iso-butane is sprayed by nozzle and is mixed to form emulsion with sulfuric acid.At reaction zone, the alkene of injection contacts with the emulsion from premixed district, reacts.The volume of the reaction zone of this reactor is greater than premixed district, and after the mixture coming from premixed district enters reaction zone, because the volume of reaction zone increases suddenly, the light component gasification in mixture, adiabatic expansion absorbs alkylated reaction liberated heat.The reaction temperature of this technique is at 8 ~ 20 DEG C, and reaction temperature is higher.
US Patent No. 5785933 discloses a kind of static mixing and sprays the alkylation patented technology combined, utilize static mixer that the mixture of iso-butane, sulfuric acid and alkene is formed emulsion, this emulsion injects reactor at a high speed, constantly carry out shearing, mix and reacting in reactor, reaction heat is taken away by the lighter hydrocarbons evaporated.The evaporation removing dependence lighter hydrocarbons of reaction heat, operation easier is comparatively large, is difficult to control under lower temperature conditions.
Chinese patent CN101274249A discloses a kind of injecting type circulation flow reactor, utilizes the kinetic energy that Liquid inject produces, and makes reaction liquid at reactor internal circulation flow, well mixes and react.But the liquid reactions due to this reactor occurs in tedge, material is shorter at rising intraductal retention time, and this reactor does not arrange heat-obtaining device simultaneously, needs longer reaction time and lower temperature conditions and be not suitable for for alkylation.
Summary of the invention
The present invention be directed to the shortcoming of prior art existence and a kind of alkylation reactor and alkylation are provided, more low viscous reaction liquid can be broken into very little drop after using reactor of the present invention, make itself and full-bodied acid Homogeneous phase mixing, emulsification in a short period of time mutually, larger liquid-liquid contact area is provided, make the conversion ratio that reaction reaches very high, and reaction heat can be removed rapidly, maintain the low temperature environment of reactor, the quick separating of sour hydrocarbon two-phase can also be realized simultaneously.
The invention provides a kind of alkylation reactor, comprise cylindrical shell and end socket, it is characterized in that: cylindrical shell top is decanting zone, region between cylindrical shell bottom and end socket is reaction zone, it is mixed zone below reaction zone, mixed zone is by columnar mixing chamber, feed pipe and outlet nozzle composition, mixing chamber top arranges outlet nozzle, bottom arranges feed pipe, mixing chamber top and outlet nozzle enter reaction zone through end socket, reaction zone is provided with olefin feedstocks pipe, cylinder dividing plate, heat-exchanging tube bundle and hydraulic barrier, reaction zone is divided into two parts by described cylinder dividing plate, cylindrical space in the middle of cylinder dividing plate is the rising area of fluid, the annular space of cylinder dividing plate is the recirculating zone of fluid, rising area is communicated with up and down with recirculating zone, decanting zone is provided with liquid tedge, eddy flow component and cylinder baffle plate, decanting zone is divided into two parts by cylinder baffle plate, cylindrical space in the middle of decanting zone and the annular space of outside, decanting zone, two parts are spatially lower to be communicated with, liquid tedge and eddy flow component are positioned at the cylindrical space in the middle of decanting zone, be communicated with the rising area of reaction zone bottom liquid tedge, liquid tedge top is connected with eddy flow component, the annular space of outside, decanting zone connects liquid acid outlet, hydrocarbon mixture outlet, described cylindrical shell, mixing chamber, cylinder dividing plate, cylinder baffle plate and liquid tedge are coaxially arranged.
The further technical characteristic of the present invention is: described feed pipe is made up of alkane feed pipe and liquid acid feed pipe respectively, alkane feed pipe is positioned at the bottom of mixing chamber, the dead in line or parallel of its axis and mixing chamber, liquid acid feed pipe is positioned at both sides in opposite directions, mixing chamber side, according to different mixed effects, the axis of liquid acid feed pipe also can become 20 ° ~ 60 ° angles with the axes normal of mixing chamber; The axis of outlet nozzle and the axis being parallel of mixing chamber.
