CN107304151A - A kind of device and method for preparing iso-butane - Google Patents
A kind of device and method for preparing iso-butane Download PDFInfo
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- CN107304151A CN107304151A CN201610256689.3A CN201610256689A CN107304151A CN 107304151 A CN107304151 A CN 107304151A CN 201610256689 A CN201610256689 A CN 201610256689A CN 107304151 A CN107304151 A CN 107304151A
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- hydrogenation
- butane
- lightness
- iso
- removing column
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2702—Catalytic processes not covered by C07C5/2732 - C07C5/31; Catalytic processes covered by both C07C5/2732 and C07C5/277 simultaneously
- C07C5/2724—Catalytic processes not covered by C07C5/2732 - C07C5/31; Catalytic processes covered by both C07C5/2732 and C07C5/277 simultaneously with metals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses a kind of apparatus and method for preparing iso-butane.Described device includes：Pre- lightness-removing column, hydrogenation reactor, hydrogenation input and output material heat exchanger, hydrogenation feed heater, hydrogenation separator, lightness-removing column, iso-butane finishing column, isomerization input and output material heat exchanger, isomerization feed heater, isomerization reactor；Hydrogenation separator includes：It is hydrogenated with hot knock-out pot, hydrogenation aftercooler and is hydrogenated with cold knockout drum；Or including hydrogenation aftercooler and hydrogenation knockout drum.Methods described includes：The raw material of carbon four enters described device via the feeding line of carbon four, iso-butane and normal butane is made after pre- de- light, hydrogenation, separation, iso-butane is made after isomerization reaction, separation in normal butane.The present invention can handle all rich in the lighter hydrocarbons of carbon four, while by waste heat recovery, improving the economic benefit of device.
Description
Technical field
The present invention relates to the lighter hydrocarbons field of carbon four, furtherly, it is related to a kind of device for preparing iso-butane
And method.
Background technology
With deepening continuously for petrochemical industry working depth, liquefied gas, associated gas, oil refining are filled
Put and ethylene unit by-product C4Reasonable utilize of each component is increasingly subject to pay attention in cut.C4In cut
The 1,3-butadiene contained can be separated with the method for extracting rectifying as production synthetic rubber, C4Evaporate
Isobutene in point generates MTBE by ether-based device and methanol reaction and can be by further accurate
Fractionation obtains the 1- butylene of high-purity, and the utilization of other components of carbon four is also less.Iso-butane can be produced
Methyl methacrylate, isobutene, isobutanol, expoxy propane etc..In recent years due to isobutene, different
The demand such as butanol and expoxy propane increases year by year so that the utilization of iso-butane increasingly causes people's
Pay attention to, and because the alkyl plant that domestic oil product upgrading drives is expanded on a large scale, it is different in refinery C four
Butane will switch to balance by surplus rapidly, even (be likely to) not enough.Meanwhile, with shale gas association
Amount of butane continue to increase, because its contain a large amount of normal butanes, by the normal butane caused in refinery C four more
Difficulty seeks one's fortune, and added value is by continuous decrease.
The wide material sources of refinery C four, are broadly divided into two types, a kind of is olefin-containing≤5wt% saturated carbon
Four, another is that carbon four is main after 40~50wt% of olefin(e) centent unsaturated carbon four, ethylene unit ether
It is alkane and monoolefine, 30~60wt% of olefin(e) centent.Currently, these C 4 mixtures overwhelming majority
Burnt up as liquefied gas as fuel, chemical utilization rate is relatively low, due to for the in great demand of iso-butane, and
Normal butane economic value is limited, and the yield for thereby how improving iso-butane is just most important.
Chinese patent literature CN102294203A discloses the carbon four in a kind of catalytic pyrolysis ethene
Secondary hydrogenation device and technique, by using two sections of selective hydrogenations, it is to avoid 1,3-butadiene depth adds
The problem of hydrogen causes reactor coking, reduction catalyst service life and plant running cycle, can be direct
Mixing carbon four is hydrogenated with, the utilization rate of raw material is improved.But for containing a small amount of or no diene
The C 4 mixture of hydrocarbon is without reference to specific separation method, also without reference to impurity such as organic sulfur nitrogen
Removal methods, more without reference to isomerization reaction etc..
