CN105233784B - Alkylation reactor and alkylation method - Google Patents
Alkylation reactor and alkylation method Download PDFInfo
- Publication number
- CN105233784B CN105233784B CN201410335877.6A CN201410335877A CN105233784B CN 105233784 B CN105233784 B CN 105233784B CN 201410335877 A CN201410335877 A CN 201410335877A CN 105233784 B CN105233784 B CN 105233784B
- Authority
- CN
- China
- Prior art keywords
- zone
- liquid
- feed pipe
- mixing chamber
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
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, it is related to a kind of for liquid acid catalysis C4Alkylation production method.Particularly
, realize that alkane, alkene and liquid acid catalyst sufficiently mix, react and sour hydrocarbon point invention further provides one kind
From alkylation reactor.
Background technology
Alkylation is isoparaffin under conditions of strongly acidic catalyst presence, is produced with the alkene generation alkylation that reacts
The process of thing.In petroleum refining field, alkylation is iso-butane and C3~C5Reaction of the alkene under strong acid existence condition, institute
Stating the alkylate oil of reaction generation has the octane number higher than raw material, and boiling spread is the component of gasoline.Alkylate oil has
Without aromatic hydrocarbons, without alkene, low-sulfur, low-steam pressure, the high-octane rating (characteristic such as RON94~96, MON92~94).Industrially commonly use
Catalyst is the concentrated sulfuric acid and hydrofluoric acid, and in order to reduce side reaction, alkylated reaction is generally carried out under cryogenic.Due to liquid
Acid system is to produce one of main method of high-knock rating gasoline at present, therefore, having been presented for kinds of schemes both at home and abroad improves sour hydrocarbon
Mixing, and bad effect is reduced to a certain extent.
In traditional method, reactant is distributed to by continuous acid phase using static mixer or turbomachine stirring
In.Most widely used mixed catalyst is to pass through the violent stirring of impeller, example together with its component with the method for reactant
Such as United States Patent (USP) US 3759318；A kind of horizontal reactor disclosed in US 4075258 and US 5785933.Reaction raw materials are entered
The suction side of the impeller of reactor, reaction mass spreads rapidly and forms emulsion, emulsification with acid under the strong stirring of impeller
Liquid is constantly circulated and reacted in reactor, and alkylated reaction heat is removed by heat-exchanging tube bundle, and part emulsion is through upper
Riser enters settler, 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 to be excessively complicated through the subtractive processes such as pickling, alkali cleaning and washing, technological process.
The B1 of United States Patent (USP) US 6194625 disclose a kind of alkylation reactor of sectional feeding, and reaction zone is divided into
The section of multiple series connection, is divided into fresh feed multiply and introduces each reaction section, and the sulfuric acid for recycling is then series flow
, mixed using churned mechanically mode in each reaction section.Although this structure overcomes the larger problem of back-mixing,
But structure is excessively complicated.In addition, the agitating paddle of this use fixed rotating speed motor-driven, under middle high-pressure operating condition easily
Leaked because poorly sealed.
United States Patent (USP) US 8461408 discloses a kind of high shear mixing method, and the patent includes one with high shear
The reactor of equipment.Sulfuric acid and hydrocarbon material form mix emulsion fluid in the presence of High shear device, and the emulsion of formation exists
Impeller eye enters reactor, under the strong stirring of impeller, completes alkylated reaction, and reaction effluent enters into acid settler
Row acid hydrocarbon is separated, and the acid of separation is recycled back into reactor, and the alkylate oil of generation then enters subsequent processing units.But high shear
Plant capacity is larger, and energy consumption is higher.
The B2 of United States Patent (USP) US 7319180 disclose a kind of alkylation reactor, and reactor is static mixing reactor.It is quiet
Filling woven wire and void space are more than the filler of the contact structure of 50% volume in state blender.Alkene and iso-butane group
Into hydrocarbon mixture enter reactor, contacted with sulfuric acid catalyst, emulsion reaction.Reaction mass makes by filler itself pressure drop
Light hydrocarbon component gasification absorbing reaction heat.It is light hydrocarbon that the reaction heat of the patent reactor removes mode, to remain relatively low anti-
Temperature is answered, reactor needs substantial amounts of gasification space.Additionally, static mixer also exist pressure drop it is excessive the shortcomings of.
United States Patent (USP) US 5443799 discloses a kind of alkylation reactor, and the reactor is divided into pre-mix zone and reaction
Area.In pre-mix zone, iso-butane is sprayed by nozzle and is mixed to form emulsion with sulfuric acid.In reaction zone, the alkene of injection with come from
The emulsion contact of pre-mix zone, reaction.The volume of the reaction zone of the reactor is more than pre-mix zone, comes from pre-mix zone
After mixture 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 the technique is at 8~20 DEG C, and reaction temperature is higher.
United States Patent (USP) US 5785933 discloses the alkylation patented technology that a kind of static mixing is combined with injection, using quiet
The mixture of iso-butane, sulfuric acid and alkene is formed emulsion by state blender, and the emulsion injects reactor at a high speed, in reactor
Inside constantly sheared, mixed and reacted, the lighter hydrocarbons that reaction heat is evaporated are taken away.The removal of reaction heat relies on the steaming of lighter hydrocarbons
Hair, operation difficulty is larger, it is difficult to control under relatively low temperature conditionss.
Chinese patent CN 101274249A disclose a kind of injecting type circulation flow reactor, using moving that liquid injection is produced
Can, reaction liquid is mixed and is reacted in reactor internal circulation flow, well.But because the liquid reactions of the reactor occur
In tedge, material is shorter in rising intraductal retention time, while the reactor is not provided with taking thermal, is needed for alkylation
Reaction time and relatively low temperature conditionss that will be more long be not appropriate for.
The content of the invention
A kind of alkylation reactor and alkylation are provided the present invention be directed to the shortcoming of prior art presence, is used
More low viscous reaction liquid can be broken into the drop of very little after reactor of the present invention, make it with high-viscosity acid very
Uniformly mix in the short time, emulsify, there is provided larger liquid-liquid contact area, reaction is reached conversion ratio very high, and energy
It is enough rapidly to remove reaction heat, the low temperature environment of maintenance reaction device, while the quick separating of sour hydrocarbon two-phase be realized.
The present invention provides a kind of alkylation reactor, including cylinder and end socket, it is characterised in that：Cylinder top is sedimentation
Area, the region between cylinder bottom and end socket is reaction zone, and reaction zone lower section is mixed zone, and mixed zone is by columnar mixing
Room, feed pipe and outlet nozzle composition, mixing chamber top set outlet nozzle, and bottom sets at the top of feed pipe, mixing chamber and goes out
Mouth nozzle enters reaction zone through end socket, and 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 the cylinder dividing plate, and the cylindrical space in the middle of cylinder dividing plate is the rising area of fluid, cylinder
The annular space of dividing plate is the recirculating zone of fluid, and rising area connects up and down with recirculating zone, and decanting zone is provided with liquid rising
Sedimentation is divided into two parts by pipe, eddy flow component and cylinder baffle plate, cylinder baffle plate, cylindrical space and sedimentation in the middle of decanting zone
Annular space outside area, two parts spatially lower connection, liquid tedge and eddy flow component are located at the cylinder in the middle of decanting zone
In shape space, liquid rises bottom of the tube and is connected with the rising area of reaction zone, and liquid tedge top is connected with eddy flow component, settles
Annular space connection liquid acid outlet outside area, hydrocarbon mixture outlet, the cylinder, mixing chamber, cylinder dividing plate, cylinder gear
Plate and liquid tedge are coaxially disposed.
The present invention is further technically characterized in that：The feed pipe is respectively by alkane feed pipe and liquid acid feed pipe group
Into alkane feed pipe is located at the bottom of mixing chamber, and its axis overlaps or parallel with the axis of mixing chamber, and liquid acid feed pipe is located at
The opposite both sides in mixing chamber side, according to different mixed effects, the axis of liquid acid feed pipe can hang down with the axis of mixing chamber
Directly also can be into 20 °~60 ° angles；The axis of outlet nozzle and the diameter parallel of mixing chamber.
The present invention is further technically characterized in that：The feed pipe is respectively by alkane feed pipe and liquid acid feed pipe group
Into from bottom insertion mixing chamber, its axis overlaps alkane feed pipe with the axis of mixing chamber, 360 ° of scopes on alkane feed pipe
The aperture that aperture is 3~Φ of Φ 15 is inside disposed with, percent opening is 20%~60%, on the basis of alkane charging tube outer surface, alkane
Hydrocarbon charging pipe end is back taper, and distance of the back taper summit at the top of mixing chamber is 1~5 times of alkane feed pipe external diameter；Liquid
Sour feed pipe is located at the opposite both sides in mixing chamber side, the axis of liquid acid feed pipe can it is vertical with the axis of mixing chamber also into
20 °~60 ° angles；The axis of outlet nozzle and the diameter parallel of mixing chamber.
The present invention is further technically characterized in that：The alkene disperses sprayed feed using multiple spot, and olefin feedstocks pipe can be with
It is arranged near the outlet nozzle of mixed zone, is also disposed at the rising area and recirculating zone of reaction zone, the olefin feedstocks Guan An
During mounted in the rising area of reaction zone, using injection upwards, spray angle and reactor axis angle are 10 °~60 °；It is arranged on
During the recirculating zone of reaction zone, using injection downwards, spray angle and reactor axis angle are 10 °~60 °.
The present invention is further technically characterized in that：0.5~0.7 times of a diameter of reactor diameter of cylinder dividing plate, circle
Distance of the cylinder dividing plate top away from liquid tedge is 0.1~0.5 times of cylinder dividing plate diameter, and cylinder dividing plate bottom is undergauge knot
Structure, outlet nozzle distance of the cylinder dividing plate bottom far from mixed zone is less than injection stream length.
The present invention is further technically characterized in that：The reaction zone sets heat-exchanging tube bundle, the material by reaction zone with change
Cooling medium heat exchange in heat pipe bundle removes alkylated reaction heat；The heat-exchanging tube bundle may be provided at the rising area of reaction zone,
May be provided at the recirculating zone of reaction zone.
The present invention is further technically characterized in that：The reaction zone sets hydraulic barrier, increases rapids of the material in reaction zone
Properties of flow, it is to avoid acid hydrocarbon emulsification liquid is layered in reaction zone, the hydraulic barrier may be provided at the rising area of reaction zone, can also set
Put in the recirculating zone of reaction zone.
The present invention is further technically characterized in that：The 0.5 of a diameter of reactor diameter of cylinder baffle plate of the decanting zone~
0.8 times, cylinder baffle plate distance of the top away from eddy flow means outlet is 0.2~0.5 times of decanting zone height, cylinder baffle bottom away from
Decanting zone distance from bottom is 0.05~0.2 times of decanting zone height.
The present invention is further technically characterized in that：The top of the liquid tedge is connected with eddy flow component, and liquid rises
The cross-sectional area of pipe is 0.1~0.3 times of rising area cross-sectional area.
The present invention is further technically characterized in that：The eddy flow component has 2~6 outlets, and emulsion is entered by tedge
After entering eddy flow component, moved downward in the way of eddy flow, the larger acid of density annular space mutually outside, density is less
Hydrocarbon phase then enters middle cylindrical space, and the bottom quiescent settling that unsegregated emulsion enters decanting zone is separated, decanting zone
Volume should ensure that residence time of the liquid in decanting zone be not less than the quiet straight separation time of liquid.
The present invention also provides a kind of alkylation of use abovementioned alkyl reactor, it is characterised in that：Alkane and liquid
Body acid is entered the mixed zone mixing chamber of alkylation reactor, mixed sour hydrocarbon by alkane feed pipe and liquid acid feed pipe respectively
Emulsion sprays into reaction zone by outlet nozzle, material into flowing up after reaction zone, with the alkene entered through olefin feedstocks pipe
Mix, disperse, emulsify and be alkylated reaction, alkylation reaction product and unreacted material shape resulting mixture stream, one
Point mixture stream by after cylinder dividing plate then under be advanced into the recirculating zone of reaction zone, to recirculating zone bottom after return again it is anti-
The rising area in area is answered, is constantly circulated in reaction zone, alkylated reaction is more fully carried out, another part mixing
Logistics enters decanting zone by the liquid tedge at the top of reaction zone, and decanting zone is provided with eddy flow component, and sour hydrocarbon mixture material is by rotation
Stream component descends eddy flow to flow backward, and the centrifugal force produced using eddy flow process promotes the separation of sour hydrocarbon, and sulfuric acid content is higher, density
The annular space bottom that larger emulsion (referred to as sour phase) enters outside decanting zone, and hydrocarbon content is higher, density is less
Emulsion (referred to as hydro carbons) then enter decanting zone in the middle of cylindrical space bottom, two parts logistics the bottom of settler after
Continuous quiescent settling layering, the acid that lower floor is separate mostly as recycle acid through liquid acid outlet out, after buffered boosting,
Recycled into the liquid acid feed pipe of mixed zone, be expelled directly out device, the hydrocarbon mixture on upper strata in the form of spent acid on a small quantity
Mutually blended hydrocarbon outlet out, after vacuum flashing as cooling medium enter reaction zone in heat-exchanging tube bundle in, after heat exchange
Hydrocarbon mixture mutually enter flash tank, gas phase in flash tank enters hydrocarbon mixture surge tank after being compressed through compressor, then by mixing
Hydrocarbon pump is pumped into the alkane feed pipe of mixed zone, and the liquid phase in flash tank enters deisobutanizer, the iso-butane that tower top is isolated with
Recycle isobutane from compressor returns to hydrocarbon mixture surge tank, and bottom of towe fractionates out alkylate oil product into subsequent treatment list
Unit.
A kind of alkylation reactor and alkylation of present invention offer compared with prior art, have the following advantages that：
(1) sour hydrocarbon good mixing effect.Liquid acid catalyst is sufficiently mixed with alkane in the mixed zone of reactor, prepares sour hydrocarbon breast
Change liquid, after the emulsion enters the reaction zone of reactor, alkylate oil is generated with olefine reaction.With other alkylation process phases
Than the present invention can be such that alkane and liquid acid catalyst is sufficiently mixed, and reduce the polymerization between alkene, the alkyl of production
The quality of carburetion is higher, while acid consumption is lower.(2) reaction temperature is low.Alkylated reaction is exothermic reaction, and the present invention is using heat exchange
Tube bank removes the heat of reaction system indirectly, and by the flow and temperature of flexible modulation cryogen, control reaction to greatest extent exists
Carried out under suitable temperature conditionss.(3) to separate rapid, acid consumption low for sour hydrocarbon.The present invention realizes sour hydrocarbon two-phase using cyclone mode
It is rapidly separated, shortens the time that sour hydrocarbon is separate, reduces the secondary response of alkylate oil.Meanwhile, effluent carries acid amount and subtracts
It is few, spent acid processing cost is reduced, decrease the pollution to environment.In addition, structure of reactor design of the present invention is ingenious, liquid-
Liquid contact area is big, without mixing component, is difficult leakage, and temperature control is uniform.
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description.But it is not intended to limit the present invention
Claimed scope.
Brief description of the drawings：
Fig. 1 is a kind of alkylation reactor schematic diagram of the invention；
Fig. 2 is a kind of structural representation of mixed zone of the invention；
Fig. 3 is the structural representation of another kind mixed zone of the invention；
Fig. 4 is alkylation simple flow chart of the present invention；
Reference is shown in figure：
1- alkylation reactors；2- mixed zones；3- reaction zones；4- decanting zones；5- alkane feed pipes；6- liquid acids feed
Pipe；7- mixing chambers；8- outlet nozzles；9- olefin feedstocks pipes；10- cylinder dividing plates；11- heat-exchanging tube bundles；12- hydraulic barriers；13- liquid
Body tedge；14- cylinder baffle plates；15- eddy flow components；16- liquid acid outlets；17- hydrocarbon mixture outlets；18- pressure-reducing valves；
19- flash tanks；20- compressors；21- deisobutanizers；22- liquid acid pumps；23- hydrocarbon mixture pumps；24- liquid acid surge tanks；25-
Hydrocarbon mixture surge tank.
Specific embodiment：
Alkane, low-carbon alkene and liquid acid catalyst are fed in reactor, low-carbon alkene includes butylene, propylene, penta
Alkene or alkene mixture, preferred reaction mass are liquefied gas and the concentrated sulfuric acid after iso-butane, ether.Operating pressure be 0.3~
0.8MPa, reaction temperature be 0~20 DEG C under conditions of, realize the alkylated reaction of alkene and alkane；The alkane alkene ratio of reaction mass
It is 1: 1~15: 1, acid hydrocarbon ratio is 1: 1~5: 1.
Other involved processing steps, such as pretreatment of raw material, gas-liquid separation, reaction stream in the method for the invention
Go out the processing units such as thing pickling, alkali cleaning identical with conventional alkylation processes.The present invention is further illustrated below in conjunction with the accompanying drawings to be carried
The method of confession, but the present invention is not therefore subject to any restriction.
As shown in figure 1, a kind of alkylation reactor 1, including cylinder and end socket, it is characterised in that：Cylinder top is sedimentation
Area 4, the region between cylinder bottom and end socket is reaction zone 3, and the lower section of reaction zone 3 is mixed zone 2, as shown in Fig. 2 mixed zone 2
It is made up of columnar mixing chamber 7, feed pipe and outlet nozzle 8, the top of mixing chamber 7 sets outlet nozzle 8, bottom sets charging
Pipe, the top of mixing chamber 7 and outlet nozzle 8 enter reaction zone 3 through end socket, reaction zone 3 be provided with olefin feedstocks pipe 9, cylinder every
Reaction zone 3 is divided into two parts by plate 10, heat-exchanging tube bundle 11 and hydraulic barrier 12, the cylinder dividing plate 10, in cylinder dividing plate 10
Between cylindrical space be the rising area of fluid, the annular space of cylinder dividing plate 10 is the recirculating zone of fluid, rising area with
Recirculating zone connects up and down, and decanting zone 4 is provided with liquid tedge 13, eddy flow component 15 and cylinder baffle plate 14, and cylinder baffle plate 14 will
4 points of decanting zone is two parts, the annular space outside cylindrical space and decanting zone 4 in the middle of decanting zone 4, and two parts are spatially
Lower connection, liquid tedge 13 and eddy flow component 15 are located in the cylindrical space in the middle of decanting zone 4, the bottom of liquid tedge 13
Rising area with reaction zone 3 connects, and the top of liquid tedge 13 is connected with eddy flow component 15, the annular space outside decanting zone 4
Connection liquid acid outlet 16, hydrocarbon mixture outlet 17, the cylinder, mixing chamber 7, cylinder dividing plate 10, cylinder baffle plate 14 and liquid
Body tedge 13 is coaxially disposed.