The further technical characteristic of the present invention is: described feed pipe is made up of alkane feed pipe and liquid acid feed pipe respectively, alkane feed pipe inserts in mixing chamber from bottom, the dead in line of its axis and mixing chamber, alkane feed pipe is furnished with the aperture that aperture is Φ 3 ~ Φ 15 within the scope of 360 °, percent opening is 20% ~ 60%, with alkane feed pipe outer surface for benchmark, alkane feed pipe end is back taper, and the distance at distance mixing chamber top, back taper summit is 1 ~ 5 times of alkane feed pipe external diameter; Liquid acid feed pipe is positioned at both sides in opposite directions, mixing chamber side, and the axis of liquid acid feed pipe also can become 20 ° ~ 60 ° angles with the axes normal of mixing chamber; The axis of outlet nozzle and the axis being parallel of mixing chamber.
The further technical characteristic of the present invention is: described alkene adopts multiple spot dispersion sprayed feed, olefin feedstocks pipe can be arranged near the outlet nozzle of mixed zone, also rising area and the recirculating zone of reaction zone can be arranged in, when described olefin feedstocks pipe is arranged on the rising area of reaction zone, adopt and upwards spray, spray angle and reactor axis angle are 10 ° ~ 60 °; When being arranged on the recirculating zone of reaction zone, adopt Jet with downward flow direction, spray angle and reactor axis angle are 10 ° ~ 60 °.
The further technical characteristic of the present invention is: described cylinder dividing plate diameter is 0.5 ~ 0.7 times of reactor diameter, the distance of cylinder dividing plate top distance liquid tedge is 0.1 ~ 0.5 times of cylinder dividing plate diameter, be undergauge structure bottom cylinder dividing plate, the outlet nozzle distance apart from mixed zone bottom cylinder dividing plate is less than injection stream length.
The further technical characteristic of the present invention is: described reaction zone arranges heat-exchanging tube bundle, removes alkylated reaction heat by the cooling medium heat exchange in the material of reaction zone and heat-exchanging tube bundle; Described heat-exchanging tube bundle can be arranged on the rising area of reaction zone, also can be arranged on the recirculating zone of reaction zone.
The further technical characteristic of the present invention is: described reaction zone arranges hydraulic barrier, increase the turbulence characteristic of material at reaction zone, avoid the layering in reaction zone of acid hydrocarbon emulsification liquid, described hydraulic barrier can be arranged on the rising area of reaction zone, also can be arranged on the recirculating zone of reaction zone.
The further technical characteristic of the present invention is: the cylinder baffle plate diameter of described decanting zone is 0.5 ~ 0.8 times of reactor diameter, the distance of cylinder baffle plate top distance eddy flow means outlet is 0.2 ~ 0.5 times of decanting zone height, is 0.05 ~ 0.2 times of decanting zone height bottom cylinder baffle plate apart from decanting zone distance from bottom.
The further technical characteristic of the present invention is: the top of described liquid tedge is connected with eddy flow component, and the cross-sectional area of liquid tedge is 0.1 ~ 0.3 times of rising area cross-sectional area.
The further technical characteristic of the present invention is: described eddy flow component has 2 ~ 6 outlets, after emulsion enters eddy flow component by tedge, move downward in the mode of eddy flow, the acid that density is larger enters outside annular space mutually, the hydrocarbon phase that density is less then enters middle cylindrical space, the bottom quiescent settling that unsegregated emulsion enters decanting zone is separated, and the volume of decanting zone should ensure that the time of staying of liquid in decanting zone is not less than the quiet straight separation time of liquid.