Chinese patent literature CN102188985A disclose a kind of C-4-fraction selective hydrogenation catalyst and
Its preparation method, the catalyst can be by the alkynes selective hydrogenation in C-4-fraction, and butadiene is substantially not
Loss, catalyst has high activity, high selectivity and preparation method simple, is widely used.But should
Selective hydrogenation of the invention mainly to alkynes in C-4-fraction, without monoolefine in alkane, alkene mixture
Method of hydrotreating, and the simply preparation of catalyst, without reference to separation method, also without reference to organic
The removal methods of the impurity such as sulphur nitrogen, also without reference to isomerization reaction etc..
Chinese patent literature CN201410444683.X and CN1170632A disclose normal butane isomery
Change prepares catalyst and the application of iso-butane, but mainly catalyst system and process operation parameter, no
It is related to flow exploitation.
Chinese patent literature CN200680015930.8 discloses normal butane to the isomerization side of iso-butane
Method, but positive iso-butane mixture separated by permoselective membrane, and non-traditional ripe rectifying
Separation method, technique is using relatively difficult to achieve.
The content of the invention
Largely had more than needed for the normal butane that solves low value in the prior art, and the iso-butane of high added value is not
Sufficient the problems such as, the invention provides a kind of device and method for preparing iso-butane.By will hydrogenation, it is different
Structure chemical industry skill is combined, and the present invention can handle all rich in the lighter hydrocarbons of carbon four, including liquefied gas, oil
The carbon fourth class after field associated gas, refinery C four and ethylene unit ether, meanwhile, it is excellent by using heat-exchange network
Change technology, by waste heat recovery, improves the economic benefit of device.
An object of the present invention is to provide a kind of device for preparing iso-butane, and described device includes：In advance
Lightness-removing column, hydrogenation reactor, hydrogenation input and output material heat exchanger, hydrogenation feed heater, hydrogenation separation dress
Put, lightness-removing column, iso-butane finishing column, isomerization input and output material heat exchanger, isomerization feed heater and
Isomerization reactor；Wherein,
The pre- lightness-removing column of the feeding line of carbon four connection, pre- lightness-removing column bottom connection hydrogenation input and output material heat exchanger,
It is hydrogenated with connection hydrogenation reactor top after feed heater；
Connection hydrogenation separator, hydrogenation point after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
It is sequentially connected after compressor suction tank, compressor and merges with the feeding line of carbon four from device, then connects
It is hydrogenated with input and output material heat exchanger；
Go out after hydrogenation separator bottom connection lightness-removing column input and output material heat exchanger with carbon after isomerization reaction four
Expects pipe line merges connection lightness-removing column；
Lightness-removing column bottom connection lightness-removing column input and output material heat exchanger after connect iso-butane finishing column, iso-butane into
Product tower side line connects isomerization reaction after being sequentially connected isomerization input and output material heat exchanger, isomerization heater
Device entrance；
Lightness-removing column is connected after isomerization reactor outlet connection isomerization input and output material heat exchanger.
The hydrogenation input and output material heat exchanger can be directly connected to by pipeline at the top of second-stage hydrogenation reactor.
The hydrogenation separator is that, in order to separate hydrogen and lighter hydrocarbons, hydrogenation separator can use following
Two kinds composition one of：
A) the hydrogenation separator includes hydrogenation hot knock-out pot, hydrogenation aftercooler and is hydrogenated with cold knockout drum；
Connection hydrogenation hot knock-out pot, heat from hydrogenation after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
Hydrogenation aftercooler is sequentially connected at the top of knockout drum and cold knockout drum is hydrogenated with, is hydrogenated with the top of cold knockout drum and connects
Compressor suction tank；It is hydrogenated with cold knockout drum bottom connection hydrogenation hot knock-out pot；Heat from hydrogenation knockout drum bottom
Connect lightness-removing column.
B) the hydrogenation separator may also comprise hydrogenation aftercooler and hydrogenation knockout drum；
Hydrogenation aftercooler and hydrogenation are sequentially connected after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
Connection compressor suction tank at the top of knockout drum, hydrogenation knockout drum, hydrogenation knockout drum bottom connection lightness-removing column.
According to two kinds of hydrogenation separators, can have after the hydrogenated input and output material heat exchanger heat exchange of reaction discharging
Two ways, one kind carries out gas-liquid separation to be introduced into hydrogenation hot knock-out pot, and top gas phase is by hydrogenation
Enter after aftercooler cooling and be hydrogenated with cold knockout drum, be hydrogenated with connection compressor suction tank at the top of cold knockout drum,
Bottom connection hydrogenation hot knock-out pot, heat from hydrogenation knockout drum bottom liquid phases connection lightness-removing column；Another way
Pass through gas-liquid separation, top gas phase connection pressure to enter hydrogenation knockout drum after first hydrogenated aftercooler cooling
Contracting machine suction tank, bottom liquid phases connection lightness-removing column.
It is preferred to use first way.
Hydrogenation feed heater described above can use common firing equipment in the prior art, such as：Electricity
Heater, steam heater or heating furnace.
Following technical scheme can specifically be used：
The device for preparing iso-butane includes：Pre- lightness-removing column, hydrogenation reactor, hydrogenation input and output material are changed
Hot device, hydrogenation feed heater, hydrogenation separator, lightness-removing column, iso-butane finishing column, isomerization
Input and output material heat exchanger, isomerization feed heater and isomerization reactor；Wherein,
The pre- lightness-removing column of the feeding line of carbon four connection, pre- lightness-removing column bottom connection hydrogenation input and output material heat exchanger,
It is hydrogenated with connection hydrogenation reactor top after feed heater；
Connection hydrogenation hot knock-out pot after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger；Heat from hydrogenation
Hydrogenation aftercooler is sequentially connected at the top of knockout drum and cold knockout drum is hydrogenated with, is hydrogenated with the top of cold knockout drum successively
Merge after connection compressor suction tank, compressor with the feeding line of carbon four, then connection hydrogenation input and output material
Heat exchanger；It is hydrogenated with cold knockout drum bottom connection hydrogenation hot knock-out pot；
Go out after heat from hydrogenation knockout drum bottom connection lightness-removing column input and output material heat exchanger with carbon after isomerization reaction four
Expects pipe line merges connection lightness-removing column；
Lightness-removing column bottom connection lightness-removing column input and output material heat exchanger after connect iso-butane finishing column, iso-butane into
Product tower side line connects isomerization reaction after being sequentially connected isomerization input and output material heat exchanger, isomerization heater
Device entrance；
Lightness-removing column is connected after isomerization reactor outlet connection isomerization input and output material heat exchanger.
The second object of the present invention is to provide a kind of method that use described device prepares iso-butane, described
Method includes：
The raw material of carbon four enters described device via the feeding line of carbon four, after pre- de- light, hydrogenation, separation
Iso-butane and normal butane is made, iso-butane is made after isomerization reaction, separation in wherein normal butane.
Specifically it may include following steps：
(a) by the raw material of carbon four that out-of-bounds comes removed first through pre- lightness-removing column include carbon two, light group of carbon three
Point；Enter hydrogenation reactor by alkene after the pre- hydrogenated input and output material heat exchanger heat exchange of lightness-removing column bottoms material
Saturation and imurity-removal are hydrogenated with, the impurity includes micro organic sulfur nitrogen etc.；
(b) hydrogenation separator is entered after the hydrogenated input and output material heat exchanger of hydrogenation reactor bottom discharge,
The hydrogen isolated returns to hydrogenation reactor, and hydrogenation separator bottoms material is changed through lightness-removing column input and output material
After hot device heat exchange lightness-removing column is combined into carbon after isomerization reaction four；
(c) iso-butane finished product is entered after lightness-removing column bottoms material exchanges heat through lightness-removing column input and output material heat exchanger
Tower；Iso-butane product is obtained by top of tower by rectifying separation, tower reactor obtains light dydrocarbon heavy constituent, tower side
Mixture of the line extraction comprising normal butane and iso-butane；
(d) mixture comprising normal butane and iso-butane is through isomerization input and output material heat exchanger, isomery
Enter isomerization reactor after changing heater heat exchange, carry out isomerization reaction, normal butane is converted into different
Butane；
(e) isomerization reactor bottom discharge is separated after being exchanged heat through isomerization input and output material heat exchanger with hydrogenation
Bottom of device material is merged into lightness-removing column.
In step (a), the raw material of carbon four includes the light component of carbon two, carbon three through the removing of pre- lightness-removing column, in advance
Lightness-removing column bottoms material, which is heated to after 160~300 DEG C, enters hydrogenation reactor.When hydrogenation reaction temperature rise
It is very high, then feed heater heating need not be hydrogenated with during normal production, is reachable by input and output material heat exchange
To reaction temperature, need to be hydrogenated with feed heater, now, hydrogenated input and output material heat exchanger when only driving
The material of heat exchange can be directly entered second-stage hydrogenation reactor by pipeline.When hydrogenation reaction temperature rise is not high,
Then during normal production in addition to being exchanged heat by input and output material, in addition it is also necessary to be hydrogenated with feed heater and heated.
In step (b), when hydrogenation separator includes hydrogenation hot knock-out pot, hydrogenation aftercooler and hydrogenation
During cold knockout drum, the hydrogenated input and output material heat exchanger of hydrogenation reactor bottom discharge is cooled to after 50~100 DEG C
Into hydrogenation hot knock-out pot, hydrogenation hot knock-out pot top gas phase is cooled to 20 by hydrogenation aftercooler~
Enter after 50 DEG C and be hydrogenated with cold knockout drum.
In step (b), when being hydrogenated with separator including being hydrogenated with aftercooler and hydrogenation knockout drum, hydrogenation
After the heat exchange of reactor bottom material hydrogenated input and output material heat exchanger, then hydrogenated aftercooler be cooled to 20~
Enter hydrogenation knockout drum after 50 DEG C.
Specifically, following technical scheme can be used：
(a) by the raw material of carbon four that out-of-bounds comes removed first through pre- lightness-removing column include carbon two, light group of carbon three
Point；The pre- hydrogenated input and output material heat exchanger heat exchange of lightness-removing column bottoms material, then hydrogenated feed heater liter
Temperature finally enters hydrogenation reactor by olefins hydrogenation and micro organic sulfur nitrogen to 160~300 DEG C
It is converted into H2S and NH3；
(b) hydrogenation reactor bottom discharge through be cooled to can after 50~100 DEG C after hydrogenation charging heat exchange
There is two ways, a kind of hydrogenated aftercooler of elder generation, which is cooled to after 20~50 DEG C, enters hydrogenation knockout drum progress
Gas-liquid separation, top gas phase connection compressor suction tank, bottom liquid phases connection dehydrogenation tower；Another side
Formula carries out gas-liquid separation to be introduced into hydrogenation hot knock-out pot, and top gas phase is cooled to by hydrogenation aftercooler
Enter after 20~50 DEG C and be hydrogenated with cold knockout drum, connection compressor suction tank at the top of cold knockout drum, bottom connects
Connect hydrogenation hot knock-out pot, heat from hydrogenation knockout drum bottom liquid phases connection lightness-removing column；
It is hydrogenated with knockout drum or is hydrogenated with cold knockout drum top gas phase and returns to hydrogenation instead mostly as circulating hydrogen
It should feed, and non-hydrogen gas stable content in circulation hydrogen system is maintained by pipeline of releasing；
(c) fresh hydrogen is compressed from out-of-bounds compressor is combined into compressor suction head space gas body
Enter hydrogenation input and output material heat exchanger after machine supercharging together with the raw material of carbon four；
(d) heat from hydrogenation knockout drum bottoms material is anti-with isomerization after being exchanged heat through lightness-removing column input and output material heat exchanger
Carbon four is mixed into lightness-removing column after answering, and is separated by rectifying, top gaseous phase removing H2S, NH3Deng not coagulating
Gas, liquid phase removing carbon two, the third light component of carbon, bottoms material enters iso-butane finishing column, passes through essence
Cut obtains iso-butane product from the top of iso-butane finishing column, and tower reactor obtains light dydrocarbon heavy constituent；
(e) by mixture of the iso-butane finishing column side take-off comprising normal butane and iso-butane with it is out-of-bounds new
The mixing of fresh hydrogen is heated to 100 by isomerization input and output material heat exchanger, isomerization feed heater~
Enter isomerization reactor after 250 DEG C, normal butane is converted into iso-butane herein；
(f) material enters lightness-removing column through isomerization input and output material heat exchanger heat exchange Posterior circle after isomerization reaction,
Separated by rectifying, removed overhead H2、H2S, carbon two, the third light component of carbon, tower reactor obtain positive isobutyl
Alkane mixture.
The present invention uses hydrogenation catalyst for nickel system or palladium series hydrocatalyst；Isomerization catalyst is
The catalyst that one or both of Pt, Pd, Ir are constituted.
The process conditions of each equipment of the present invention can use the process conditions generally used in the prior art,
In the present invention, preferably using following process conditions：
The operating condition of the pre- lightness-removing column includes：Pressure is 1~3MPaG (gauge pressure, as follows),
Tower top operation temperature is 20~90 DEG C, and the number of plates is 30~120, and reflux ratio is 1~15；
Hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 160~300 DEG C, and pressure is
1.5~4.5MPaG, reaction temperature rising is 5~100 DEG C, and hydrogen/oil mol ratio is 0.2~5, and liquid volume is empty
Speed is 0.5~6h-1；
The operating condition of lightness-removing column includes：Pressure is 1~3MPaG, and tower top operation temperature is 30~90 DEG C,
The number of plates is 30~80, and reflux ratio is 1~100；
The operating condition of iso-butane finishing column includes：Pressure is 0.1~1MPaG, and tower top operation temperature is
20~70 DEG C, the number of plates is 80~150, and reflux ratio is 1~20；
Isomerization reactor is fixed bed reactors, and reactor inlet temperature is 100~250 DEG C, pressure
For 1.0~4.0MPaG, reaction temperature rising is 5~50 DEG C, and liquid volume air speed is 1~20h-1。
It is characteristic of the invention that：
1) unsaturated olefin is completely converted into saturated hydrocarbons by being hydrogenated with, organic sulfur nitrogen etc. in raw material is miscellaneous
Matter is converted into H2S and NH3Removed, it is to avoid influence to product；
2) by rationally setting heat exchange order, recover energy to the full extent, reduce system energy consumption, carry
The high economic benefit of device, passes through a series of heat exchange network optimizations, saves energy consumption more than 15%；
3) bottom temperature is made to be below 150 DEG C by suitable operating parameter, 45 DEG C or so of tower top temperature,
It can be exchanged heat using more cheap low-pressure steam and recirculated cooling water, the steaming high-grade without outside intervention
The chilled water of vapour and high-quality；
4) present invention can handle all rich in carbon four by the way that hydrogenation and isomerization process are combined
Lighter hydrocarbons be used for produce iso-butane；
5) present invention, can also by-product carbon two, the product of carbon three in addition to iso-butane is obtained.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
It is of the invention by the way that exemplary embodiment of the invention is described in more detail with reference to accompanying drawing
Above-mentioned and other purposes, feature and advantage will be apparent, wherein, it is exemplary in the present invention
In embodiment, identical reference number typically represents same parts.
Fig. 1 is the schematic device for preparing iso-butane of the invention, wherein hydrogenation separator includes adding
Hydrogen hot knock-out pot, hydrogenation aftercooler and the cold knockout drum of hydrogenation.
Fig. 2 is the schematic device for preparing iso-butane of the invention, wherein hydrogenation separator includes adding
Hydrogen aftercooler and hydrogenation knockout drum.
Description of reference numerals：
Pre- lightness-removing column 1, pre- condenser of light component removal column 2, pre- lightness-removing column reboiler 3, hydrogenation reactor 4,
Be hydrogenated with input and output material heat exchanger 5, hydrogenation feed heater 6, hydrogenation aftercooler 7, hydrogenation knockout drum 8,
It is hydrogenated with hot knock-out pot 9, is hydrogenated with cold knockout drum 10, compressor suction tank 11, compressor 12, lightness-removing column
Input and output material heat exchanger 13, lightness-removing column 14, condenser of light component removal column 15, lightness-removing column reboiler 16, isobutyl
Alkane finishing column 17, iso-butane finishing column condenser 18, iso-butane finishing column reboiler 19, isomerization are entered
Effluent exchanger 20, isomerization feed heater 21, isomerization reactor 22, the raw material 23 of carbon four,
Pre- lightness-removing column fixed gas 24, pre- lightness-removing column top liquid phase 25, periodic off-gases 26, hydrogenation hydrogen make-up 27,
Lightness-removing column top fixed gas 28, lightness-removing column top C3Liquid phase 29, iso-butane product 30, light dydrocarbon heavy constituent 31,
Isomerization hydrogen make-up 32.
Embodiment
The preferred embodiment of the present invention is more fully described below with reference to accompanying drawings.
Iso-butane is prepared using combination unit as shown in Figure 1.
The device includes：Pre- lightness-removing column 1, hydrogenation reactor 4, hydrogenation input and output material heat exchanger 5, hydrogenation
Feed heater 6, hydrogenation separator, lightness-removing column 14, iso-butane finishing column 17, isomerization turnover
Expect heat exchanger 20, isomerization feed heater 21 and isomerization reactor 22；Wherein,
The feeding line of carbon four connects pre- lightness-removing column 1, the pre- bottom of lightness-removing column 1 connection hydrogenation input and output material heat exchanger
5th, connection hydrogenation reactor 4 top after hydrogenation feed heater 6；
Connection hydrogenation hot knock-out pot 9 after the bottom of hydrogenation reactor 4 connection hydrogenation input and output material heat exchanger 5；Plus
The top of hydrogen hot knock-out pot 9 is sequentially connected hydrogenation aftercooler 7 and is hydrogenated with cold knockout drum 10, is hydrogenated with cold separation
The top of tank 10 is sequentially connected after compressor suction tank 11, compressor 12 to be merged with the feeding line of carbon four,
Then connection is hydrogenated with input and output material heat exchanger 5；It is hydrogenated with the cold bottom of knockout drum 10 connection hydrogenation hot knock-out pot 9；
It is hydrogenated with after the bottom of hot knock-out pot 9 connection lightness-removing column input and output material heat exchanger 13 and carbon after isomerization reaction
Four discharging pipelines merge connection lightness-removing column 14；
Connection iso-butane finishing column 17 after the bottom of lightness-removing column 14 connection lightness-removing column input and output material heat exchanger 13,
The side line of iso-butane finishing column 17 is sequentially connected isomerization input and output material heat exchanger 20, isomerization heater 21
The entrance of isomerization reactor 22 is connected afterwards；
Lightness-removing column 14 is connected after the outlet of isomerization reactor 22 connection isomerization input and output material heat exchanger 20.
Preparing the method for iso-butane includes：
(a) by the raw material 23 of carbon four out-of-bounds come is removed including carbon two, carbon three through pre- lightness-removing column 1 first
Light component；The pre- hydrogenated input and output material heat exchanger 5 of the bottoms material of lightness-removing column 1 exchanges heat, then it is hydrogenated enter
Material heater 6 is warming up to 240 DEG C, finally enters hydrogenation reactor 4 by olefins hydrogenation and micro
Organic sulfur nitrogen is converted into H2S and NH3；
(b) bottom discharge of hydrogenation reactor 4 with being cooled to enter after 80 DEG C after hydrogenation charging heat exchange through adding
Hydrogen hot knock-out pot 9 carry out gas-liquid separation, top gas phase by hydrogenation aftercooler 7 be cooled to 40 DEG C it is laggard
Enter to be hydrogenated with cold knockout drum 10, be hydrogenated with the cold top of knockout drum 10 connection compressor suction tank 11, bottom connects
Connect hydrogenation hot knock-out pot 9, hydrogenation hot knock-out pot 9 bottom liquid phases connection lightness-removing column 14；
It is hydrogenated with the cold top gas phase of knockout drum 10 and returns to hydrogenation reaction charging mostly as circulating hydrogen, and
Periodic off-gases 26 are discharged by pipeline of releasing and maintain non-hydrogen gas stable content in circulation hydrogen system；
(c) fresh hydrogen as hydrogenation hydrogen make-up 27 from out-of-bounds with the top gas body of compressor suction tank 11
Compressor 12 is combined into, entering hydrogenation input and output material together with the raw material of carbon four after being pressurized through compressor 12 changes
Hot device 5；
(d) hydrogenation the bottoms material of hot knock-out pot 9 through lightness-removing column input and output material heat exchanger 13 exchange heat after with it is different
Carbon four is mixed into lightness-removing column 14 after structureization reaction, is separated by rectifying, top gaseous phase removing H2S,
NH3Deng fixed gas, liquid phase removing carbon two, the third light component of carbon, bottoms material enters iso-butane finished product
Tower 17, obtains iso-butane product 30, tower reactor is obtained by rectifying separation by the top of iso-butane finishing column 17
To light dydrocarbon heavy constituent 31；
(e) by mixture and boundary of the side take-off of iso-butane finishing column 17 comprising normal butane and iso-butane
Outer fresh hydrogen is the mixing of isomerization hydrogen make-up 32 by isomerization input and output material heat exchanger 20, isomerization
Feed heater 21 is heated to after 160 DEG C entering isomerization reactor 22, is herein converted into normal butane
Iso-butane；
(f) material enters de- light through the heat exchange Posterior circle of isomerization input and output material heat exchanger 20 after isomerization reaction
Tower 14, is separated by rectifying, removed overhead H2、H2S, carbon two, the third light component of carbon, tower reactor are obtained
To positive iso-butane mixture.
Using following process conditions：
The operating condition of the pre- lightness-removing column includes：Pressure is 2MPaG, and tower top operation temperature is 55 DEG C,
The number of plates is 80, and reflux ratio is 10；
Hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 240 DEG C, and pressure is 3MPaG,
Reaction temperature rising is 25 DEG C, and hydrogen/oil mol ratio is 1.1, and liquid volume air speed is 2h-1；
The operating condition of lightness-removing column includes：Pressure is 1.8MPaG, and tower top operation temperature is 50 DEG C, tower
Plate number is 50, and reflux ratio is 50；
The operating condition of iso-butane finishing column includes：Pressure is 0.5MPaG, and tower top operation temperature is
50 DEG C, the number of plates is 130, and reflux ratio is 6；
Isomerization reactor is fixed bed reactors, and reactor inlet temperature is 160 DEG C, and pressure is
3.3MPaG, reaction temperature rising is 30 DEG C, and liquid volume air speed is 10h-1。
Using system as shown in Figure 1, the result of table 1 is obtained.
As a result show, using the system and method iso-butane of the present invention, iso-butane yield ＞ 97%.
Table 1
By said apparatus and process, energy consumption more than 15% is saved.
It is described above various embodiments of the present invention, described above is exemplary, and exhaustive
Property, and it is also not necessarily limited to disclosed each embodiment.In the model without departing from illustrated each embodiment
Enclose and spirit in the case of, many modifications and changes for those skilled in the art
It will be apparent from.
Claims (10)
1. a kind of device for preparing iso-butane, it is characterised in that：
Described device includes：Pre- lightness-removing column, hydrogenation reactor, hydrogenation input and output material heat exchanger, be hydrogenated with into
Expect heater, hydrogenation separator, lightness-removing column, iso-butane finishing column, the heat exchange of isomerization input and output material
Device, isomerization feed heater and isomerization reactor；Wherein,
The pre- lightness-removing column of the feeding line of carbon four connection, pre- lightness-removing column bottom connection hydrogenation input and output material heat exchanger,
It is hydrogenated with connection hydrogenation reactor top after feed heater；
Connection hydrogenation separator, hydrogenation point after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
It is sequentially connected after compressor suction tank, compressor and merges with the feeding line of carbon four from device, then connects
It is hydrogenated with input and output material heat exchanger；
Go out after hydrogenation separator bottom connection lightness-removing column input and output material heat exchanger with carbon after isomerization reaction four
Expects pipe line merges connection lightness-removing column；
Lightness-removing column bottom connection lightness-removing column input and output material heat exchanger after connect iso-butane finishing column, iso-butane into
Product tower side line connects isomerization reaction after being sequentially connected isomerization input and output material heat exchanger, isomerization heater
Device entrance；
Lightness-removing column is connected after isomerization reactor outlet connection isomerization input and output material heat exchanger.
2. the device as claimed in claim 1 for preparing iso-butane, it is characterised in that：
The hydrogenation separator includes hydrogenation hot knock-out pot, hydrogenation aftercooler and is hydrogenated with cold knockout drum；
Connection hydrogenation hot knock-out pot, heat from hydrogenation after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
Hydrogenation aftercooler is sequentially connected at the top of knockout drum and cold knockout drum is hydrogenated with, is hydrogenated with the top of cold knockout drum and connects
Compressor suction tank；It is hydrogenated with cold knockout drum bottom connection hydrogenation hot knock-out pot；Heat from hydrogenation knockout drum bottom
Connect lightness-removing column.
3. the device as claimed in claim 1 for preparing iso-butane, it is characterised in that：
The hydrogenation separator includes hydrogenation aftercooler and hydrogenation knockout drum；
Hydrogenation aftercooler and hydrogenation are sequentially connected after hydrogenation reactor bottom connection hydrogenation input and output material heat exchanger
Connection compressor suction tank at the top of knockout drum, hydrogenation knockout drum, hydrogenation knockout drum bottom connection lightness-removing column.
4. the device for preparing iso-butane as described in any one in claim 1-3, it is characterised in that：
The hydrogenation feed heater is electric heater, steam heater or heating furnace.
5. a kind of method that device using as described in any one in claim 1-4 prepares iso-butane,
Characterized in that, methods described includes：
The raw material of carbon four enters described device via the feeding line of carbon four, after pre- de- light, hydrogenation, separation
Iso-butane and normal butane is made, iso-butane is made after isomerization reaction, separation in wherein normal butane.
6. the method as claimed in claim 5 for preparing iso-butane, it is characterised in that methods described bag
Include：
(a) by the raw material of carbon four that out-of-bounds comes removed first through pre- lightness-removing column include carbon two, light group of carbon three
Point；Enter hydrogenation reactor by alkene after the pre- hydrogenated input and output material heat exchanger heat exchange of lightness-removing column bottoms material
It is hydrogenated with saturation and imurity-removal；
(b) hydrogenation separator is entered after the hydrogenated input and output material heat exchanger of hydrogenation reactor bottom discharge,
The hydrogen isolated returns to hydrogenation reactor, and hydrogenation separator bottoms material is changed through lightness-removing column input and output material
After hot device heat exchange lightness-removing column is combined into carbon after isomerization reaction four；
(c) iso-butane finished product is entered after lightness-removing column bottoms material exchanges heat through lightness-removing column input and output material heat exchanger
Tower；Iso-butane product is obtained by top of tower by rectifying separation, tower reactor obtains light dydrocarbon heavy constituent, tower side
Mixture of the line extraction comprising normal butane and iso-butane；
(d) mixture comprising normal butane and iso-butane is through isomerization input and output material heat exchanger, isomery
Enter isomerization reactor after changing heater heat exchange, carry out isomerization reaction, normal butane is converted into different
Butane；
(e) isomerization reactor bottom discharge is separated after being exchanged heat through isomerization input and output material heat exchanger with hydrogenation
Bottom of device material is merged into lightness-removing column.
7. the method as claimed in claim 6 for preparing iso-butane, it is characterised in that：
In step (a), the raw material of carbon four includes the light component of carbon two, carbon three through the removing of pre- lightness-removing column, in advance
Lightness-removing column bottoms material, which is heated to after 160~300 DEG C, enters hydrogenation reactor.
8. the method as claimed in claim 6 for preparing iso-butane, it is characterised in that：
In step (b), when hydrogenation separator includes hydrogenation hot knock-out pot, hydrogenation aftercooler and hydrogenation
During cold knockout drum, the hydrogenated input and output material heat exchanger of hydrogenation reactor bottom discharge is cooled to after 50~100 DEG C
Into hydrogenation hot knock-out pot, hydrogenation hot knock-out pot top gas phase is cooled to 20 by hydrogenation aftercooler~
Enter after 50 DEG C and be hydrogenated with cold knockout drum.
9. the method as claimed in claim 6 for preparing iso-butane, it is characterised in that：
In step (b), when being hydrogenated with separator including being hydrogenated with aftercooler and hydrogenation knockout drum, hydrogenation
After the heat exchange of reactor bottom material hydrogenated input and output material heat exchanger, then hydrogenated aftercooler be cooled to 20~
Enter hydrogenation knockout drum after 50 DEG C.
10. the method for preparing iso-butane as described in any one in claim 6-9, it is characterised in that：
The operating condition of pre- lightness-removing column includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
90 DEG C, the number of plates is 30~120, and reflux ratio is 1~15；
Hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 160~300 DEG C, and pressure is
1.5~4.5MPaG, reaction temperature rising is 5~100 DEG C, and hydrogen/oil mol ratio is 0.2~5, and liquid volume is empty
Speed is 0.5~6h-1；
The operating condition of lightness-removing column includes：Pressure is 1~3MPaG, and tower top operation temperature is 30~90 DEG C,
The number of plates is 30~80, and reflux ratio is 1~100；
The operating condition of iso-butane finishing column includes：Pressure is 0.1~1MPaG, and tower top operation temperature is
20~70 DEG C, the number of plates is 80~150, and reflux ratio is 1~20；
Isomerization reactor is fixed bed reactors, and reactor inlet temperature is 100~250 DEG C, pressure
For 1.0~4.0MPaG, reaction temperature rising is 5~50 DEG C, and liquid volume air speed is 1~20h-1。
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