In reaction zone 3,0.5~0.7 times of a diameter of reactor diameter of cylinder dividing plate 10, the top of cylinder dividing plate 10 is away from liquid
The distance of body tedge 13 is 0.1~0.5 times of the diameter of cylinder dividing plate 10, and the bottom of cylinder dividing plate 10 is undergauge structure, cylinder every
Distance of the bottom of plate 10 far from the outlet nozzle 8 of mixed zone 2 is less than injection stream length.The olefin feedstocks pipe 9 can be arranged in
Near the outlet nozzle 8 of mixed zone 2, the rising area and recirculating zone of reaction zone 3 are also disposed at, the olefin feedstocks pipe 9 is installed
At the rising area of reaction zone 3, using injection upwards, spray angle and reactor axis angle are 10~60 °, olefin feedstocks
When pipe 9 is arranged on the recirculating zone of reaction zone 3, using injection downwards, spray angle and reactor axis angle are 10~60 °,
Certain spray angle can promote fluid in reaction zone internal circulation flow；Cooling medium and reaction in the heat-exchanging tube bundle 11
The material-heat-exchanging in area 3 removes alkylated reaction heat；The hydraulic barrier 12 increases turbulence characteristic of the material in reaction zone 3, it is to avoid
The layering in reaction zone 3 of acid hydrocarbon emulsification liquid.The decanting zone 4 is provided with liquid tedge 13, cylinder baffle plate 14, eddy flow component
15th, liquid acid outlet 16 and hydrocarbon mixture outlet 17.4 points by decanting zone of cylinder baffle plate 14 is two parts, and middle circle is empty
Between and outside annular space, two parts spatially lower connection, 0.5~0.8 times of a diameter of barrel diameter of cylinder baffle plate 14, circle
Distance of the top of cylinder baffle plate 14 away from the outlet of eddy flow component 15 is 0.2~0.5 times of decanting zone height, and the bottom of cylinder baffle plate 14 is away from heavy
The drop distance from bottom of area 4 is 0.05~0.2 times of decanting zone height；Eddy flow component 15 is located in middle cylindrical space, eddy flow
Component 15 has 2~6 outlets, and liquid tedge 13 is connected with eddy flow component 15, and the cross-sectional area of liquid tedge 13 is upper
0.1~0.3 times of area's cross-sectional area is risen, axis overlaps with the axis of reactor.
As shown in figure 3, to open foraminate mixed zone 2 on alkane feed pipe 5, it is fed by alkane feed pipe 5, liquid acid
Pipe 6, mixing chamber 7 and outlet nozzle 8 are constituted, alkane feed pipe 5 from bottom insertion mixing chamber 7, the axis of alkane feed pipe 5 with it is mixed
Close the axis of room 7 to overlap or parallel (to overlap shown in Fig. 2), liquid acid feed pipe 6 is located at the opposite both sides in the side of mixing chamber 7,
According to different mixed effects, the axis of liquid acid feed pipe 6 can be vertical with the axis of mixing chamber 7 also into 20 °~60 ° angles, goes out
Mouth nozzle 8 is located at the top of mixing chamber 7, axis and the diameter parallel of mixing chamber 7 of nozzle 8.Cloth in the range of 360 ° on alkane feed pipe 5
The aperture that aperture is 3~Φ of Φ 15 is equipped with, percent opening is 20%~60% (on the basis of alkane charging tube outer surface), and alkane enters
The end of expects pipe 5 is back taper, back taper summit and 1~5 times that the spacing of the top exit of mixing chamber 7 is alkane feed pipe external diameter, liquid
Body acid feed pipe 6 is located at the opposite both sides in the side of mixing chamber 7, and the axis of liquid acid feed pipe 6 can be vertical with the axis of mixing chamber 7
Into 20~60 ° of angles, outlet nozzle 8 is located at the top of mixing chamber 7, nozzle-axis and the diameter parallel of mixing chamber 7.Reaction zone and sedimentation
The structure in area is same as Example 1.
As shown in figure 4, a kind of alkylation reaction method, its process is：Iso-butane and liquid acid catalyst are respectively by alkane
Feed pipe 5 and liquid acid feed pipe 6 are injected into mixing chamber 7, and two strands of materials are collided in mixing chamber 7, emulsify mixing,
The acid hydrocarbon emulsification liquid that liquid acid is continuous phase, alkane is dispersed phase is formed in mixed zone 2, mixed acid hydrocarbon emulsification liquid is by going out
Mouthful nozzle 8 sprays at a high speed reaction zone 3, material into flowing up after reaction zone 3, with the olefin feedstocks being arranged in reaction zone 3
The alkene that pipe 9 sprays quickly mixes, disperses, emulsifies, and the hydrocarbon mixture and liquid acid of alkane and alkene are made under alkylating conditions
Catalyst is contacted, so as to obtain alkylate oil.Mixed liquor is advanced into recirculating zone, liquid flowing under transferring after cylinder dividing plate 10
Rising area is returned to again after to recirculating zone bottom.The kinetic energy produced using injection makes emulsion constantly be followed in reaction zone 3
Circulation is moved, and alkylated reaction is more fully carried out.Another part emulsion (product, unreacted reactant and liquid
Body acid catalyst) decanting zone 4 is entered by the liquid tedge 13 at the top of reaction zone 3, decanting zone 4 is provided with eddy flow component 15, sour hydrocarbon
Mixed material is moved downward by the state after eddy flow component 15 rotate at high speed, because sour hydrocarbon two-phase has larger density
Difference, the centrifugal force produced during downward eddy flow using emulsion is by most sour hydrocarbon centrifugation, the larger acid of density
Annular space outside mutually entering, the less hydro carbons of density then enters middle cylindrical space, and unsegregated emulsion then enters
Enter the bottom of decanting zone 4 and continue quiescent settling layering, the volume of decanting zone 4 should ensure that residence time of the liquid in decanting zone 4 be not small
In the liquid static layering time.The acid that lower floor is separate introduces liquid acid surge tank as recycle acid through liquid acid outlet 16
24, in then pumping into the liquid acid feed pipe 6 of mixed zone 2 by liquid acid pump 22, device is expelled directly out in the form of spent acid on a small quantity.On
The mutually blended hydrocarbon outlet 17 of hydrocarbon mixture of layer enters temperature reduction after the vacuum flashing of pressure-reducing valve 18, and the hydrocarbon mixture after decompression is mutually made
In the heat-exchanging tube bundle 11 entered in reaction zone 3 for cooling medium, the hydrocarbon mixture after heat exchange mutually enters flash tank 19, in flash tank 19
Gas phase compressed through compressor 20 after enter hydrocarbon mixture surge tank 25, then pumping into mixed zone 2 alkane by hydrocarbon mixture pump 23 feeds
In pipe 5, the liquid phase in flash tank 19 enters deisobutanizer 21, iso-butane and the circulation from compressor 20 that tower top is isolated
Iso-butane returns to hydrocarbon mixture surge tank 25, and bottom of towe fractionates out alkylate oil product and enters subsequent processing units.
In the alkylation ken that possesses of art personnel, alkylation reactor of the present invention and alkylation
Can also produce various changes, and technical scheme that all do not depart from the scope of the invention and its improvement, it all should cover in this hair
In the middle of bright right.
Claims (11)
1. a kind of alkylation reactor, including cylinder and end socket, it is characterised in that：Cylinder top be decanting zone, cylinder bottom and
Region between end socket is reaction zone, and reaction zone lower section is mixed zone, and mixed zone is by columnar mixing chamber, feed pipe and outlet
Nozzle is constituted, and mixing chamber top sets outlet nozzle, and bottom sets feed pipe, and mixing chamber top and outlet nozzle enter through end socket
Enter reaction zone, reaction zone is provided with olefin feedstocks pipe, cylinder dividing plate, heat-exchanging tube bundle and hydraulic barrier, and the cylinder dividing plate will be anti-
Zoning is answered to be divided into two parts, the cylindrical space in the middle of cylinder dividing plate is the rising area of fluid, the outer annular of cylinder dividing plate is empty
Between be the recirculating zone of fluid, rising area connects up and down with recirculating zone, and decanting zone is provided with liquid tedge, eddy flow component and cylinder
Sedimentation is divided into two parts by baffle plate, cylinder baffle plate, the annular space outside cylindrical space and decanting zone in the middle of decanting zone,
Two parts spatially lower connection, liquid tedge and eddy flow component are located at the top of the cylindrical space in the middle of decanting zone, liquid
Rise bottom of the tube to be connected with the rising area of reaction zone, liquid tedge top is connected with eddy flow component, the annular outside decanting zone
Space connects liquid acid outlet and hydrocarbon mixture outlet, on the cylinder, mixing chamber, cylinder dividing plate, cylinder baffle plate and liquid
Riser is coaxially disposed.
2. a kind of alkylation reactor according to claim 1, it is characterised in that：The feed pipe by alkane feed pipe and
Liquid acid feed pipe is constituted, and alkane feed pipe is located at the bottom of mixing chamber, and its axis overlaps or parallel, liquid with the axis of mixing chamber
Body acid feed pipe is located at the opposite both sides in mixing chamber side, and its axis is vertical with the axis of mixing chamber or into 20 °~60 ° angles；
The axis of outlet nozzle and the diameter parallel of mixing chamber.
3. a kind of alkylation reactor according to claim 1, it is characterised in that：The feed pipe by alkane feed pipe and
Liquid acid feed pipe is constituted, and from bottom insertion mixing chamber, its axis overlaps alkane feed pipe with the axis of mixing chamber, and alkane enters
Be disposed with the range of 360 ° in expects pipe aperture be 3~Φ of Φ 15 aperture, percent opening be 20%~60%, with alkane feed pipe outside
On the basis of surface, alkane charging pipe end is back taper, and distance of the back taper summit at the top of mixing chamber is alkane feed pipe external diameter
1~5 times；Liquid acid feed pipe is located at the opposite both sides in mixing chamber side, and the axis of liquid acid feed pipe can be with mixing chamber
Axis is vertical or into 20~60 ° of angles；The axis of outlet nozzle and the diameter parallel of mixing chamber.
4. a kind of alkylation reactor according to claim 1, it is characterised in that：The olefin feedstocks pipe is arranged in mixing
Around the outlet nozzle in area, or the rising area or recirculating zone of reaction zone are arranged in, the olefin feedstocks pipe is arranged in reaction zone
During rising area, using injection upwards, spray angle and reactor axis angle are 10~60 °；It is arranged in the backflow of reaction zone
Qu Shi, using injection downwards, spray angle and reactor axis angle are 10~60 °.
5. a kind of alkylation reactor according to claim 1, it is characterised in that：The a diameter of reactor of cylinder dividing plate
0.5~0.7 times of diameter, distance of the cylinder dividing plate top away from liquid tedge is 0.1~0.5 times of cylinder dividing plate diameter, circle
Cylinder dividing plate bottom is undergauge structure, and outlet nozzle distance of the cylinder dividing plate bottom far from mixed zone is less than injection stream length.
6. a kind of alkylation reactor according to claim 1, it is characterised in that：The heat exchanger tube that the reaction zone is set
Beam, is arranged on the rising area or recirculating zone of reaction zone.
7. a kind of alkylation reactor according to claim 1, it is characterised in that：The baffling gear that the reaction zone is set
Plate, is arranged on the rising area of reaction zone, or reaction zone recirculating zone.
8. a kind of alkylation reactor according to claim 1, it is characterised in that：The cylinder baffle plate diameter of the decanting zone
Be 0.5~0.8 times of reactor diameter, cylinder baffle plate distance of the top away from eddy flow means outlet for decanting zone height 0.2~
0.5 times, cylinder baffle bottom is away from 0.05~0.2 times that decanting zone distance from bottom is decanting zone height.
9. a kind of alkylation reactor according to claim 1, it is characterised in that：The cross-sectional area of the liquid tedge
It is 0.1~0.3 times of rising area cross-sectional area.
10. a kind of alkylation reactor according to claim 1, it is characterised in that：The eddy flow component is provided with 2~6
Individual outlet.
The alkylation of alkylation reactor described in a kind of 11. usage right requirements 1, it is characterised in that：Alkane and liquid acid
Enter the mixed zone mixing chamber of alkylation reactor, mixed acid hydrocarbon emulsification by alkane feed pipe and liquid acid feed pipe respectively
Liquid sprays into reaction zone by outlet nozzle, material into flowing up after reaction zone, with the olefin entered through olefin feedstocks pipe,
Disperse, emulsify and be alkylated reaction, alkylation reaction product and unreacted material shape resulting mixture stream, part mixing
Logistics by after cylinder dividing plate then under be advanced into the recirculating zone of reaction zone, to recirculating zone bottom after return to reaction zone again
Rising area, constantly circulates generation alkylated reaction in reaction zone, another part mixing logistics by reaction zone at the top of
Liquid tedge enters decanting zone, and decanting zone is provided with eddy flow component, and sour hydrocarbon mixture material descends eddy flow stream backward by eddy flow component
Dynamic, the centrifugal force produced using eddy flow process separates sour hydrocarbon, and the annular space bottom that acid mutually enters outside decanting zone, hydro carbons enters
Enter the bottom of the cylindrical space in the middle of decanting zone, two parts logistics continues quiescent settling layering, lower floor in the bottom of decanting zone
Separation acid mostly as recycle acid through liquid acid outlet out, after buffered boosting, into the liquid acid of mixed zone
Recycled in feed pipe, be expelled directly out device in the form of spent acid on a small quantity, the mutually blended hydrocarbon outlet of hydrocarbon mixture on upper strata goes out
Come, in the heat-exchanging tube bundle entered in reaction zone as cooling medium after vacuum flashing, hydrocarbon mixture after heat exchange mutually enters flash distillation
Tank, the gas phase in flash tank enters hydrocarbon mixture surge tank after being compressed through compressor, then pumps into mixed zone alkane by hydrocarbon mixture pump
In feed pipe, the liquid phase in flash tank enters deisobutanizer, and the iso-butane that tower top is isolated is different with the circulation from compressor
Butane returns to hydrocarbon mixture surge tank, and bottom of towe fractionates out alkylate oil product and enters subsequent processing units.
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 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410335877.6A CN105233784B (en) | 2014-07-07 | 2014-07-07 | Alkylation reactor and alkylation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105233784A CN105233784A (en) | 2016-01-13 |
| CN105233784B true CN105233784B (en) | 2017-05-24 |
Family
ID=55031755
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410335877.6A Active CN105233784B (en) | 2014-07-07 | 2014-07-07 | Alkylation reactor and alkylation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105233784B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN110876854B (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 |
| CN111589407B (en) * | 2020-05-20 | 2022-04-12 | 中石化南京工程有限公司 | Sulfuric acid alkylation system and method for producing isooctane by using same |
| 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047811A (en) * | 1989-02-22 | 1990-12-19 | 菲利浦石油公司 | The separation of alkylation catalyst |
| WO1998031454A1 (en) * | 1997-01-21 | 1998-07-23 | Mobil Oil Corporation | Sulfuric acid alkylation reactor system with static mixers |
| CN102690375A (en) * | 2011-03-25 | 2012-09-26 | 住友化学株式会社 | Olefin polymerization reactor, polyolefin production system, and polyolefin production process |
| CN103801242A (en) * | 2012-11-03 | 2014-05-21 | 中国石油化工股份有限公司 | Reactor and alkylation reaction method using same |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR0101433B1 (en) * | 2001-04-10 | 2011-02-22 | multi-functional input method and device for downflow tubular reactor. |
-
2014
- 2014-07-07 CN CN201410335877.6A patent/CN105233784B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047811A (en) * | 1989-02-22 | 1990-12-19 | 菲利浦石油公司 | The separation of alkylation catalyst |
| WO1998031454A1 (en) * | 1997-01-21 | 1998-07-23 | Mobil Oil Corporation | Sulfuric acid alkylation reactor system with static mixers |
| CN102690375A (en) * | 2011-03-25 | 2012-09-26 | 住友化学株式会社 | Olefin polymerization reactor, polyolefin production system, and polyolefin production process |
| CN103801242A (en) * | 2012-11-03 | 2014-05-21 | 中国石油化工股份有限公司 | Reactor and alkylation reaction method using same |
Non-Patent Citations (1)
| Title |
|---|
| 离子液体催化苯与1-十二烯烷基化的循环反应-分离实验装置;乔聪震等;《化工学报》;20041231;第55卷(第12期);2038-2042 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105233784A (en) | 2016-01-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106179146B (en) | A kind of percussion flow heterophase reactor | |
| CN103357369B (en) | A kind of alkylated reaction device and method | |
| CN105219428B (en) | A kind of method of sulfuric acid alkylation reaction | |
| CN105233784B (en) | Alkylation reactor and alkylation method | |
| CN105251433B (en) | A kind of liquid acid alkylation reactor and its application process | |
| KR20140057465A (en) | Reactor and alkylation process using the reactor | |
| CN105016946B (en) | A kind of alkylation reaction method and device of the acid catalyzed isoparaffin of liquid and alkene | |
| CN105268394B (en) | Liquid acid alkylation reactor and application method thereof | |
| CN107519828A (en) | Using the alkylation and device of new micro passage reaction | |
| CN106032472B (en) | A kind of alkylation reaction method and device of liquid acid catalyzed isoparaffin and alkene | |
| EP1286938B1 (en) | Method and device for the production of alkylates | |
| CN106032349A (en) | Alkylation reaction method for isoparaffin and alkene with liquid acid for catalysis | |
| CN107523328B (en) | Alkylation process using microchannel reactor | |
| CN204656510U (en) | A kind of alkylation reactor | |
| US20230211309A1 (en) | Device and method for preparing polyalphaolefin | |
| US10077219B2 (en) | Continuous mixing reactor and method of use | |
| CN105018134A (en) | Static tube type alkylation reaction device and alkylation reaction method for liquid acid catalysis | |
| CN106732309A (en) | A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction | |
| US2438852A (en) | Multistage alkylation method | |
| US3925502A (en) | Alkylation process | |
| CN108264929A (en) | A kind of sulfuric acid alkylation method | |
| EP2332897B1 (en) | Method for producing alkylbenzene and a reactor for the sulfuric acid alkylation of isobutane with olefins | |
| CN106693875A (en) | Vertical alkylation reactor | |
| CN106943980A (en) | A kind of novel tower-type alkylated reaction device and its operating method | |
| WO2017100493A1 (en) | Reactor system for use with an ionic liquid catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |