CN106732309A - A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction - Google Patents
A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction Download PDFInfo
- Publication number
- CN106732309A CN106732309A CN201710028166.8A CN201710028166A CN106732309A CN 106732309 A CN106732309 A CN 106732309A CN 201710028166 A CN201710028166 A CN 201710028166A CN 106732309 A CN106732309 A CN 106732309A
- Authority
- CN
- China
- Prior art keywords
- reaction
- reactor
- tubulation
- injecting type
- type shell
- 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.)
- Granted
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 112
- 238000000034 method Methods 0.000 title claims abstract description 16
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000000945 filler Substances 0.000 claims abstract description 27
- 230000008016 vaporization Effects 0.000 claims abstract description 22
- 239000001282 iso-butane Substances 0.000 claims abstract description 19
- 235000013847 iso-butane Nutrition 0.000 claims abstract description 19
- 238000009834 vaporization Methods 0.000 claims abstract description 18
- -1 alkane alkene Chemical class 0.000 claims abstract description 13
- 230000009471 action Effects 0.000 claims abstract description 12
- 230000000694 effects Effects 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims description 30
- 229930195733 hydrocarbon Natural products 0.000 claims description 30
- 150000002430 hydrocarbons Chemical class 0.000 claims description 30
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 25
- 238000000605 extraction Methods 0.000 claims description 23
- 239000000463 material Substances 0.000 claims description 18
- 239000002253 acid Substances 0.000 claims description 17
- 238000012856 packing Methods 0.000 claims description 9
- 238000006555 catalytic reaction Methods 0.000 claims description 8
- 238000009826 distribution Methods 0.000 claims description 6
- 239000000839 emulsion Substances 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 210000004534 cecum Anatomy 0.000 claims description 3
- 150000004965 peroxy acids Chemical class 0.000 claims description 3
- 238000007747 plating Methods 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 238000012545 processing Methods 0.000 claims description 2
- 229910001220 stainless steel Inorganic materials 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 abstract description 4
- 238000002347 injection Methods 0.000 abstract description 2
- 239000007924 injection Substances 0.000 abstract description 2
- 238000005804 alkylation reaction Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 4
- 230000029936 alkylation Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 239000002826 coolant Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 3
- UHZZMRAGKVHANO-UHFFFAOYSA-M chlormequat chloride Chemical compound [Cl-].C[N+](C)(C)CCCl UHZZMRAGKVHANO-UHFFFAOYSA-M 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000007171 acid catalysis Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- 239000001117 sulphuric acid Substances 0.000 description 2
- 208000012826 adjustment disease Diseases 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Classifications
-
- 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
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/56—Addition to acyclic hydrocarbons
- C07C2/58—Catalytic processes
- C07C2/62—Catalytic processes with acids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/02—Sulfur, selenium or tellurium; Compounds thereof
- C07C2527/03—Acids of sulfur other than sulfhydric acid or sulfuric acid, e.g. halosulfonic acids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction, reactor of the invention includes vertical reactor cylinder, upper cover, low head, upper perforated plate and lower supporting plate, wherein, reaction zone is constituted between upper perforated plate and lower supporting plate, vaporization Disengagement zone is constituted between lower supporting plate and low head, it is dispersed with vertically in reaction zone on every tubulation tube wall of many tubulations and aperture is distributed with, upper perforated plate is provided with circular hole, circular hole aperture is identical with tubulation caliber, in reaction zone, tubulation outside is filled with filler.Shear action with filler is acted on by the small hole injection of tubulation, being sufficiently mixed for reaction mass is capable of achieving；Heat is taken by the way that unreacted iso-butane is vaporized, and the mode of Posterior circle to reactor feed is cooled down through overcompression, both ensure that reaction is carried out under the conditions of low temperature, suitable alkane alkene ratio, turn avoid because being brought using indirect cooling method the problems such as taking refrigerant, the leakage of refrigerant that thermal effect is poor, introducing is new.
Description
Technical field
It is anti-the present invention relates to alkylated reaction technical field, more particularly to a kind of injecting type tubulation for alkylated reaction
Answer device and its reaction method.
Background technology
The alkylate oil produced under sulphuric acid catalysis effect by low-carbon alkene and iso-butane, with octane number higher,
It is preferable gasoline blend component.But because reaction raw materials iso-butane is poor with the intersolubility of the catalyst concentrated sulfuric acid, reaction raw materials
Mixed effect with the catalyst concentrated sulfuric acid turns into one of key influence factor of alkylated reaction.Additionally, alkylated reaction is to put
Thermal response, if reaction heat can not be removed timely and effectively, will aggravate the generation of olefinic polymerization side reaction, therefore, alkyl sodium sulfate
Chemical industry skill should realize that sour hydrocarbon two-phase is sufficiently mixed, and ensure that alkylated reaction is carried out at constant relatively low temperature again.It is existing
Alkylation reactor species mainly including injection-type reactor, stirring reactor, packed column reactor etc..
Patent US5443799 discloses a kind of alkylation reactor, and the reactor is divided into pre-mix zone and reaction zone.Anti-
The pre-mix zone of device, iso-butane is answered to be sprayed via injector and be mixed to form emulsion with sulfuric acid, alkene is in reaction zone and from pre-
The emulsion of mixed zone inversely reacted by contact.Reaction zone volume is significantly greater than the premix of pre-mix zone, iso-butane and sulfuric acid
After compound enters reaction zone, volume increases suddenly, and adiabatic expansion absorbs alkylated reaction liberated heat.The reaction of the reactor
Temperature can only be controlled at 8~20 DEG C, and reaction temperature is higher.
Patent US3759318 discloses a kind of Horizontal stirring reactor, and reaction raw materials are entered at reactor impeller, in impeller
Strong stirring under formed acid hydrocarbon emulsification liquid.Emulsion is contacted with the heat-exchanging tube bundle of inside reactor, and the cooling of heat-exchanging tube bundle is situated between
Matter takes alkylated reaction heat away.Stratco Horizontal stirrings reactor is largely industrialized, but the scale of single reactor has
Limit, expanding the scale of production can only rely on the increase of reactor quantity.
Patent specification CN101104570A discloses a kind of alkylation reactor, and inside reactor is one mixed by dispersion
The static mixing system of clutch composition.Dispersing mixer includes woven wire contact with containing void space more than 50% volume
The filler of property structure.Reaction mass relies on filler itself pressure drop, light hydrocarbon component is gasified, and consumes reaction heat.And the reactor
Structure construction is complicated, relatively costly.
Patent CN103357369A discloses a kind of structured packing alkylated reaction device with cavity structure, and reaction is former
Material enters reactor by liquid distribution device, and the cavity two ends of filler are provided with coolant distribution pipe, cavity in reactor
Interior formation heat transfer zone, forms reaction zone between cavity and cavity, reaction zone and heat transfer zone arrange in reactor radially alternating, and reaction
Area and heat transfer zone are not communicated with, reaction mass enter reaction zone after under the cutting of structured packing, peptizaiton, sour hydrocarbon is carried out fully
Mixing, reaction heat is taken away by cooling medium.The method needs to introduce new cooling medium, and exists because of cooling medium leakage
Have a strong impact on the risk of reaction effect.
The content of the invention
It is anti-a kind of injecting type tubulation for alkylated reaction to be provided it is an object of the invention to be directed to above-mentioned deficiency
Answer device and its reaction method.
To solve above technical problem, the technical solution adopted by the present invention is：A kind of injecting type for alkylated reaction
Shell-and-tube reactor, including a vertical reactor cylinder, the upper and lower end socket being connected with the vertical reactor cylinder are arranged at
The upper perforated plate and lower supporting plate of the vertical reactor inner barrel, reaction zone is constituted between the upper perforated plate and lower supporting plate,
Vaporization Disengagement zone is constituted between lower supporting plate and low head, circular hole is offered on the upper perforated plate, in the reaction zone vertically
Many tubulations are distributed with, aperture is distributed with the tube wall of the tubulation, the caliber of the aperture of circular hole and tubulation on the upper perforated plate
Identical, described tubulation one end is connected and communicates with the circular hole of upper perforated plate, and the other end is cecum, is connected with the lower supporting plate
Fixed, the tubulation outside in the reaction zone is filled with filler, and charging aperture, the reaction zone are provided with the top of the upper cover
Interior vertical reactor cylinder side is provided with side entry feed mouthful, is provided with gas phase on the top cylinder of the vaporization Disengagement zone and adopts
Outlet, bottom is provided with side take-off mouthful, and extraction mouth in bottom is provided with the low head.
Further, the regularity of distribution of aperture is that top is close on the tubulation tube wall, and bottom is sparse.Alkylated reaction is main
The top half of reaction zone is concentrated on, with the carrying out of reaction, closer to reaction zone outlet, alkylated reaction gradually slows down, root
There is severe degree according to reaction, material is carried out reasonable disposition.
Further, the vertical reactor cylinder side in the reaction zone is disposed with multiple side lines and enters from top to bottom
Material mouth, can be by adjusting the inlet amount and feed composition of diverse location side entry feed mouthful, in time, effectively adjustment reaction alkane alkene
Than, it is ensured that the alkane alkene ratio of whole conversion zone is in controlled range.
Further, the lower supporting plate is made up of multiple layer metal silk screen and grid, and filler and tubulation can either be played
Support and fixation, can make reacting rear material smoothly enter vaporization Disengagement zone again.
Further, the filler in the reaction zone is preferably polypropylene or stainless steel cloth filler, naturally it is also possible to be
Other fillers, are not limited thereof here.
Further, the bottom in the vaporization Disengagement zone is provided with filler, described filler be corrugated plate regular packing or
Corrugated plating random packing or inclined plate packing.
In reactor of the invention, upper cover forms semi-enclosed space with upper perforated plate, and the concentrated sulfuric acid at the top of upper cover by entering
Material mouth is entered into reactor through its top feed line, is flowed along tubulation by the small sircle hole of upper perforated plate, in certain pressure effect
Under, equably it is ejected into reaction zone by the aperture on tubulation tube wall, and entered through side entry feed line by side entry feed mouthful
Total hydrocarbon feed, under the shear action of filler, forms mixed solution and with the generation of alkylated reaction.Due to cutting for filler
Cut the jet-action with tubulation so that whole inside reactor forms numerous small-sized turbulent flow, has reached material well-mixed
Effect.
During the course of the reaction, most of iso-butane is vaporized under differential pressure action, sponges reaction liberated heat, makes reaction
Carry out at a lower temperature.
Gas phase iso-butane by vaporize Disengagement zone gas phase extraction mouth produce, through overcompression cooling treatment after, through hydrocarbon circular route
Reactor pump-around charging aperture is looped back, is recycled and for adjusting reaction alkane alkene ratio.
Vaporization Disengagement zone bottom is filled with the multi_layer extraction of sour hydrocarbon in product after filler can accelerate to react.Most of sulfuric acid leads to
Reactor bottom extraction mouth extraction is crossed, and reactor head charging aperture is looped back through sour circular route, a small amount of spent acid is through waste discharge acid
Line enters aftertreatment device；Hydrocarbon material after layering is produced by side take-off mouthful through producing line, is then fed into subsequent products
Separator.
Present invention also offers a kind of method for being alkylated reaction using above-mentioned injecting type shell-and-tube reactor, including with
Lower step:
(1) concentrated sulfuric acid is entered into the injecting type shell-and-tube reactor by its top feed mouthful of the upper cover, and is passed through
The circular hole for crossing upper perforated plate flows along tubulation；
(2) under certain pressure effect, equably it is ejected into reaction zone by the aperture on the tubulation tube wall, and with
By the total hydrocarbon feed of side entry feed mouthful entrance under the shear action of filler, form sour hydrocarbon emulsion and simultaneously complete catalytic reaction；By
In the shearing and the jet-action of tubulation of filler so that whole inside reactor forms small-sized turbulent flow, enhances material and catalysis
Being fully contacted for agent, reduces the generation of side reaction so that reaction has acid consumption low, the obvious advantage such as effect is good；
(3) complete the product after catalytic reaction and reaction vaporization Disengagement zone is entered under differential pressure action in reactor, wherein,
Gas phase iso-butane is produced by the gas phase extraction mouth for vaporizing Disengagement zone；
(4) reacted most of sulfuric acid produces mouth and produces by the bottom of low head, and is looped back through peracid circular route
To upper cover charging aperture, a small amount of spent acid enters follow-up processing unit through waste discharge acid line, and the hydrocarbon material after layering is by side take-off
Follow-up product separator is sent into after mouth extraction.
Preferably, in step (2), catalytic reaction temperature is controlled at -3~4 DEG C.
Further, after also including the gas phase iso-butane that will be produced through overcompression cooling treatment after step (2), followed through hydrocarbon
Loop wire loops back reactor pump-around charging aperture, and it is 8 to control reaction alkane alkene mass ratio：1~10：1.
Preferably, the volume ratio of reaction acid hydrocarbon is 0.8：1~2：1, reaction zone top pressure is controlled for 350~400KPa,
Reaction zone outlet pressure is 3.5~8.5KPa, using method of the present invention reaction raw materials butene conversion up to 100%, product
Up to 93~97, sour consumption is 10~50kg/t to octane number.
In sum, with technical scheme, have the advantages that：Injecting type tubulation reaction of the invention
Device structure design is simple, and cost is low；Shear action with filler is acted on by the small hole injection of tubulation, reactant is capable of achieving
That expects is sufficiently mixed；Heat is taken by taking to be vaporized unreacted iso-butane, and through overcompression cooling Posterior circle to reaction
The mode of device charging, both ensure that reaction is carried out under the conditions of low temperature, suitable alkane alkene ratio, turn avoid because using cooling indirectly
Thermal effect is poor for method and taking of bringing, the problems such as introduce new refrigerant, leakage of refrigerant；Alkylation reaction method acid consumption
Low, product octane number is high, quality better.
Brief description of the drawings
Fig. 1 is the structural representation of reactor of the present invention；
Fig. 2 is reactor cross section schematic diagram of the present invention；
Fig. 3 is tubulation structural representation of the invention；
Fig. 4 is schematic flow sheet of the invention.
In accompanying drawing：1 reactor shell, 2 upper covers, 3 low heads, 4 upper perforated plates, 5 lower supporting plates, 6 its top feeds mouthful, 7 sides
Line charging aperture, 8 gas phases extraction mouth, 9 side take-offs mouthful, 10 bottoms extraction mouth, 11 tubulations, 201 side entry feed lines, 202 tops are entered
Stockline, 203 hydrocarbon circular routes, 204 sour circular routes, 205 waste discharges acid line, 206 extraction lines
Specific embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation is described, but does not constitute limiting the scope of the invention.
With reference to Fig. 1,2,3, in the present embodiment, the present invention is with diameter 4200mm, the alkylation reactor of height 5500mm
As a example by, including vertical reactor cylinder 1, upper cover 2, low head 3, upper perforated plate 4 and lower supporting plate 5.
Wherein, reaction zone is constituted between upper perforated plate 4 and lower supporting plate 5, vaporization is constituted between lower supporting plate 4 and low head 3
Disengagement zone.
8800 tubulations 11 are uniformly distributed vertically in reaction zone, aperture is distributed with the every tube wall of tubulation 11, aperture
The regularity of distribution is that top is close, and bottom is sparse, and aperture is 3mm.
Upper perforated plate 4 is provided with 8800 small sircle holes in equilateral triangle distribution, and small sircle hole aperture is identical with the caliber of tubulation 11
It is 25mm.The one end of tubulation 11 is connected and communicates with the small sircle hole of upper perforated plate 4, and the other end of tubulation 11 is cecum, with lower support
Plate 5 is connected.
In reaction zone, wire packing of the outside of tubulation 11 filled with polypropylene material.In the upper cover of reactor shell 1
2 are provided with its top feed mouthful 6, and 3 side entry feeds mouthful 7 are provided with the reactor shell 4 below reaction zone inner upper tube plate 4,
Vaporization Disengagement zone includes that gas phase produces mouth 8, side take-off mouthful 9 and bottom extraction mouth 10.
Corrugated plating random packing is filled with vaporization Disengagement zone bottom, the ratio that vaporization Disengagement zone accounts for reactor volume is
40%.
Concentrated sulfuric acid catalyst is entered into reactor by its top feed mouthful of upper cover, total hydrocarbon feed is by side entry feed
Mouth enters reactor, and in the presence of tubulation aperture and filler, sour hydrocarbon material is realized being sufficiently mixed under turbulence state, mixing
N-butene and iso-butane in hydrocarbon feed react generation iso-butane product in the catalytic action of sulfuric acid.During the course of the reaction, big portion
The iso-butane for having neither part nor lot in reaction is divided to be vaporized under differential pressure action, absorbing reaction liberated heat, gas phase iso-butane is separated by vaporization
The gas phase extraction mouth extraction in area, after being processed through overcompression cooling system, returns reactor pump-around and feeds by pump circulation.Reacting rear material
By realizing sour hydrocarbon multi_layer extraction in vaporization Disengagement zone bottom after reaction zone, most of sulfuric acid is produced into mouth by reactor bottom
Extraction, reactor head charging aperture is returned by pump circulation, and a small amount of acid enters Waste acid treating device.
Refer to the attached drawing 4, alkylation reaction method of the invention is as follows：In above-mentioned injecting type shell-and-tube reactor, the concentrated sulfuric acid
Entered into reactor through its top feed line 202 by its top feed mouthful 6 of upper cover 2, by the small sircle hole of upper perforated plate 4 along row
Pipe 11 flows, and under certain pressure effect, is equably ejected into reaction zone by the aperture on the tube wall of tubulation 11, and by side line
The total hydrocarbon feed that charging aperture 7 enters through side entry feed line 201, under the shear action of filler, forms sour hydrocarbon emulsion and completes
Catalytic reaction.Due to the shearing and the jet-action of tubulation of filler so that whole inside reactor forms small-sized turbulent flow, enhances
Being fully contacted for material and catalyst, reduces the generation of side reaction so that reaction has acid consumption low, and effect waits well substantially excellent
Point.
During the course of the reaction, most of iso-butane is vaporized under differential pressure action, and controlling reaction temperature is -3~4 DEG C.
Product enters into reaction vaporization Disengagement zone under differential pressure action in reactor after reaction.Gas phase iso-butane is by vaporizing
Disengagement zone gas phase extraction mouth 8 produce, through overcompression cooling treatment after, through hydrocarbon circular route 203 loop back reactor pump-around feed
Mouth 7, by reconciling the inlet amount and feed composition of diverse location side entry feed mouthful 7, in time, efficiently controls whole conversion zone
Alkane alkene mass ratio, preferred alkane alkene mass ratio is 8：1~10：1.
Vaporization Disengagement zone bottom is filled with the multi_layer extraction of sour hydrocarbon in product after filler can accelerate to react.Most of sulfuric acid leads to
After crossing the reactor bottom extraction extraction of mouth 10, reactor head charging aperture 6, a small amount of spent acid are looped back through peracid circular route 204
Aftertreatment device is entered through waste discharge acid line 205.Hydrocarbon material after layering by after the extraction of side take-off mouthful 9 by producing line 206
Feeding subsequent products separator.
Reaction acid hydrocarbon volume ratio of the invention is 0.8：1~2.0：1, reaction zone top pressure is controlled for 350~450KPa,
Reaction zone outlet pressure is 3.5~8.5KPa, using method of the present invention reaction raw materials butene conversion up to 100%, product
Up to 93~97, sour consumption is 10~50kg/t to octane number.
Specific embodiment and experimental data see the table below 1
Wherein, sulphuric acid catalysis agent concentration is 98%, and total hydrocarbon feed inlet amount is 23t/h, and wherein butene concentration is
34.5%, concentration of isobutane is 42.2%.
Table 1
The above is the preferred embodiment of the present invention, it is noted that for those skilled in the art
For, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications are also considered as
Protection scope of the present invention.
Claims (10)
1. a kind of injecting type shell-and-tube reactor for alkylated reaction, an including vertical reactor cylinder is vertical with described
The upper and lower end socket of reactor shell connection, is arranged at the upper perforated plate and lower supporting plate of the vertical reactor inner barrel, and it is special
Levy and be：Reaction zone is constituted between the upper perforated plate and lower supporting plate, vaporization Disengagement zone is constituted between lower supporting plate and low head,
Circular hole is offered on the upper perforated plate, many tubulations are distributed with vertically in the reaction zone, be distributed on the tube wall of the tubulation
There is aperture, the aperture of circular hole and the caliber of tubulation are identical on the upper perforated plate, described tubulation one end is connected with the circular hole of upper perforated plate
Fix and communicate, the other end is cecum, be connected with the lower supporting plate, the tubulation outside in the reaction zone is filled out
Material, is provided with charging aperture at the top of the upper cover, the vertical reactor cylinder side in the reaction zone is provided with side line and enters
Material mouth, is provided with gas phase extraction mouth on the top cylinder of the vaporization Disengagement zone, bottom is provided with side take-off mouthful, under described
Extraction mouth in bottom is provided with end socket.
2. a kind of injecting type shell-and-tube reactor for alkylated reaction as claimed in claim 1, it is characterised in that：The row
The regularity of distribution of aperture is that top is close on tube wall, and bottom is sparse.
3. a kind of injecting type shell-and-tube reactor for alkylated reaction as claimed in claim 1, it is characterised in that：It is described anti-
The vertical reactor cylinder side in area is answered to be disposed with multiple side entry feeds mouthful from top to bottom.
4. a kind of injecting type shell-and-tube reactor for alkylated reaction as described in claims 1 to 3, it is characterised in that：Institute
Lower supporting plate is stated to be made up of multiple layer metal silk screen and grid.
5. a kind of injecting type shell-and-tube reactor for alkylated reaction as claimed in claim 4, it is characterised in that：It is described anti-
It is polypropylene or stainless steel cloth filler to answer the filler in area.
6. a kind of injecting type shell-and-tube reactor for alkylated reaction as claimed in claim 5, it is characterised in that：Described
The bottom for vaporizing Disengagement zone is provided with filler, and described filler is that corrugated plate regular packing or corrugated plating random packing or swash plate are filled out
Material.
7. a kind of method that injecting type shell-and-tube reactor using as described in claim 1~6 is alkylated reaction, its feature
It is to comprise the following steps:
(1) concentrated sulfuric acid is entered into the injecting type shell-and-tube reactor by its top feed mouthful of the upper cover, and by upper
The circular hole of tube sheet flows along tubulation；
(2) certain pressure effect under, be equably ejected into reaction zone by the aperture on the tubulation tube wall, and with by side
The total hydrocarbon feed that line charging aperture enters forms sour hydrocarbon emulsion and completes catalytic reaction under the shear action of filler；
(3) complete the product after catalytic reaction and reaction vaporization Disengagement zone is entered under differential pressure action in reactor, wherein, gas phase
Iso-butane is produced by the gas phase extraction mouth for vaporizing Disengagement zone；
(4) reacted most of sulfuric acid produces mouth and produces by the bottom of low head, and is cycled back to through peracid circular route
End socket charging aperture, a small amount of spent acid enters follow-up processing unit through waste discharge acid line, and the hydrocarbon material after layering is adopted by side take-off mouthful
Follow-up product separator is sent into after going out.
8. the method being alkylated using injecting type shell-and-tube reactor as claimed in claim 7, it is characterised in that：In step
(2) in, catalytic reaction temperature is controlled at -3~4 DEG C.
9. the method being alkylated using injecting type shell-and-tube reactor as claimed in claim 7, it is characterised in that：Step
(2) after also including the gas phase iso-butane that will be produced through overcompression cooling treatment after, reactor pump-around is looped back through hydrocarbon circular route
Charging aperture, it is 8 to control reaction alkane alkene mass ratio：1~10：1.
10. the method being alkylated using injecting type shell-and-tube reactor as claimed in claim 7, it is characterised in that：Reaction
The volume ratio of sour hydrocarbon is 0.8：1~2：1, reaction zone top pressure is controlled for 350~400KPa, reaction zone outlet pressure is 3.5
~8.5KPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710028166.8A CN106732309B (en) | 2017-01-13 | 2017-01-13 | A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710028166.8A CN106732309B (en) | 2017-01-13 | 2017-01-13 | A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106732309A true CN106732309A (en) | 2017-05-31 |
| CN106732309B CN106732309B (en) | 2019-04-16 |
Family
ID=58946991
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710028166.8A Active CN106732309B (en) | 2017-01-13 | 2017-01-13 | A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106732309B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107497392A (en) * | 2017-10-11 | 2017-12-22 | 中石化上海工程有限公司 | Novel injection reactor mouth of pipe nozzle |
| CN110420614A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of multiphase flow process intensification reactor |
| CN110893335A (en) * | 2018-09-12 | 2020-03-20 | 中国石化工程建设有限公司 | Liquid acid alkylation reactor and alkylation reaction method |
| CN113750921A (en) * | 2020-06-04 | 2021-12-07 | 欧瑞康巴马格惠通（扬州）工程有限公司 | Continuous production system of PET or PBT |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130247454A1 (en) * | 2012-03-26 | 2013-09-26 | Sundrop Fuels, Inc. | Various methods and apparatuses for internally heated radiant tubes in a chemical reactor |
| CN203295447U (en) * | 2013-02-19 | 2013-11-20 | 中石化洛阳工程有限公司 | Alkylation reactor for generating high-octane rating alkylate oil |
| CN103769005A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Tubular fixed bed reactor |
| CN104174343A (en) * | 2013-05-22 | 2014-12-03 | 中石化洛阳工程有限公司 | Liquid acid alkylation reactor |
-
2017
- 2017-01-13 CN CN201710028166.8A patent/CN106732309B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130247454A1 (en) * | 2012-03-26 | 2013-09-26 | Sundrop Fuels, Inc. | Various methods and apparatuses for internally heated radiant tubes in a chemical reactor |
| CN103769005A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Tubular fixed bed reactor |
| CN203295447U (en) * | 2013-02-19 | 2013-11-20 | 中石化洛阳工程有限公司 | Alkylation reactor for generating high-octane rating alkylate oil |
| CN104174343A (en) * | 2013-05-22 | 2014-12-03 | 中石化洛阳工程有限公司 | Liquid acid alkylation reactor |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107497392A (en) * | 2017-10-11 | 2017-12-22 | 中石化上海工程有限公司 | Novel injection reactor mouth of pipe nozzle |
| CN107497392B (en) * | 2017-10-11 | 2019-07-16 | 中石化上海工程有限公司 | Injection reactor nozzle nozzle |
| CN110893335A (en) * | 2018-09-12 | 2020-03-20 | 中国石化工程建设有限公司 | Liquid acid alkylation reactor and alkylation reaction method |
| CN110420614A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of multiphase flow process intensification reactor |
| CN113750921A (en) * | 2020-06-04 | 2021-12-07 | 欧瑞康巴马格惠通（扬州）工程有限公司 | Continuous production system of PET or PBT |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106732309B (en) | 2019-04-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107519828B (en) | Using the alkylation and device of micro passage reaction | |
| CN106732309B (en) | A kind of injecting type shell-and-tube reactor and its reaction method for alkylated reaction | |
| KR20140057465A (en) | Reactor and alkylation process using the reactor | |
| CN105219428B (en) | A kind of method of sulfuric acid alkylation reaction | |
| CN102958900B (en) | The liquid phase hydrogenation process of phthalic acid ester | |
| CN107519835B (en) | Micro-channel reactor | |
| CN111087378A (en) | Method for preparing ethylene carbonate | |
| CN105233784B (en) | Alkylation reactor and alkylation method | |
| WO2023284030A1 (en) | Instant dewatering dmc preparation system and preparation method | |
| CN206273355U (en) | Around pipe heat exchange type alkylation reactor | |
| CN107523328B (en) | Alkylation process using microchannel reactor | |
| CN104174343B (en) | A kind of liquid acid alkylation reactor | |
| CN204656510U (en) | A kind of alkylation reactor | |
| CN105413592B (en) | A kind of combined type fixed bed reactors and the device formed by it | |
| US10077219B2 (en) | Continuous mixing reactor and method of use | |
| CN204159342U (en) | A kind of alkylation reactor | |
| CN206535555U (en) | A kind of vertical alkylation reactor | |
| CN104262077B (en) | Parallel ring cast direct chlorination produces the device of 1,2-dichloroethanes | |
| US5286884A (en) | Thermosyphonic reaction of propylene with tertiary butyl hydroperoxide and reactor | |
| CN204111619U (en) | Direct chlorination produces the device of 1,2-ethylene dichloride | |
| CN104387258B (en) | A kind of production of chloroacetic acid method and chlorination reactor | |
| CN205235936U (en) | Modular fixed bed reactor reaches device by its formation | |
| CN114432976B (en) | Alkylated gasoline production device and method | |
| CN205435685U (en) | Hybrid system | |
| CN105032329B (en) | A kind of alkylation reaction method and pulse-flow reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |