CN106854126B - A kind of process units that isooctane is prepared with iso-butane, butene alkylation - Google Patents
A kind of process units that isooctane is prepared with iso-butane, butene alkylation Download PDFInfo
- Publication number
- CN106854126B CN106854126B CN201611142674.0A CN201611142674A CN106854126B CN 106854126 B CN106854126 B CN 106854126B CN 201611142674 A CN201611142674 A CN 201611142674A CN 106854126 B CN106854126 B CN 106854126B
- Authority
- CN
- China
- Prior art keywords
- tank
- pipeline
- butane
- iso
- deisobutanizer
- 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
Classifications
-
- 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
Abstract
The process units of isooctane is prepared with iso-butane, butene reaction the invention discloses a kind of, including is sequentially communicated the raw material dehydration device D201 in alkylation reactor feed end, heat exchanger, de- lighter hydrocarbons tower C101, butene feed heater E101, butene feedstock surge tank D101；Also include being sequentially communicated the flash tank D203 in alkylation reactor discharge end, pickling tank D209, caustic treater D210, water washing tank D211, deisobutanizer, deisobutanizer C201；Wherein deisobutanizer C201 tops connection deisobutanizer return tank D212, isobutane feedstock delivery pipe connection return tank D212, isobutane feedstock, recycle isobutane are sent back to and connected with butene feedstock transfer pipeline with threeway by deisobutanizer reflux pump P209A/B by pipeline, then send alkylation reactor.
Description
Technical field
The present invention relates to petrochemical industry, and in particular to the process units of isooctane is prepared with iso-butane, butene reaction.
Background technology
Isobutane and butene alkylated reaction prepares isooctane, is to prepare the common method of isooctane at present.It is general to use
Technique be, iso-butane-butene feed together with device recycle isobutane and cryogen enter reactor, sulfuric acid catalysis make
Under, alkylated reaction occurs for iso-butane and butylene, generates alkylate oil.
Isobutane and butene alkylated reaction is more complicated, and main reaction meets carbonium ion chain reaction mechanism, iso-butane with
Butylene addition is isooctane, and side reaction mainly has the reaction such as autohemagglutination, fracture, isomerization, esterification.Main reaction is as follows：
1、C4H8 + H2SO4→（C4H9）HSO4
2、（C4H9）HSO4 + C4H10 → C8H18 + H2SO4
Isooctane product is obtained, it is necessary to isobutane and butene mol ratio 1:1 participate in reaction, but in practical operation in order that
Butylene reacts completely, and reduces the side reactions such as alkene generation autohemagglutination, need to ensure that the isobutane and butene in alkylation reactor rubs
You are than being 7-14:1.During system is normally produced, from the foregoing, the iso-butane in alkylation reactor, one is from process
The iso-butane for being used to circulate returned after C201 and C202 separation, two be from charging, at present, the charging that most enterprises are used
Mode is, is all the way mixed olefins, and another road is the iso-butane of high-purity, and two-way raw material enters after being mixed in raw material surge tank
Pretreatment of raw material workshop section, enters alkylation reactor after pretreatment.
There is three below in above-mentioned feeding manner：
Firstth, the iso-butane of high-purity enters pretreatment of raw material tower（De- lighter hydrocarbons tower）, it can not only increase the steam consumption of tower,
It can also bring to expand from raw material surge tank to all devices volume entered before alkylation reactor and be twice the above, this undoubtedly will
Greatly increase the cost of investment of enterprise；Simultaneously as alkylated reaction needs to carry out in less than 6 degrees Celsius, therefore, by de-
About 46 degrees Celsius of temperature of charge is sent outside after lighter hydrocarbons tower, in addition it is also necessary to which the energy in consumption system is cooled down to it.For original
Expect for iso-butane, consumption heat energy raises temperature, then consumes low-temperature receiver reduction temperature, the need for being not alkylated reaction, it is seen then that
There is serious irrationality in this feed way.
Second, in system is normally run, the effluent after alkylated reaction, by C201 and C202 separation processes, portion
Point iso-butane can take system out of by isooctane and normal butane, therefore, the iso-butane added from feed end remove with butene reaction
Consumption is outer, and some is consumed by subsequent separation system, and this part iso-butane of piece-rate system consumption, can be because uncontrollable
Factor is sometimes more sometimes then less, so requires feed end to add the amounts of iso-butane, should be with butylene by mole 1:1
Charging, when realistic again according to the reflux cycle amount of follow-up iso-butane number be adjusted, can ensure in alkylated reaction
Isobutane and butene mol ratio in device is 1:1.But because intermediate equipment is more（D105、C101、E104、E201、D201）, flow
Long and volume is big, and the amount to the iso-butane in alkylation reactor can not accomplish timely adjustment, due to that can not accomplish adjustment in time,
Therefore, the mol ratio of iso-butane can be caused not in the range of design requirement, make output object impurity content high, even result in product
It is unqualified, What is more cause parking accident.
3rd, raw material to raw material, it is necessary to pre-process before alkylation reactor is entered, and de- lighter hydrocarbons unit therein takes off
Except carbon three in raw material and following light component, make the carbon after alkylated reaction three and following light component in compression cooling system
Content maintains the appropriate scopes of 3%-6%.If carbon three and following light component content are too high（More than more than 6%, it is the reason for high
Light component is too many in raw material or de- lighter hydrocarbons tower operational issue etc. can cause light component abjection unclean）, compressor can be caused
Poor refrigerating efficiency, causes power consumption to increase, meanwhile, the light component not removed can be not only enriched with the cryogen tank of compressibility, be made
Cooling-down effect is influenceed into the increase of compressor assembly outlet pressure and increases power consumption, and part carbon three is brought into the way of escape and takes off iso-butane
Tower and de- normal butane tower, can cause tower top pressure to raise, and cause steam energy consumption during fractionation to increase.Of the same trade at present generally does
Method, one is to draw carbon three and following light component from cryogen tank top, torch of setting fire burn-up, this will undoubtedly cause the wasting of resources and
Environmental pollution；Two be the incinerator burning for being sent directly into plant area, and this scheme drawback is, because combustion gas be acidity can caused by fire
The corrosion of equipment is burnt, simultaneously as also resulting in the wasting of resources containing 35-40 ﹪ iso-butanes, butylene in component.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of production dress that isooctane is prepared with iso-butane, butene reaction
Put, it is overcoming that prior art is present, it cannot be guaranteed that design proportioning of iso-butane when with olefin alkylation reaction, and energy consumption
The defects such as height, the wasting of resources, environmental pollution.
The present invention is achieved through the following technical solutions：
It is a kind of that the process units of isooctane is prepared with iso-butane, butene reaction, including be sequentially communicated in alkylation reactor
Raw material dehydration device D201, raw material-effluent heat exchanger E201AC, reactor feed heat exchanger E104, the de- lighter hydrocarbons tower of feed end
C101, butene feedstock feed heater E101, butene feedstock surge tank D101；
Also include being sequentially communicated the flash tank D203 in alkylation reactor discharge end, effluent pickling tank D209, flow out
Alkaloids cleaning of evaporator D210, effluent water washing tank D211, alkylate oil-deisobutanizer feed exchanger E213, deisobutanizer
C201, de- normal butane tower C202, heat exchanger, product tank；Wherein deisobutanizer C201 tops connection deisobutanizer backflow
Recycle isobutane is passed through pipe by tank D212, deisobutanizer reflux pump P209A/B, the deisobutanizer reflux pump P209A/B
Road sends alkylation reactor back to through effluent heat exchanger E201AC, raw material dehydration device D201；
The top connection compressor of the flash tank D203, the gaseous component output of flash tank D203 inner tops is after compression
D204 is filled into cryogen, the cryogen fills D204 bottoms and material is conveyed through into cryogen cooler D203AB by pipeline, then leads to
Cross and send flash tank D203 flash distillation heat absorptions at the top of pipeline connection flash tank D203 back to；
Iso-butane storage tank is provided with control valve by the first pipeline connection iso-butane tower return tank D212, first pipeline；
The cryogen tank top is communicated with the second pipeline, second pipeline by cryogen tank top be enriched with containing 35-40 ﹪ butylene and
Iso-butane, acid light-component gas are delivered to light component alkali cleaning and fill D220, and water washing tank D221 washings, stream are passed through after alkali cleaning
The light-component gas for going out water washing tank D221 pass through the 3rd pipeline connection butene feedstock surge tank D101.
Further improvement project of the invention is that the alkylation reactor is provided with two, is the first alkylated reaction respectively
Device R201A, the second alkylation reactor R201B, the first alkylation reactor R201A, the second alkylation reactor R201B
It is respectively communicated with raw material dehydration device D201 by the first three-way pipe；
The deisobutanizer reflux pump P209A/B, by the raw material iso-butane in deisobutanizer return tank D212, circulation
Iso-butane is pumped out, and is exported through the 6th pipeline, and with the pipeline of butene feedstock conveying the 5th, raw material-outflow is connected by the second three-way pipe
Thing heat exchanger E201AC.
Further improvement project of the invention is that the light component alkali cleaning fills D220, washing filling D221 and is respectively equipped with alkali, water and follows
Ring pump P220AB, P221AB.Light-component gas after alkali cleaning pass through the 3rd pipeline（3）It is communicated in butene feedstock surge tank D101
Bottom, the 3rd pipeline（3）It is provided with light component pump P222AB.
First pipeline, the second pipeline, the 5th pipeline, it is respectively equipped with control valve on the 6th pipeline.
The present invention has advantage following prominent compared with prior art
First, the present invention is by isobutane feedstock, by the first pipeline connection iso-butane tower return tank D212, with iso-butane tower stream
The recycle isobutane gone out sends into alkylation reactor together.（1）It is short with flow because without intermediate equipment, can be in time to alkyl
The mol ratio for changing the iso-butane in reactor and butylene is adjusted, it is ensured that isobutane and butene mol ratio exists in alkylated reaction
Within the scope of defined, so as to ensure the normal operation of production；（2）Compared with prior art, due to feed end all devices, only
The processing of butylene is undertaken, therefore, into the machine utilization reduction before reactor, heat exchange and other effects is greatly improved, and is dropped significantly
Low production cost；（3）Because the present invention enters the isobutane feedstock of alkylation reactor, gratuitous heating had not both been needed,
Exchanged heat also without with low-temperature receiver（This refers to change extra increased heat）Caused energy waste twice, the present invention is by operation
Experiment, in terms of producing 200000 tons of isooctane per year, steam energy consumption reduces by 2 tons per hour, and power consumption reduces about 200KW, Nian Kejie per hour
About 2,880,000 yuan of energy resource consumption.
2nd, about 40% iso-butane, butylene are contained in the acid light-component gas being enriched with due to cryogen tank top, the present invention will
The acid light-component gas of cryogen tank top enrichment are delivered to alkali cleaning and fill the light-component gas feeding butene feedstock after D220 alkali cleanings
Surge tank D101, system, recyclable iso-butane and butylene therein and light component are reentered as raw material, are both avoided existing
There is technology using the method pollution environment burned, resource has been saved again, the production cost of enterprise is reduced.The present invention is by operation
Experiment, in terms of producing 200000 tons of isooctane per year, power consumption of compressor saves 2000 degree of electricity daily, can economize on electricity in year million yuan；Meanwhile, reclaim
Raw material, Nian Kewei enterprises save raw material cost millions of members.
Brief description of the drawings
Fig. 1 is present invention process flow chart.
Embodiment
As shown in drawings, it is a kind of that the process units of isooctane is prepared with iso-butane, butene reaction, including be sequentially communicated in alkane
Raw material dehydration device D201, raw material-effluent heat exchanger E201AC, the reactor feed heat exchanger of glycosylation reaction device feed end
E104, de- lighter hydrocarbons tower C101, butene feedstock feed heater E101, butene feedstock surge tank D101；
Also include being sequentially communicated the flash tank D203 in alkylation reactor discharge end, effluent pickling tank D209, flow out
Alkaloids cleaning of evaporator D210, effluent water washing tank D211, alkylate oil-deisobutanizer feed exchanger E213, deisobutanizer
C201, de- normal butane tower C202, heat exchanger, normal butane product tank；Wherein deisobutanizer C201 tops connection takes off iso-butane
Tower return tank D212, deisobutanizer reflux pump P209A/B, the deisobutanizer reflux pump P209A/B are by recycle isobutane
Alkylation reactor is sent back to through effluent heat exchanger E201AC, raw material dehydration device D201 by pipeline；
The top connection compressor of the flash tank D203, the gaseous component output of flash tank D203 inner tops is after compression
D204 is filled into cryogen, the cryogen fills D204 bottoms and material is conveyed through into cryogen cooler D203AB by pipeline, then leads to
Cross and send flash tank D203 flash distillation heat absorptions at the top of pipeline connection flash tank D203 back to；
Isobutane feedstock connects iso-butane tower return tank D212 by the first pipeline 1, and the first pipeline 1 is provided with control valve.It is different
Butane tower return tank D212 is provided with liquid level gauge, according to the display of liquid level gauge, it is determined whether the control valve opened on the first pipeline 1 is mended
Plus iso-butane.
The cryogen tank top is communicated with the second pipeline 2, and second pipeline 2 contains 35- by what cryogen tank top was enriched with
40 ﹪ butylene and iso-butane, acid light-component gas are delivered to light component alkali cleaning and fill D220, and water washing tank is passed through after alkali cleaning
D221 is washed（Caustic treater passes through pipeline communication with water washing tank）, outflow water washing tank D221 light-component gas pass through the 3rd pipeline 3
Connect butene feedstock surge tank D101（Water washing tank D221 light-component gas are flowed out in neutrality）, the 3rd pipeline 3 is provided with
Light component pump P222AB.The light component alkali cleaning fill D220, washing fill D221 be respectively equipped with alkali, water-circulating pump P220AB,
P221AB.Second pipeline 2 is provided with control valve.
Alkali cleaning fills D220 and is additionally provided with alkali lye feed supplement pipe, salkali waste discharge pipe（Not shown in two pipe figures）, the PH of buck
Value is between 8-10.Washing fills D221 and connected with water pipe, provided with waste liquid discharge pipe（Not shown in two pipe figures）.
The alkylation reactor is provided with two, is the first alkylation reactor R201A, the second alkylation reactor respectively
R201B, the first alkylation reactor R201A, the second alkylation reactor R201B and raw material dehydration device D201 pass through first
Three-way pipe 4 is respectively communicated with.
The deisobutanizer reflux pump P209A/B, by the raw material iso-butane in deisobutanizer return tank D212, circulation
Iso-butane is pumped out, and is exported through the 6th pipeline 6, and raw material-stream is connected by the second three-way pipe 5 with the pipeline 7 of butene feedstock conveying the 5th
Go out thing heat exchanger E201AC, then alkylation reactor is sent back to through raw material dehydration device D201.
Pot bottom connection the refrigerant cycle pump P202AB, refrigerant cycle pump P202AB of the flash tank D203 cryogen output
Pipe is respectively communicated with the first alkylation reactor R201A, the second alkylation reactor R201B feed end by the first three-way pipe 4.
Effluent pickling tank D209 bottoms respectively with the first alkylation reactor R201A, the second alkylation reactor R201B
Feed end connection, be alkylation reactor mend acid.First alkylation reactor R201A, the second alkylation reactor R201B
Reaction chamber is respectively communicated with acid settler D202A, and the semi-finished product alkylate oil after being settled through acid settler D202A is recycled to alkylation
The discharge end of reactor, acid is recycled to the feed end of alkylation reactor.
Running of the present invention：
Two alkylation reactor chargings, dischargings are parallel connection, therefore, only describe material from charging with one of reactor
To the running of discharging.
Butene feedstock through washing, dehydration after enter butene feedstock surge tank D101, by pump P101AB pump out through with de- lighter hydrocarbons
After the heat exchange of tower C101 effluents（Exchanged heat with reactor feed heat exchanger E104）, again by feed heater E101 heating, enter
De- lighter hydrocarbons tower C101.The de- lighter hydrocarbons tower condenser E103AB of connection at the top of de- lighter hydrocarbons tower C101, condensed material flows into de- lighter hydrocarbons
Tower return tank D103, return tank D103 are connected by pump with de- lighter hydrocarbons tower C101.
Butylene after de- lighter hydrocarbons, reacted device feed exchanger E104 through the 5th pipeline 7 with after butene feedstock heat exchange, exporting
The second three-way pipe 5 is connected with raw material iso-butane, the pipeline 6 of recycle isobutane conveying the 6th, is exported through the second three-way pipe 5, then through original
Material-effluent heat exchanger E201AC changes cold（11 DEG C or so）, raw material dehydration device D201 dehydration（The free water in raw material after dehydration
Content is down to 10ppm（Weight））, mixed after the first three-way pipe 4 with the circulation cryogen from flash tank D-203, reduce temperature
A point two-way respectively enters alkylation reactor after to about 3.0 DEG C.Reactor is equipped with interior circulation chuck, heat removing tube beam and stirring
The pressure vessel of impeller, is STRATCO house journals product.
React complete catalyst-hydrocarbon emulsion and be directly entered catalyst settler through a tedge（Not shown in figure）,
And the sedimentation separation of catalyst and hydro carbons is carried out herein, the catalyst separated follows down-comer Returning reactor and reused.From urging
After the hydrocarbon that agent settler is separated is depressured through pressure-control valve, the heat removing tube beam part vaporization in reactor is flowed through, heat is absorbed
Measure elimination reaction heat.Vapour-liquid mixture in alkylation reactor enters flash tank D203 from discharge end output.Flash tank D-
203, which are one, carries central dividing plate and has the horizontal vessel of common separated space（Market is bought）.Flowed out for reaction dividing plate side
Thing carries out gas-liquid separation, and opposite side carries out vapour-liquid separation for circulation cryogen.
Flash tank D203 effluents are extracted out with effluent pump P-201AB, through effluent heat exchanger E201AC and raw material butylene
Change it is cold after, into effluent pickling tank D209, effluent caustic treater D210, effluent water washing tank D211, outflow water washing tank D211
Material afterwards, enters deisobutanizer C201 after alkylate oil-deisobutanizer feed exchanger E213 heat exchange.It is described de-
The de- iso-butane condenser A202 of connection at the top of iso-butane tower C201, it is condensed after iso-butane enter iso-butane tower return tank D212
（As shown in figure 1, raw material iso-butane fills into return tank D212 by the first pipeline 1）, the de- isobutyl connected with return tank D212
Alkane tower reflux pump P209A/B, the fourth exported with the 5th pipeline 7 is exported by raw material iso-butane, recycle isobutane by the 6th pipeline 6
Alkene raw material, is exported through the second three-way pipe 5.
The material of deisobutanizer C201 bottoms outflow enters de- normal butane tower C202, takes off the thing on normal butane tower C202 tops
Material is by the de- normal butane tower return tank D214 of normal butane condenser E211 feedings, and what is connected with de- normal butane tower return tank D214 is de-
Normal butane is sent into tank field by normal butane tower reflux pump P210AB.
The product oil of de- normal butane tower C202 bottoms outflow, is pumped out through alkylate oil discharge pump P211AB, by with alkyl
After carburetion-circulation alkali water- to-water heat exchanger E205AB heat exchange, then through alkylate oil-deisobutanizer feed exchanger E213 heat exchange, alkane
Tank field is sent into after base carburetion cooler E214AB heat exchange.
The hydrocarbon gas come out from flash tank D203 gas-phase spaces enters compressor one-level entrance, and supplement enters into two grades
The gas of mouth is at the top of energy-saving tank D-207.It is empty by cryogen that above-mentioned gas are compressed to 8.2kg/cm2 (a) through compressor
Cooler A-201 is condensed, and the hydrocarbon liquids of condensation enter cryogen tank D-204.The overwhelming majority of the liquid is through cooler E-202AB
Enter energy-saving tank D-207 after cooling, and flashed under the pressure of energy-saving tank, the gas rich in liquefied gas returns to two grades of compressor and entered
Mouthful, the liquid of energy-saving tank outflow removes flash tank, refrigerant temperature is reduced to -10 DEG C or so through being depressured flash distillation, with circulation cryogenic fluid pump
P202AB, which is extracted out, delivers to reactor inlet circulation.
The containing 35-40 ﹪ butylene and iso-butane of enrichment, acid light-component gas are delivered to gently at the top of cryogen tank D-204
Component alkali cleaning fills D220, passes through water washing tank D221 washings after alkali cleaning, and outflow water washing tank D221 light-component gas pass through the
Three pipelines 3 feeding butene feedstock surge tank D101 bottoms（It is easy to be sufficiently mixed with raw material butylene）.
Claims (5)
1. the process units of isooctane is prepared with iso-butane, butene reaction a kind of, including is sequentially communicated to enter in alkylation reactor
Expect raw material dehydration device D201, raw material-effluent heat exchanger E201AC, reactor feed heat exchanger E104, the de- lighter hydrocarbons tower at end
C101, butene feedstock feed heater E101, butene feedstock surge tank D101；
Also include being sequentially communicated the flash tank D203 in alkylation reactor discharge end, effluent pickling tank D209, flow out alkaloids
It is cleaning of evaporator D210, effluent water washing tank D211, alkylate oil-deisobutanizer feed exchanger E213, deisobutanizer C201, de-
Normal butane tower C202, heat exchanger, product tank；Wherein deisobutanizer C201 tops connection deisobutanizer return tank D212,
Deisobutanizer reflux pump P209A/B, the deisobutanizer reflux pump P209A/B are by recycle isobutane by pipeline through outflow
Thing heat exchanger E201AC, raw material dehydration device D201 send alkylation reactor back to；
Gaseous component output in the top connection compressor of the flash tank D203, flash tank D203 enters cryogen after compression
D204 is filled, the cryogen fills D204 bottoms and material is conveyed through into cryogen cooler D203AB by pipeline, then connects by pipeline
Send flash tank D203 flash distillation heat absorptions at the top of logical flash tank D203 back to；
It is characterized in that：The cryogen tank top is communicated with the second pipeline（2）, second pipeline（2）Cryogen tank top is rich
The acid light-component gas of collection are delivered to light component alkali cleaning and fill D220, and water washing tank D221 washings, outflow water are passed through after alkali cleaning
Cleaning of evaporator D221 light-component gas pass through the 3rd pipeline（3）Connect butene feedstock surge tank D101；
Light-component gas after alkali cleaning pass through the 3rd pipeline（3）It is communicated in butene feedstock surge tank D101 bottoms, the 3rd pipeline
（3）It is provided with light component pump P222AB；
Iso-butane storage tank passes through the first pipeline（1）Connect iso-butane tower return tank D212, the first pipeline（1）It is provided with control valve；
The deisobutanizer reflux pump P209A/B, by the raw material iso-butane in deisobutanizer return tank D212, circulation isobutyl
Alkane is pumped out, through the 6th pipeline（6）Output, with the pipeline of butene feedstock conveying the 5th（7）Merge, pass through the second three-way pipe（5）Connection
Raw material-effluent heat exchanger E201AC.
2. a kind of process units that isooctane is prepared with iso-butane, butene reaction according to claim 1, its feature exists
In：The alkylation reactor is provided with two, is the first alkylation reactor R201A, the second alkylation reactor respectively
R201B, the first alkylation reactor R201A, the second alkylation reactor R201B and raw material dehydration device D201 pass through first
Three-way pipe（4）It is respectively communicated with.
3. a kind of process units that isooctane is prepared with iso-butane, butene reaction according to claim 1, its feature exists
In：5th pipeline（7）, the 6th pipeline（6）On be respectively equipped with control valve.
4. a kind of process units that isooctane is prepared with iso-butane, butene reaction according to claim 1, its feature exists
In：The light component alkali cleaning fills D220, washing filling D221 and is respectively equipped with alkali, water-circulating pump P220AB, P221AB.
5. a kind of process units that isooctane is prepared with iso-butane, butene reaction according to claim 1, its feature exists
In：Second pipeline（2）Provided with control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611142674.0A CN106854126B (en) | 2016-12-13 | 2016-12-13 | A kind of process units that isooctane is prepared with iso-butane, butene alkylation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611142674.0A CN106854126B (en) | 2016-12-13 | 2016-12-13 | A kind of process units that isooctane is prepared with iso-butane, butene alkylation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106854126A CN106854126A (en) | 2017-06-16 |
| CN106854126B true CN106854126B (en) | 2017-11-03 |
Family
ID=59126383
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611142674.0A Active CN106854126B (en) | 2016-12-13 | 2016-12-13 | A kind of process units that isooctane is prepared with iso-butane, butene alkylation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106854126B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110028374A (en) * | 2019-04-28 | 2019-07-19 | 东营市科德化工有限公司 | A kind of aviation fuel high-octane isooctane and preparation method thereof |
| CN111533631A (en) * | 2020-05-20 | 2020-08-14 | 海南汇智石化精细化工有限公司 | Industry isooctane production system |
| CN215809415U (en) * | 2021-08-17 | 2022-02-11 | 惠州宇新化工有限责任公司 | Low-temperature alkylation refrigeration system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2158172A2 (en) * | 2007-06-27 | 2010-03-03 | H R D Corporation | System and process for alkylation |
| CN104151119A (en) * | 2014-08-08 | 2014-11-19 | 山东利丰达生物科技有限公司 | Method for preparing isooctane by deep processing of n-butane |
-
2016
- 2016-12-13 CN CN201611142674.0A patent/CN106854126B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2158172A2 (en) * | 2007-06-27 | 2010-03-03 | H R D Corporation | System and process for alkylation |
| CN104151119A (en) * | 2014-08-08 | 2014-11-19 | 山东利丰达生物科技有限公司 | Method for preparing isooctane by deep processing of n-butane |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106854126A (en) | 2017-06-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106631657B (en) | A kind of production line that isooctane is prepared with iso-butane, butene alkylation | |
| CN104151119B (en) | The method of octane-iso is prepared in the deep processing of a kind of carbon four | |
| CN106854126B (en) | A kind of process units that isooctane is prepared with iso-butane, butene alkylation | |
| CN103357369B (en) | A kind of alkylated reaction device and method | |
| CN113521786B (en) | Thermal coupling and heat pump combined separation process and separation device for alkylation reaction product | |
| CN216536963U (en) | Separation system of sulfuric acid alkylation reaction product | |
| CN108211402B (en) | Alkylation reaction product separation device and alkylation reaction product separation method | |
| CN101323553B (en) | Method for improving ethylene apparatus quench oil tower bottom temperature | |
| CN105016946A (en) | Liquid acid catalyzed alkylation reaction method and device for isoparaffin and alkene | |
| CN101244970B (en) | Apparatus and technique for producing ethylene with ethyl alcohol | |
| CN103242895B (en) | C4 alkylation production method and device | |
| CN110028374A (en) | A kind of aviation fuel high-octane isooctane and preparation method thereof | |
| CN218306233U (en) | Energy-saving separation device for sulfuric acid alkylation reaction product | |
| CN107243242A (en) | Refinery's amine liquid desulphurization system and its sulfur method | |
| CN215809415U (en) | Low-temperature alkylation refrigeration system | |
| CN105907481A (en) | Alternating serial reaction device for producing biodiesel from high-pressure gas-phase methanol | |
| CN216062073U (en) | Separation device for sulfuric acid alkylation reaction product | |
| CN111533631A (en) | Industry isooctane production system | |
| CN104109088B (en) | Sec-Butyl Acetate production line | |
| CN201684534U (en) | Nitrated tail gas absorption apparatus | |
| CN205328950U (en) | Device of liquefied gas production petrol | |
| CN212731096U (en) | Oil refinery alkylation unit rectification system | |
| CN204752631U (en) | Continuous production system of environmental protection rubber softening agent | |
| CN111992166B (en) | Novel horizontal alkylation reactor of sulfuric acid process | |
| CN218306234U (en) | Energy-saving separation device for alkylation reaction product |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 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 | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 223005 8 Lu Ji Road, salt chemical industry park, Jiangsu economic and Technological Development Zone, Huaian Patentee after: Lian Li environmental protection new energy Co., Ltd. Address before: 223125 8, Lu Ji Road, salinization new material industrial park, Huaian, Jiangsu Patentee before: LIANLI environmental protection and new energy Limited by Share Ltd |