CN106693875A - Vertical alkylation reactor - Google Patents
Vertical alkylation reactor Download PDFInfo
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- CN106693875A CN106693875A CN201710042355.0A CN201710042355A CN106693875A CN 106693875 A CN106693875 A CN 106693875A CN 201710042355 A CN201710042355 A CN 201710042355A CN 106693875 A CN106693875 A CN 106693875A
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- reactor
- inner sleeve
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- distributor
- guide shell
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00083—Coils
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1081—Alkanes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
- C10G2300/1092—C2-C4 olefins
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention aims at providing a vertical alkylation reactor which comprises a housing, guide cylinders, inner sleeves, structured packing, a sulfuric acid distributor, a liquid hydrocarbon distributor, a gas phase C4 distributor and cooling coils, wherein an acid outlet is formed in the bottom of a lower end plate of the housing; a gas outlet is formed in the upper part of an upper end plate of the housing; the gas phase C4 distributor is arranged at the lower part of the housing, and connected with a gas phase C4 inlet; at least two stages of guide cylinders and inner sleeves are sequentially arranged on the gas phase C4 distributor; the inner sleeves are only internally provided with the structured packing; the liquid hydrocarbon distributor and the structured packing are arranged in the downmost inner sleeve; the liquid hydrocarbon distributor is connected with a liquid hydrocarbon inlet; the sulfuric acid distributor is arranged at the upper part of the housing, and connected with an acid inlet; a liquid phase outlet is formed in the top of the housing; and the cooling coils are arranged between the guide cylinders and the inner sleeves in a parallel or series connection manner. With the adoption of the reactor, reaction hydrocarbon and a catalyst, namely sulfuric acid are sufficiently contacted and uniformly mixed, so that a larger liquid-liquid contact area is provided and a high conversion rate is reached.
Description
Technical field
The invention belongs to petrochemical industry, more particularly to a kind of alkylation reactor, more particularly to urged with sulfuric acid
The C4 alkane alkylation reactors of agent.
Background technology
Alkylated reaction is one of significant process of petroleum refining industry, and at present, the alkylation techniques of international mature have：
Two kinds of sulfuric acid process and hydrogen fluoride, i.e., in the presence of sulfuric acid and hydrofluoric acid catalyst, isobutane and butene reaction obtains alkyl
Carburetion.Corrosivity due to sulfuric acid and the influence to environment are smaller than hydrofluoric acid, therefore sulfuric acid process is advantageously.
Current sulfuric acid alkylation technology is substantially external monopolization, most popular U.S. DUPONT companies alkyl sodium sulfate
Change technology, the technology is horizontal eccentric contact reactor using STRATCD reactors, is internally provided with agitator arm, circulating sleeve
Cylinder and U-shaped cooling tube, circulating sleeve and cooling tube bundle are parallel to reactor wall.Acid and hydrocarbon in contact reactor interior circulation, by leaf
The strong shearing of wheel produces the turbulent closure scheme of height, and reaction heat is removed by the heat exchange with cooling tube bundle.The reactor it is anti-
Temperature is answered to be generally 6~10 DEG C.The CDAlky sulfuric acid alkylation techniques of CDTECH companies exploitation use filling filler special
The vertical tower of separate unit, filler can ensure that acid and hydrocarbon between realize good contact, it is not necessary to high energy consumption agitator.Simultaneously should
Reactor is fed using bubble point, and reaction heat is removed by the gasification of iso-butane in reactor.Both reactors all at present into
Ripe patent equipment, is at home and abroad widely used.
United States Patent (USP) US5443799 discloses a kind of alkylation reactor, and the reactor is divided into pre-mix zone and reaction zone.
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 and from premix
After the mixture stream in conjunction area enters reaction zone, because the volume of reaction zone increases suddenly, the hydrocarbon component gasification in mixture is adiabatic
Expansion absorption alkylated reaction liberated heat.The reaction temperature of the technique between 8~20 DEG C, temperature drift.
United States Patent (USP) US5785933 discloses a kind of alkylation reactor system of sulfuric acid as catalyst, in reactor
Portion makes hydro carbons and acid catalyst that mixing is formed in reactor by setting multiple injection pipeline entrances that baffle plate and tangential height are put
Stirring, so as to cancel mechanical moving element.The technology utilizes the principle design of static mixer sulfuric acid catalysis alkylated reactions
Device, but mixed effect needs further to improve.
Chinese patent CN101104570A discloses a kind of alkylation reactor, and inside reactor is one by dispersion mixing
The static mixing system of device composition.Dispersing mixer more than 50% volume regular is filled out comprising woven wire and containing void space
Material.Reactant makes gasification of hydrocarbons maintenance reaction temperature by itself pressure drop of filler.The patent is similar with US5785933, is all
Cause that sulfuric acid and hydro carbons mix using the principle of static mixer.
Patent CN105400544A discloses a kind of multiple stage circulation flow reactor, and the reactor includes housing, guide shell, interior
Sleeve, oleic acid segregation section, inner sleeve structured packing and liquid hydrocarbon distributor, due to introducing gas phase C4, the structure of reactor is caused
Gas phase C4 hydrocarbon contents in inner sleeve are far longer than the gas phase content between inner sleeve and housing, and pressure is formed inside and outside inner sleeve
Difference so that the concentrated sulfuric acid and liquid phase reacting material are moved upwards with gas phase C4 in inner sleeve, between inner sleeve and housing to
Lower circulation, forms inner loop stream.The reactor removes reaction heat in the form of C4 evaporations, and reaction temperature is 5~13 DEG C, instead
It is 1.1~2.0bar to answer pressure.
Although DUPONT sulfuric acid alkylations technology and CDAlky sulfuric acid alkylations technique are all to produce alkylate oil at present
Technology, but STRATCD reactors and filling filler special the vertical tower of separate unit be belonging respectively to DUPONT companies and
The patent equipment of CDTECH companies, domestic enterprise needs to pay certain patent fee using these reactors.Other DUPONT
Sulfuric acid alkylation technology needs to use the motor of highly energy-consuming to stir using STRATCD reactors, is fully mixed so as to reach sour hydrocarbon
The purpose of conjunction, therefore the energy consumption of the equipment is very high；The separate unit of the filling filler special that CDAlky sulfuric acid alkylation techniques are used stands
Formula tower uses special filler, and cost is very high.A kind of multiple stage circulation flow reactor has compared with above two reactor
There is a low energy consumption, the advantage of low cost, while as CDAlky sulfuric acid alkylation techniques, due to being removed in the form of C4 evaporations
Reaction heat, must be carried out at lower pressures in order to reduce side reaction, cause the treating capacity of reactor unit cross-sectional area relatively low,
The energy consumption of compressor compresses hydrocarbon gas is higher.
The content of the invention
It is an object of the invention to provide a kind of vertical alkylation reactor, the reactor can make reacted hydrocarbon and catalyst sulphur
Acid is fully contacted, and is well mixed, there is provided larger liquid liquid contact area, reaches conversion ratio high.The reactor has energy consumption low,
Reactor unit cross-sectional area treating capacity is big, and acid consumption is low, and liquid-liquid contact area is big, the features such as high conversion rate.
The present invention provides a kind of vertical alkylation on the basis of multiple stage circulation flow reactor disclosed in CN105400544A
Reactor, its primary structure is housing, guide shell, inner sleeve, inner sleeve structured packing, sulfuric acid distributor, liquid hydrocarbon distributor, gas
Phase C4 distributors and cooling coil.
Technical scheme is as follows：
A kind of vertical alkylation reactor, including housing 2, guide shell 3, inner sleeve 4, structured packing 5, sulfuric acid distributor
6th, liquid hydrocarbon distributor 7, gas phase C4 distributors 8 and cooling coil 9；The bottom of housing low head 18 sets acid outlet 10, on housing
The top of end socket 19 sets gas vent 17；The bottom of housing 2 is provided with gas phase C4 distributors 8, with gas phase C4 imports 11
It is connected；Gas phase C4 distributors 8 are disposed with least 2 grades of guide shell 3 and inner sleeve 4 above, and rule are only set inside inner sleeve 4
Whole filler 5, liquid hydrocarbon distributor 7 and structured packing 5 are internally provided with nethermost inner sleeve 4, and liquid hydrocarbon distributor 7 enters with liquid hydrocarbon
Mouth 12 is connected；The top of housing 2 is provided with sulfuric acid distributor 6, is connected with sour import 13；Case top sets liquid-phase outlet 16；, cooling
Coil pipe 9 is arranged between guide shell 3 and inner sleeve 4 in parallel or series.
Described cooling coil is arranged in parallel, and cooling coil 9 is arranged side by side between guide shell 3 and inner sleeve 4；Every layer
Cooling coil 9 is separately provided coolant inlet and outlet.
Described cooling coil is arranged in series, and one end of cooling coil is connected on the coolant inlet 14 of housing bottom,
The spiral since the guide shell 3 of bottom, through the structured packing 5 inside inner sleeve 4, structured packing 5 needs to be opened for coil pipe
Hole, into the guide shell 3 and spiral on top, untill on uppermost guide shell 3, is connected to the cooling on housing 2
Agent is exported.
Described guide shell 3 is circular table structure, and round platform bus is 45 °~60 ° with the angle α of bottom surface, upper bottom surface
Diameter is 0.3~0.6 than d/D, and the size according to reactor determines that bottom surface is recommended with the size of the gap σ and height H of housing
σ be 5~30mm, H be 50~300mm.
The described sectional area of inner sleeve 4 is 0.25~0.75 with the ratio of housing section product, and ratio of height to diameter is 5~20, quantity
Between 2~10, guide shell 3 and the arranged for interval of inner sleeve 4, the number of guide shell 3 add 1 for the number of inner sleeve 4.
Multistage structured packing 5 is placed in the described inside of inner sleeve 4, and the height of structured packing 5 is the 0.05 of the height of inner sleeve 4
~0.2 times, adjacent two pieces of structured packings interlock 90 ° and place.
Described liquid hydrocarbon distributor 7 uses shower nozzle type liquid distribution trough, shower nozzle to be provided with upwardsAperture, open
Porosity is 20%~60%.
The porous gas explosion head that described gas phase C4 distributors 8 are made of metal sintering, aperture 1 μm~100 μm it
Between.
Described sulfuric acid distributor 6 uses calandria liquid distributors, comb to be provided with downwardsAperture, often put down
Square rice reactor enclosure body section is provided with 100~600 holes.
The caliber of described cooling coil 9 can in parallel or series be arranged in guide shell in DN15~DN20, cooling coil 9
Between 3 and inner sleeve 4.When cooling coil is to be arranged in series, structured packing 5 needs to be coil pipe perforate, sees accompanying drawing 4.
Reactor proposed by the present invention is applied to alkylated reaction, is particularly well-suited to the C4 alkylation systems that sulfuric acid is catalyst
The reaction of alkylate oil.The reactor has energy consumption low, and reactor unit cross-sectional area treating capacity is big, and acid consumes low, liquid-liquid contact face
Product is big, the features such as high conversion rate.
Brief description of the drawings
Fig. 1 is vertical alkylation reactor structure chart A of the invention
Fig. 2 is vertical alkylation reactor structure chart B of the invention.
Fig. 3 is guide shell facade view.
Fig. 4 is structured packing perforate top view.
Fig. 5 is process chart of the vertical alkylation reactor of the invention in alkylation process
Wherein：The vertical alkylation reactors of 1-；2- housings；3- guide shells；4- inner sleeves；5- structured packings；6- sulfuric acid point
Cloth device；7- liquid hydrocarbon distributors；8- gas phase C4 distributors；9- cooling coils；10- acid outlets；11- gas phase C4 imports；12- liquid hydrocarbons enter
Mouthful；13- acid imports；14- coolant inlets；15- coolant outlets；16- liquid-phase outlets；Sealed under 17- gaseous phase outlet 18- housings
Head；19- housing upper covers；20- compressors；21- flash tanks；22- acid settlers；23- acid circulating pumps.
Specific embodiment
It is described in detail below in conjunction with the accompanying drawings：
Such as Fig. 1 and Fig. 2, a kind of vertical alkylation reactor 1 in the present invention, including housing 2, guide shell 3, inner sleeve 4, rule
Whole filler 5, sulfuric acid distributor 6, liquid hydrocarbon distributor 7, gas phase C4 distributors 8 and cooling coil 9 are constituted.
With reference to shown in accompanying drawing 1 and Fig. 2, the bottom of housing low head 18 sets acid outlet 10, the top of housing upper cover 19
Gas vent 17 is set；Gas phase C4 imports 11 are located at the bottom of housing 2, and are connected with gas phase C4 distributors 8；Gas phase C4 imports 11
The above is guide shell 3 and inner sleeve 4, and structured packing 5 is placed in the inside of inner sleeve 4, and the middle and lower part of housing 2 is provided with liquid hydrocarbon import 12, liquid
Hydrocarbon import 12 is connected in the inside of inner sleeve 4 with liquid hydrocarbon distributor 7；The top of housing 2 is provided with sour import 13, and with sulfuric acid distributor 6
It is connected；It is provided for removing the cooling coil 9 of reaction heat inside guide shell 3 and inner sleeve 4；Case top sets liquid-phase outlet
16。
Guide shell 3 as described in Figure 3 is circular table structure, and round platform bus is 45 °~60 °, upper bottom with the angle α of bottom surface
The diameter in face is 0.3~0.6 than d/D, and bottom surface is 5~30mm with the gap σ of housing, and height H is 50~300mm, preferably 100
~200mm.
The described sectional area of inner sleeve 4 is 0.25~0.75 with the ratio of housing section product, and ratio of height to diameter is 5~20, preferably
10~15, between 2~10, preferably 3~6, the number of guide shell 4 Jia 1 to quantity for inner sleeve number 3, guide shell 3 and interior
Sleeve 4 is spaced apart.
Multistage structured packing 5 is placed in the described inside of inner sleeve 4, and the height of structured packing 5 is the 0.05 of inner sleeve height
~0.2 times, adjacent two pieces of structured packings interlock 90 ° and place.
Described liquid hydrocarbon distributor 7 uses shower nozzle type liquid distribution trough, shower nozzle to be provided with upwardsAperture, open
Porosity is 20%~60%.
The porous gas explosion head that described gas phase C4 distributors 8 are made of metal sintering, aperture 1 μm~100 μm it
Between, preferably 20 μm~50 μm.
Described sulfuric acid distributor 6 uses calandria liquid distributors, comb to be provided with downwardsAperture, often put down
Square rice reactor enclosure body section is provided with 100~600 holes.
In DN15~DN20, cooling coil as shown in Figure 19 is arranged in parallel at guide shell 3 to the caliber of described cooling coil 9
And inner sleeve 4 between, cooling coil 9 is arranged in series in inside guide shell 3 and inner sleeve 4 as described in Figure 2, now structured packing 5
Need to be coil pipe perforate, see accompanying drawing 4.
As shown in figure 5, a kind of process chart of the vertical alkylation reactor of the present invention in alkylation process, C4 alkane
Reactor middle and lower part is mixed into proportion with C4 alkene, and under the catalytic action of the concentrated sulfuric acid, operation temperature is -3~10 DEG C, behaviour
Make pressure for 0.3~0.7MPa, realize alkylated reaction, the alkane alkene ratio of liquid hydrocarbon charging is 5~20, and acid hydrocarbon ratio is 0.5~2.
The application method of vertical alkylation reactor is further illustrated with reference to Fig. 5.
C4 alkane and C4 alkene enter liquid hydrocarbon charging aperture 12 together in certain proportion, and liquid hydrocarbon enters by liquid hydrocarbon distributor 7
Row distribution；Gas phase C4 is distributed by gas phase C4 imports 11 in gas phase C4 distributors 8；The catalyst concentrated sulfuric acid is entered by sour import 13
Enter reactor and the distribution in acid spreader 6；From the gas phase C4 out of gas phase C4 distributors 8, motion is upwards, in guide shell 3
The central area of housing cross-sectional is gathered under effect, it is ensured that gas phase C4 is most of into the inside of inner sleeve 4；Due to gas phase
C4 major parts are all present in the inside of inner sleeve 4, and the gas holdup of the interior or exterior space of inner sleeve 4 is different, causes inner sleeve 4 and housing 2
Between sulfuric acid and liquid hydrocarbon to the internal motion of inner sleeve 4, i.e., internal circulation so increases contact of the liquid hydrocarbon with sulfuric acid, and increase is instead
Between seasonable, gas carries liquid hydrocarbon and sulfuric acid is moved upwards in inner sleeve 4, is cut by structured packing 5, disperseed so that sulfuric acid and
Liquid hydrocarbon is fully contacted well mixed, realizes alkylated reaction, produces alkylate oil, and the reaction heat of generation is carried by cooling coil 9
Go out reactor；Gas phase C4 is continued up from gas phase C4 outlets 17 and is entered compressor 20, and reactor bottom acid outlet 10 is produced
Acid and liquid-phase outlet 16 extraction liquid phase enter acid settler 22, acid settler lower floor for acid returned by acid circulating pump 23
To sour import 13, a part is produced as spent acid, and the upper oil phase of acid settler enters flash tank 21, what flash tank 21 was flashed off
Gas phase enters compressor 20, and subsequent cell is entered after being compressed together with top gaseous phase C4, and the liquid phase of flash tank 21 enters de- iso-butane
The subsequent cells such as tower are until obtain alkylation products.
The concrete operations parameter of embodiment 1~3 is shown in Table 1.
Example described above is only to absolutely prove preferred embodiment that is of the invention and being lifted, and protection scope of the present invention is not
It is limited to this.Equivalent substitute or conversion that those skilled in the art are made on the basis of the present invention, in guarantor of the invention
Within the scope of shield.Protection scope of the present invention is defined by claims.
Claims (10)
1. a kind of vertical alkylation reactor, including housing 2, guide shell 3, inner sleeve 4, structured packing 5, sulfuric acid distributor 6,
Liquid hydrocarbon distributor 7, gas phase C4 distributors 8 and cooling coil 9；It is characterized in that the bottom of housing low head 18 sets acid outlet 10,
The top of housing upper cover 19 sets gas vent 17；The bottom of housing 2 is provided with gas phase C4 distributors 8, enters with gas phase C4
11, mouth is connected；Gas phase C4 distributors 8 are disposed with least 2 grades of guide shell 3 and inner sleeve 4 above, inside inner sleeve 4 only
Structured packing 5 is set, liquid hydrocarbon distributor 7 and structured packing 5 is internally provided with nethermost inner sleeve 4, liquid hydrocarbon distributor 7 with
Liquid hydrocarbon import 12 is connected；The top of housing 2 is provided with sulfuric acid distributor 6, is connected with sour import 13；Case top sets liquid-phase outlet
16；, cooling coil 9 is arranged between guide shell 3 and inner sleeve 4 in parallel or series.
2. reactor as claimed in claim 1, it is characterized in that described cooling coil is arranged in parallel, cooling coil 9 is simultaneously arranged
Put between guide shell 3 and inner sleeve 4；Every layer of cooling coil 9 is separately provided coolant inlet and outlet.
3. reactor as claimed in claim 1, it is characterized in that cooling coil is arranged in series, one end of cooling coil is connected to shell
On the coolant inlet 14 of body bottom, the spiral since the guide shell 3 of bottom, the structured packing through inside inner sleeve 4
5, structured packing 5 needs to be coil pipe perforate, into the guide shell 3 and spiral on top, until being on uppermost guide shell 3
Only, it is connected to the coolant outlet on housing 2.
4. reactor as claimed in claim 1, it is characterized in that described guide shell 3 is circular table structure, round platform bus and bottom
The angle α in face is 45 °~60 °, and the diameter of upper bottom surface is 0.3~0.6 than d/D, and the size according to reactor determines bottom surface
The σ recommended with the size of the gap σ and height H of housing is 5~30mm, and H is 50~300mm.
5. reactor as claimed in claim 1, it is characterized in that the ratio of the sectional area of inner sleeve 4 and housing section product for 0.25~
0.75, ratio of height to diameter is 5~20, quantity between 2~10, guide shell 3 and the arranged for interval of inner sleeve 4, the number of guide shell 3 is
The number of inner sleeve 4 adds 1.
6. reactor as claimed in claim 1, it is characterized in that multistage structured packing 5 is placed in the described inside of inner sleeve 4, it is regular
The height of filler 5 is 0.05~0.2 times of the height of inner sleeve 4, and adjacent two pieces of structured packings interlock 90 ° and place.
7. reactor as claimed in claim 1, it is characterized in that described liquid hydrocarbon distributor 7 uses shower nozzle type liquid distribution trough,
Shower nozzle is provided with upwardsAperture, percent opening is 20%~60%.
8. reactor as claimed in claim 1, it is characterized in that described gas phase C4 distributors 8 using metal sintering be made it is many
Permeability gas explosion head, aperture is between 1 μm~100 μm.
9. reactor as claimed in claim 1, it is characterized in that described sulfuric acid distributor 6 uses calandria liquid distributors,
Comb is provided with downwardsAperture, be provided with 100~600 holes per square meter of reactor housing section.
10. reactor as claimed in claim 1, it is characterized in that the caliber of described cooling coil 9 is in DN15~DN20.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710042355.0A CN106693875A (en) | 2017-01-20 | 2017-01-20 | Vertical alkylation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710042355.0A CN106693875A (en) | 2017-01-20 | 2017-01-20 | Vertical alkylation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106693875A true CN106693875A (en) | 2017-05-24 |
Family
ID=58909979
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710042355.0A Pending CN106693875A (en) | 2017-01-20 | 2017-01-20 | Vertical alkylation reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111111566A (en) * | 2019-12-27 | 2020-05-08 | 江苏奥克化学有限公司 | Packed tower reactor for producing cyclic carbonate and production method |
| CN111249999A (en) * | 2018-11-30 | 2020-06-09 | 中国科学院大连化学物理研究所 | Fixed bed reactor for catalytic reduction of hexavalent uranium by hydrazine nitrate and application |
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| CN102921369A (en) * | 2012-11-28 | 2013-02-13 | 宁夏宝塔石化集团有限公司 | Novel alkylation stirring reactor of horizontal type built-in heat exchanging pipe |
| CN204159342U (en) * | 2014-10-10 | 2015-02-18 | 中石化洛阳工程有限公司 | A kind of alkylation reactor |
| CN105400544A (en) * | 2015-12-03 | 2016-03-16 | 天津如有科技有限公司 | Method for preparing alkylate oil by using multistage circulating flow reactor |
| CN206535555U (en) * | 2017-01-20 | 2017-10-03 | 天津大学 | A kind of vertical alkylation reactor |
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2017
- 2017-01-20 CN CN201710042355.0A patent/CN106693875A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102921369A (en) * | 2012-11-28 | 2013-02-13 | 宁夏宝塔石化集团有限公司 | Novel alkylation stirring reactor of horizontal type built-in heat exchanging pipe |
| CN204159342U (en) * | 2014-10-10 | 2015-02-18 | 中石化洛阳工程有限公司 | A kind of alkylation reactor |
| CN105400544A (en) * | 2015-12-03 | 2016-03-16 | 天津如有科技有限公司 | Method for preparing alkylate oil by using multistage circulating flow reactor |
| CN206535555U (en) * | 2017-01-20 | 2017-10-03 | 天津大学 | A kind of vertical alkylation reactor |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111249999A (en) * | 2018-11-30 | 2020-06-09 | 中国科学院大连化学物理研究所 | Fixed bed reactor for catalytic reduction of hexavalent uranium by hydrazine nitrate and application |
| CN111111566A (en) * | 2019-12-27 | 2020-05-08 | 江苏奥克化学有限公司 | Packed tower reactor for producing cyclic carbonate and production method |
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