The present invention also provides a kind of alkylation using abovementioned alkyl reactor, it is characterized in that: alkane and liquid acid are entered the mixed zone mixing chamber of alkylation reactor respectively by alkane feed pipe and liquid acid feed pipe, mixed acid hydrocarbon emulsification liquid sprays into reaction zone by outlet nozzle, material enters the backward upper flowing of reaction zone, with the olefin entered through olefin feedstocks pipe, dispersion, emulsification and carry out alkylated reaction, alkylation reaction product and unreacted material shape resulting mixture stream, the recirculating zone of reaction zone is advanced under transferring after part mixture flows through cylinder dividing plate, the rising area of reaction zone is returned to again after bottom recirculating zone, constantly circulate in reaction zone, alkylated reaction is carried out more fully, another part mixing logistics enters decanting zone by the liquid tedge at reaction zone top, decanting zone is provided with eddy flow component, acid hydrocarbon mixture material is by the backward lower swirling two-phase flows of eddy flow component, the separation of the centrifugal forces enhance acid hydrocarbon utilizing eddy flow process to produce, sulfuric acid content is higher, the emulsion (being called sour phase) that density is larger enters bottom the annular space of outside, decanting zone, and hydrocarbon content is higher, the emulsion (being called hydro carbons) that density is less then enters the bottom of the cylindrical space in the middle of decanting zone, two parts logistics continues quiescent settling layering in the bottom of settler, lower floor be separated acid mutually major part as recycle acid through liquid acid outlet out, after buffering boosting, enter in the liquid acid feed pipe of mixed zone and recycle, a small amount of with the direct discharger of the form of spent acid, the mixing hydrocarbon phase on upper strata through hydrocarbon mixture outlet out, enter in the heat-exchanging tube bundle in reaction zone after vacuum flashing as cooling medium, mixing hydrocarbon phase after heat exchange enters flash tank, gas phase in flash tank enters hydrocarbon mixture surge tank after compressor compression, then pump in the alkane feed pipe of mixed zone by hydrocarbon mixture pump, liquid phase in flash tank enters deisobutanizer, the isolated iso-butane of tower top returns hydrocarbon mixture surge tank with the recycle isobutane from compressor, alkylate oil product introduction subsequent processing units is fractionated out at the bottom of tower.
Compared with prior art, tool has the following advantages for a kind of alkylation reactor provided by the invention and alkylation: (1) sour hydrocarbon good mixing effect.Liquid acid catalyst mixes fully with the mixed zone of alkane at reactor, prepares acid hydrocarbon emulsification liquid, after this emulsion enters the reaction zone of reactor, generates alkylate oil with olefine reaction.Compared with other alkylation process, the present invention can make alkane and liquid acid catalyst mix fully, and reduce the polymerization between alkene, the quality of the alkylate oil of production is higher, and acid consumption is simultaneously lower.(2) reaction temperature is low.Alkylated reaction is exothermic reaction, and the present invention utilizes heat-exchanging tube bundle indirectly to remove the heat of reaction system, by flow and the temperature of flexible modulation cryogen, controls reaction to greatest extent and carries out under suitable temperature conditions.(3) sour hydrocarbon separation is rapid, acid consumption is low.The present invention adopts cyclone mode to realize the rapid separation of sour hydrocarbon two-phase, shortens the time that sour hydrocarbon is separated, decreases the secondary response of alkylate oil.Meanwhile, effluent carries acid amount to be reduced, and reduces spent acid processing cost, decreases the pollution to environment.In addition, structure of reactor design of the present invention is ingenious, and liquid-liquid contact area is large, without mixing component, not easily leaks, and temperature controls evenly.
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.But do not limit the scope of protection of present invention.
Accompanying drawing illustrates:
Fig. 1 is a kind of alkylation reactor schematic diagram of the present invention;
Fig. 2 is the structural representation of a kind of mixed zone of the present invention;
Fig. 3 is the structural representation of the another kind of mixed zone of the present invention;
Fig. 4 is alkylation simple flow chart of the present invention;
Reference numeral shown in figure is:
1-alkylation reactor; 2-mixed zone; 3-reaction zone; 4-decanting zone; 5-alkane feed pipe; 6-liquid acid feed pipe; 7-mixing chamber; 8-outlet nozzle; 9-olefin feedstocks pipe; 10-cylinder dividing plate; 11-heat-exchanging tube bundle; 12-hydraulic barrier; 13-liquid tedge; 14-cylinder baffle plate; 15-eddy flow component; 16-liquid acid outlet; 17-hydrocarbon mixture outlet; 18-pressure-reducing valve; 19-flash tank; 20-compressor; 21-deisobutanizer; 22-liquid acid pump; 23-hydrocarbon mixture pump; 24-liquid acid surge tank; 25-hydrocarbon mixture surge tank.
Detailed description of the invention:
Be fed in reactor by alkane, low-carbon alkene and liquid acid catalyst, low-carbon alkene comprises butylene, propylene, amylene or alkene mixture, and preferred reaction mass is liquefied gas and the concentrated sulfuric acid after iso-butane, ether.Be 0.3 ~ 0.8MPa at operating pressure, reaction temperature is under the condition of 0 ~ 20 DEG C, realizes the alkylated reaction of alkene and alkane; The alkane alkene ratio of reaction mass is 1: 1 ~ 15: 1, and acid hydrocarbon ratio is 1: 1 ~ 5: 1.
Other processing steps involved in the method for the invention, such as pretreatment of raw material, gas-liquid separation, the processing units such as reaction effluent pickling, alkali cleaning are identical with conventional alkylation processes.Further illustrate method provided by the present invention below in conjunction with accompanying drawing, but the present invention is not therefore subject to any restriction.
As shown in Figure 1, a kind of alkylation reactor 1, comprise cylindrical shell and end socket, it is characterized in that: cylindrical shell top is decanting zone 4, region between cylindrical shell bottom and end socket is reaction zone 3, it is mixed zone 2 below reaction zone 3, as shown in Figure 2, mixed zone 2 is by columnar mixing chamber 7, feed pipe and outlet nozzle 8 form, mixing chamber 7 top arranges outlet nozzle 8, bottom arranges feed pipe, mixing chamber 7 top and outlet nozzle 8 enter reaction zone 3 through end socket, reaction zone 3 is provided with olefin feedstocks pipe 9, cylinder dividing plate 10, heat-exchanging tube bundle 11 and hydraulic barrier 12, reaction zone 3 is divided into two parts by described cylinder dividing plate 10, cylindrical space in the middle of cylinder dividing plate 10 is the rising area of fluid, the annular space of cylinder dividing plate 10 is the recirculating zone of fluid, rising area is communicated with up and down with recirculating zone, decanting zone 4 is provided with liquid tedge 13, eddy flow component 15 and cylinder baffle plate 14, decanting zone 4 is divided into two parts by cylinder baffle plate 14, cylindrical space in the middle of decanting zone 4 and the annular space of outside, decanting zone 4, two parts are spatially lower to be communicated with, liquid tedge 13 and eddy flow component 15 are positioned at the cylindrical space in the middle of decanting zone 4, be communicated with the rising area of reaction zone 3 bottom liquid tedge 13, liquid tedge 13 top is connected with eddy flow component 15, the annular space of outside, decanting zone 4 connects liquid acid outlet 16, hydrocarbon mixture outlet 17, described cylindrical shell, mixing chamber 7, cylinder dividing plate 10, cylinder baffle plate 14 and liquid tedge 13 are coaxially arranged.
In reaction zone 3, the diameter of cylinder dividing plate 10 is 0.5 ~ 0.7 times of reactor diameter, the distance of cylinder dividing plate 10 top distance liquid tedge 13 is 0.1 ~ 0.5 times of cylinder dividing plate 10 diameter, be undergauge structure bottom cylinder dividing plate 10, the distance of the outlet nozzle 8 apart from mixed zone 2 bottom cylinder dividing plate 10 is less than injection stream length.Described olefin feedstocks pipe 9 can be arranged near the outlet nozzle 8 of mixed zone 2, also rising area and the recirculating zone of reaction zone 3 can be arranged in, when described olefin feedstocks pipe 9 is arranged on the rising area of reaction zone 3, adopt and upwards spray, spray angle and reactor axis angle are 10 ~ 60 °, when olefin feedstocks pipe 9 is arranged on the recirculating zone of reaction zone 3, adopt Jet with downward flow direction, spray angle and reactor axis angle are 10 ~ 60 °, and certain spray angle can promote that fluid is at reaction zone internal circulation flow; Cooling medium in described heat-exchanging tube bundle 11 and the material-heat-exchanging of reaction zone 3 remove alkylated reaction heat; Described hydraulic barrier 12 increases the turbulence characteristic of material at reaction zone 3, avoids the layering in reaction zone 3 of acid hydrocarbon emulsification liquid.Described decanting zone 4 is provided with liquid tedge 13, cylinder baffle plate 14, eddy flow component 15, liquid acid outlet 16 and hydrocarbon mixture outlet 17.Decanting zone 4 is divided into two parts by cylinder baffle plate 14, middle circular space and outside annular space, two parts are spatially lower to be communicated with, cylinder baffle plate 14 diameter is 0.5 ~ 0.8 times of barrel diameter, cylinder baffle plate 14 top is 0.2 ~ 0.5 times of decanting zone height apart from the distance that eddy flow component 15 exports, and is 0.05 ~ 0.2 times of decanting zone height bottom cylinder baffle plate 14 apart from decanting zone 4 distance from bottom; Eddy flow component 15 is positioned at middle cylindrical space, eddy flow component 15 has 2 ~ 6 outlets, liquid tedge 13 is connected with eddy flow component 15, and the cross-sectional area of liquid tedge 13 is 0.1 ~ 0.3 times of rising area cross-sectional area, and axis overlaps with the axis of reactor.
As shown in Figure 3, for alkane feed pipe 5 being opened foraminate mixed zone 2, it is by alkane feed pipe 5, liquid acid feed pipe 6, mixing chamber 7 and outlet nozzle 8 form, alkane feed pipe 5 inserts in mixing chamber 7 from bottom, alkane feed pipe 5 axis and mixing chamber 7 dead in line or parallel (for overlapping shown in Fig. 2), liquid acid feed pipe 6 is positioned at both sides in opposite directions, mixing chamber 7 side, according to different mixed effects, liquid acid feed pipe 6 axis also can become 20 ° ~ 60 ° angles with mixing chamber 7 axes normal, outlet nozzle 8 is positioned at mixing chamber 7 top, the axis of nozzle 8 and mixing chamber 7 axis being parallel.Alkane feed pipe 5 is furnished with the aperture that aperture is Φ 3 ~ Φ 15 within the scope of 360 °, percent opening is 20% ~ 60% (with alkane feed pipe outer surface for benchmark), alkane feed pipe 5 end is back taper, the spacing of back taper summit and mixing chamber 7 top exit is 1 ~ 5 times of alkane feed pipe external diameter, liquid acid feed pipe 6 is positioned at both sides in opposite directions, mixing chamber 7 side, liquid acid feed pipe 6 axis also can become 20 ~ 60 ° of angles with mixing chamber 7 axes normal, outlet nozzle 8 is positioned at mixing chamber 7 top, nozzle-axis and mixing chamber 7 axis being parallel.Reaction zone is identical with embodiment 1 with the structure of decanting zone.
As shown in Figure 4, a kind of alkylation reaction method, its process is: iso-butane and liquid acid catalyst are sprayed by alkane feed pipe 5 and liquid acid feed pipe 6 respectively and enter in mixing chamber 7, two strands of materials collide in mixing chamber 7, emulsification mixes, in mixed zone 2, form liquid acid is continuous phase, alkane is the acid hydrocarbon emulsification liquid of decentralized photo, mixed acid hydrocarbon emulsification liquid sprays into reaction zone 3 at a high speed by outlet nozzle 8, material enters the backward upper flowing of reaction zone 3, the alkene rapid mixing sprayed with the olefin feedstocks pipe 9 be arranged in reaction zone 3, dispersion, emulsification, alkane is made to contact with liquid acid catalyst with the hydrocarbon mixture of alkene under alkylating conditions, thus acquisition alkylate oil.Mixed liquor is advanced into recirculating zone under transferring after cylinder dividing plate 10, returns to rising area again after bottom liquid flow to recirculating zone.Utilize the kinetic energy spraying generation that emulsion is constantly circulated in reaction zone 3, alkylated reaction is carried out more fully.Another part emulsion (product, unreacted reactant and liquid acid catalyst) enter decanting zone 4 by the liquid tedge 13 at reaction zone 3 top, decanting zone 4 is provided with eddy flow component 15, acid hydrocarbon mixture material is moved downward by the state with High Rotation Speed after eddy flow component 15, because sour hydrocarbon two-phase has larger density contrast, the centrifugal force utilizing emulsion to produce in downward eddy flow process is by most sour hydrocarbon centrifugation, the acid that density is larger enters outside annular space mutually, the hydro carbons that density is less then enters middle cylindrical space, unsegregated emulsion then enters bottom decanting zone 4 and continues quiescent settling layering, decanting zone 4 volume should ensure that the time of staying of liquid in decanting zone 4 is not less than the liquid static layering time.The acid that lower floor is separated introduces liquid acid surge tank 24 as recycle acid through liquid acid outlet 16, then pumps in mixed zone 2 liquid acid feed pipe 6, on a small quantity with the direct discharger of the form of spent acid by liquid acid pump 22.The mixing hydrocarbon phase on upper strata enters temperature after pressure-reducing valve 18 vacuum flashing through hydrocarbon mixture outlet 17 to be reduced, post-decompression mixing hydrocarbon phase enters in the heat-exchanging tube bundle 11 in reaction zone 3 as cooling medium, mixing hydrocarbon phase after heat exchange enters flash tank 19, gas phase in flash tank 19 enters hydrocarbon mixture surge tank 25 after compressor 20 compresses, then pump in mixed zone 2 alkane feed pipe 5 by hydrocarbon mixture pump 23, liquid phase in flash tank 19 enters deisobutanizer 21, the isolated iso-butane of tower top returns hydrocarbon mixture surge tank 25 with the recycle isobutane from compressor 20, alkylate oil product introduction subsequent processing units is fractionated out at the bottom of tower.
In the ken that alkylation those skilled in the art possess, alkylation reactor of the present invention and alkylation can also produce multiple change, and all do not depart from technical scheme and the improvement thereof of the scope of the invention, it all should be encompassed in the middle of right of the present invention.
Claims (11)
1. an alkylation reactor, comprise cylindrical shell and end socket, it is characterized in that: cylindrical shell top is decanting zone, region between cylindrical shell bottom and end socket is reaction zone, it is mixed zone below reaction zone, mixed zone is by columnar mixing chamber, feed pipe and outlet nozzle composition, mixing chamber top arranges outlet nozzle, bottom arranges feed pipe, mixing chamber top and outlet nozzle enter reaction zone through end socket, reaction zone is provided with olefin feedstocks pipe, cylinder dividing plate, heat-exchanging tube bundle and hydraulic barrier, reaction zone is divided into two parts by described cylinder dividing plate, cylindrical space in the middle of cylinder dividing plate is the rising area of fluid, the annular space of cylinder dividing plate is the recirculating zone of fluid, rising area is communicated with up and down with recirculating zone, decanting zone is provided with liquid tedge, eddy flow component and cylinder baffle plate, decanting zone is divided into two parts by cylinder baffle plate, cylindrical space in the middle of decanting zone and the annular space of outside, decanting zone, two parts are spatially lower to be communicated with, liquid tedge and eddy flow component are positioned at the cylindrical space in the middle of decanting zone, be communicated with the rising area of reaction zone bottom liquid tedge, liquid tedge top is connected with eddy flow component, the annular space of outside, decanting zone connects liquid acid outlet and hydrocarbon mixture outlet, described cylindrical shell, mixing chamber, cylinder dividing plate, cylinder baffle plate and liquid tedge are coaxially arranged.
2. a kind of alkylation reactor according to claim 1, it is characterized in that: described feed pipe is made up of alkane feed pipe and liquid acid feed pipe, alkane feed pipe is positioned at the bottom of mixing chamber, the dead in line or parallel of its axis and mixing chamber, liquid acid feed pipe is positioned at both sides in opposite directions, mixing chamber side, the axes normal of its axis and mixing chamber or become 20 ° ~ 60 ° angles; The axis of outlet nozzle and the axis being parallel of mixing chamber.
3. a kind of alkylation reactor according to claim 1, it is characterized in that: described feed pipe is made up of alkane feed pipe and liquid acid feed pipe, alkane feed pipe inserts in mixing chamber from bottom, the dead in line of its axis and mixing chamber, alkane feed pipe is furnished with the aperture that aperture is Φ 3 ~ Φ 15 within the scope of 360 °, percent opening is 20% ~ 60%, with alkane feed pipe outer surface for benchmark, alkane feed pipe end is back taper, and the distance at distance mixing chamber top, back taper summit is 1 ~ 5 times of alkane feed pipe external diameter; Liquid acid feed pipe is positioned at both sides in opposite directions, mixing chamber side, and the axis of liquid acid feed pipe with the axes normal of mixing chamber or can become 20 ~ 60 ° of angles; The axis of outlet nozzle and the axis being parallel of mixing chamber.
4. a kind of alkylation reactor according to claim 1, it is characterized in that: described olefin feedstocks pipe is arranged in around the outlet nozzle of mixed zone, or be arranged in rising area or the recirculating zone of reaction zone, when described olefin feedstocks pipe is arranged in the rising area of reaction zone, adopt and upwards spray, spray angle and reactor axis angle are 10 ~ 60 °; When being arranged in the recirculating zone of reaction zone, adopt Jet with downward flow direction, spray angle and reactor axis angle are 10 ~ 60 °.
5. a kind of alkylation reactor according to claim 1, it is characterized in that: described cylinder dividing plate diameter is 0.5 ~ 0.7 times of reactor diameter, the distance of cylinder dividing plate top distance liquid tedge is 0.1 ~ 0.5 times of cylinder dividing plate diameter, be undergauge structure bottom cylinder dividing plate, the outlet nozzle distance apart from mixed zone bottom cylinder dividing plate is less than injection stream length.
6. a kind of alkylation reactor according to claim 1, is characterized in that: the heat-exchanging tube bundle that described reaction zone is arranged, and is arranged on rising area or the recirculating zone of reaction zone.
7. a kind of alkylation reactor according to claim 1, is characterized in that: the hydraulic barrier that described reaction zone is arranged, and is arranged on the rising area of reaction zone, or the recirculating zone of reaction zone.
8. a kind of alkylation reactor according to claim 1, it is characterized in that: the cylinder baffle plate diameter of described decanting zone is 0.5 ~ 0.8 times of reactor diameter, the distance of cylinder baffle plate top distance eddy flow means outlet is 0.2 ~ 0.5 times of decanting zone height, is 0.05 ~ 0.2 times of decanting zone height bottom cylinder baffle plate apart from decanting zone distance from bottom.
9. a kind of alkylation reactor according to claim 1, is characterized in that: the cross-sectional area of described liquid tedge is 0.1 ~ 0.3 times of rising area cross-sectional area.
10. a kind of alkylation reactor according to claim 1, is characterized in that: described eddy flow component is provided with 2 ~ 6 outlets.
11. 1 kinds of alkylations using alkylation reactor described in claim 1, it is characterized in that: alkane and liquid acid are entered the mixed zone mixing chamber of alkylation reactor respectively by alkane feed pipe and liquid acid feed pipe, mixed acid hydrocarbon emulsification liquid sprays into reaction zone by outlet nozzle, material enters the backward upper flowing of reaction zone, with the olefin entered through olefin feedstocks pipe, dispersion, emulsification and carry out alkylated reaction, alkylation reaction product and unreacted material shape resulting mixture stream, the recirculating zone of reaction zone is advanced under transferring after part mixture flows through cylinder dividing plate, the rising area of reaction zone is returned to again after bottom recirculating zone, generation alkylated reaction is constantly circulated in reaction zone, another part mixing logistics enters decanting zone by the liquid tedge at reaction zone top, decanting zone is provided with eddy flow component, acid hydrocarbon mixture material is by the backward lower swirling two-phase flows of eddy flow component, the centrifugal force utilizing eddy flow process to produce makes sour hydrocarbon be separated, acid enters bottom the annular space of outside, decanting zone mutually, hydro carbons enters the bottom of the cylindrical space in the middle of decanting zone, two parts logistics continues quiescent settling layering in the bottom of settler, lower floor be separated acid mutually major part as recycle acid through liquid acid outlet out, after buffering boosting, enter in the liquid acid feed pipe of mixed zone and recycle, a small amount of with the direct discharger of the form of spent acid, the mixing hydrocarbon phase on upper strata through hydrocarbon mixture outlet out, enter in the heat-exchanging tube bundle in reaction zone after vacuum flashing as cooling medium, mixing hydrocarbon phase after heat exchange enters flash tank, gas phase in flash tank enters hydrocarbon mixture surge tank after compressor compression, then pump in the alkane feed pipe of mixed zone by hydrocarbon mixture pump, liquid phase in flash tank enters deisobutanizer, the isolated iso-butane of tower top returns hydrocarbon mixture surge tank with the recycle isobutane from compressor, alkylate oil product introduction subsequent processing units is fractionated out at the bottom of tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410335877.6A CN105233784B (en) | 2014-07-07 | 2014-07-07 | Alkylation reactor and alkylation method |
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| CN111589407A (en) * | 2020-05-20 | 2020-08-28 | 中石化南京工程有限公司 | Sulfuric acid alkylation system and method for producing isooctane by using same |
| CN112237896A (en) * | 2020-09-21 | 2021-01-19 | 中国石油大学(华东) | Novel mixing-enhanced reactor for alkylation of ionic liquid |
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| CN110876855B (en) * | 2018-09-06 | 2021-05-14 | 中国石油化工股份有限公司 | Separation method of low-carbon olefin and alkane alkylation product, separation method and device for low-carbon olefin and alkane alkylation reaction |
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| CN112237896B (en) * | 2020-09-21 | 2022-04-12 | 中国石油大学(华东) | Novel mixing-enhanced reactor for alkylation of ionic liquid |
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