CN107304155A - The process units and method of a kind of iso-butane - Google Patents
The process units and method of a kind of iso-butane Download PDFInfo
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- CN107304155A CN107304155A CN201610258442.5A CN201610258442A CN107304155A CN 107304155 A CN107304155 A CN 107304155A CN 201610258442 A CN201610258442 A CN 201610258442A CN 107304155 A CN107304155 A CN 107304155A
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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
- C07C5/2767—Changing the number of side-chains
- C07C5/277—Catalytic processes
- C07C5/2791—Catalytic processes 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 process units of iso-butane and method.Described device includes：Hydrogenation reactor, hydrogenation input and output material heat exchanger, hydrogenation feed heater, hydrogenation separator, dethanizer, depropanizing tower, stabilizer, 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 hydrogenated, separation, iso-butane is made after isomerization reaction, separation in normal butane, while the product of by-product carbon three.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 process units of 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.
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 process units of iso-butane and method.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 process units of iso-butane, and described device includes：Plus
Hydrogen reactor, hydrogenation input and output material heat exchanger, hydrogenation feed heater, hydrogenation separator, deethanization
Tower, depropanizing tower, stabilizer, iso-butane finishing column, isomerization input and output material heat exchanger, isomerization are entered
Expect heater and isomerization reactor；Wherein,
Connection hydrogenation is anti-after the feeding line of carbon four connection hydrogenation input and output material heat exchanger, hydrogenation feed heater
Answer device top；
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；
Separator bottom connection dethanizer is hydrogenated with, Deethanizer bottom connection depropanizing tower takes off third
Merge company with the discharging pipeline of carbon after isomerization reaction four after alkane tower bottom stable connection tower input and output material heat exchanger
Connect stabilizer；
Connect iso-butane finishing column after stable tower bottom stable connection tower input and output material heat exchanger, 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；
Stable connection tower 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 dethanizer.
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 deethanization
Tower.
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 connect dethanizer (such as Fig. 1 institutes
Show)；Another way passes through gas-liquid separation to enter hydrogenation knockout drum after first hydrogenated aftercooler cooling,
Top gas phase connects compressor suction tank, bottom liquid phases connection dethanizer (as shown in Figure 2).
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 process units of the iso-butane includes：Hydrogenation reactor, hydrogenation input and output material heat exchanger, hydrogenation
Feed heater, hydrogenation separator, dethanizer, depropanizing tower, stabilizer, iso-butane finished product
Tower, isomerization input and output material heat exchanger, isomerization feed heater and isomerization reactor；Wherein,
Connection hydrogenation is anti-after the feeding line of carbon four connection hydrogenation input and output material heat exchanger, hydrogenation feed heater
Answer device top；
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；
Heat from hydrogenation knockout drum bottom connects dethanizer, and Deethanizer bottom connection depropanizing tower takes off third
Merge company with the discharging pipeline of carbon after isomerization reaction four after alkane tower bottom stable connection tower input and output material heat exchanger
Connect stabilizer；
Connect iso-butane finishing column after stable tower bottom stable connection tower input and output material heat exchanger, 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；
Stable connection tower 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 produces iso-butane, described
Method includes：
The raw material of carbon four enters described device via the feeding line of carbon four, and isobutyl is made after hydrogenated, separation
Iso-butane is made after isomerization reaction, separation in alkane and normal butane, wherein normal butane, while by-product carbon
Three products.
Specifically it may include following steps：
(a) hydrogenation reactor is entered after the hydrogenated input and output material heat exchanger heat exchange of the raw material of carbon four out-of-bounds come
By olefins hydrogenation and imurity-removal；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 enters dethanizer, led to
Cross rectifying separation top and separate the light component of carbon two；
(c) Deethanizer bottom material enters depropanizing tower, and top separates the liquid-phase product of carbon three, bottom
Material is combined into stabilizer after being exchanged heat through stabilizer input and output material heat exchanger with carbon after isomerization reaction four；
(d) iso-butane finished product is entered after stabilizer bottoms material exchanges heat through stabilizer 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；
(e) 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；
(f) with depropanizing tower after isomerization reactor bottom discharge exchanges heat through isomerization input and output material heat exchanger
Bottoms material is merged into stabilizer.
In step (a), the raw material of carbon four, which is heated to after 160~300 DEG C, enters hydrogenation reactor.When adding
Hydrogen reaction temperature rising is very high, then feed heater heating need not be hydrogenated with during normal production, passes through input and output material
Heat exchange i.e. can reach reaction temperature, only drive when need be hydrogenated with feed heater, now, it is hydrogenated enter
The material of effluent exchanger heat exchange can be directly entered second-stage hydrogenation reactor by pipeline.Work as 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 enter
Row heating.
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) circulating hydrogen returned by the raw material of carbon four out-of-bounds come with compressor is mixed into hydrogenation turnover
Expect that heat exchanger, then hydrogenated feed heater are warming up to 160~300 DEG C, finally enter hydrogenation reactor
H is converted into by olefins hydrogenation and micro organic sulfur nitrogen2S 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 dethanizer；It is another
Mode carries out gas-liquid separation to be introduced into hydrogenation hot knock-out pot, and top gas phase is by hydrogenation aftercooler cooling
Enter after to 20~50 DEG C and be hydrogenated with cold knockout drum, connection compressor suction tank, bottom at the top of cold knockout drum
Connection hydrogenation hot knock-out pot, heat from hydrogenation knockout drum bottom liquid phases connection dethanizer.
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 enters dethanizer, and carbon is separated by rectifying separation top
Two light components；
(e) Deethanizer bottom material enters depropanizing tower, and top separates the liquid-phase product of carbon three, bottom
Material is combined into stabilizer after being exchanged heat through stabilizer input and output material heat exchanger with carbon after isomerization reaction four；
(f) iso-butane finishing column is entered after stabilizer bottoms material exchanges heat through stabilizer input and output material heat exchanger,
Iso-butane product is obtained at the top of iso-butane finishing column by rectifying separation, tower reactor obtains light dydrocarbon heavy constituent.
(g) 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, 100 are heated to 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；
(h) material enters stable through isomerization input and output material heat exchanger heat exchange Posterior circle after isomerization reaction
Tower, is separated by rectifying, removed overhead H2、H2The light components such as S, tower reactor obtains positive iso-butane mixing
Thing.
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 hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 160~300 DEG C, pressure
Power is 1.5~4.5MPaG (gauge pressure, as follows), and reaction temperature rising is 5~100 DEG C, hydrogen/oil mol ratio
For 0.2~5, liquid volume air speed is 0.5~6h-1；
The operating condition of dethanizer includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
80 DEG C, the number of plates is 30~100, and reflux ratio is 1~20；
The operating condition of depropanizing tower includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
80 DEG C, the number of plates is 30~100, and reflux ratio is 1~20；
The operating condition of stabilizer includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
100 DEG C, the number of plates is 30~100, 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 be while the product of by-product carbon three.
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 process units schematic diagram of the iso-butane of the present invention, wherein hydrogenation separator includes adding
Hydrogen hot knock-out pot, hydrogenation aftercooler and the cold knockout drum of hydrogenation.
Fig. 2 is the process units schematic diagram of the iso-butane of the present invention, wherein hydrogenation separator includes adding
Hydrogen aftercooler and hydrogenation knockout drum.
Description of reference numerals：
Hydrogenation reactor 1, hydrogenation input and output material heat exchanger 2, hydrogenation feed heater 3, hydrogenation aftercooler
4th, hydrogenation knockout drum 5, hydrogenation hot knock-out pot 6, the cold knockout drum 7 of hydrogenation, compressor suction tank 8, pressure
Contracting machine 9, dethanizer 10, dethanizer condenser 11, deethanizer reboiler 12, depropanizing tower
13rd, depropanizing tower condenser 14, depropanizing tower reboiler 15, stabilizer input and output material heat exchanger 16, steady
Determine tower 17；Stabilizer condenser 18, stabilizer reboiler 19, iso-butane finishing column 20, iso-butane
Finishing column condenser 21, iso-butane finishing column reboiler 22, isomerization input and output material heat exchanger 23, isomery
Change feed heater 24, isomerization reactor 25, the raw material 26 of carbon four, periodic off-gases 27, hydrogenation supplement
Hydrogen 28, C2Product 29, C3Product 30, stable tower top fixed gas 31, iso-butane product 32, carbon
Quintet point 33, isomerization hydrogen make-up 34.
Embodiment
The preferred embodiment of the present invention is more fully described below with reference to accompanying drawings.
Iso-butane is produced using device as shown in Figure 1.
The process units of the iso-butane includes：Hydrogenation reactor 1, hydrogenation input and output material heat exchanger 2 plus
Hydrogen feed heater 3, hydrogenation separator, dethanizer 10, depropanizing tower 13, stabilizer 17,
Iso-butane finishing column 20, isomerization input and output material heat exchanger 23, isomerization feed heater 24 and isomery
Change reactor 25；Wherein,
Hydrogenation is connected after the feeding line of carbon four connection hydrogenation input and output material heat exchanger 2, hydrogenation feed heater 3
The top of reactor 1；
Connection hydrogenation hot knock-out pot 6 after the bottom of hydrogenation reactor 1 connection hydrogenation input and output material heat exchanger 2；Plus
The top of hydrogen hot knock-out pot 6 is sequentially connected hydrogenation aftercooler 4 and is hydrogenated with cold knockout drum 7, is hydrogenated with cold knockout drum
7 tops are sequentially connected after compressor suction tank 8, compressor 9 to be merged with the feeding line of carbon four, Ran Houlian
Connect hydrogenation input and output material heat exchanger 2；It is hydrogenated with the cold bottom of knockout drum 7 connection hydrogenation hot knock-out pot 6；
It is hydrogenated with the bottom of hot knock-out pot 6 connection dethanizer 10, the bottom of dethanizer 10 connection depropanizing tower
13, with carbon after isomerization reaction four after the bottom stable connection tower input and output material heat exchanger 16 of depropanizing tower 13
The pipeline that discharges merges stable connection tower 17；
Iso-butane finishing column 20 is connected after the bottom stable connection tower input and output material heat exchanger 16 of stabilizer 17,
The side line of iso-butane finishing column 20 is sequentially connected isomerization input and output material heat exchanger 23, isomerization heater 24
The entrance of isomerization reactor 25 is connected afterwards；
Stable connection tower 17 after the outlet of isomerization reactor 25 connection isomerization input and output material heat exchanger 23.
The method of production iso-butane includes：
(a) circulating hydrogen returned by the raw material 26 of carbon four out-of-bounds come with compressor is mixed into hydrogenation
Input and output material heat exchanger 2, then hydrogenated feed heater 3 are warming up to 240 DEG C, finally enter hydrogenation reaction
Micro organic sulfur nitrogen by olefins hydrogenation and is converted into H by device 12S and NH3；
(b) bottom discharge of hydrogenation reactor 1 after being cooled to 80 DEG C after hydrogenation charging heat exchange through with being introduced into
It is hydrogenated with hot knock-out pot 6 and carries out gas-liquid separation, top gas phase is after hydrogenation aftercooler 4 is cooled to 40 DEG C
Into cold knockout drum 7 is hydrogenated with, the cold top of knockout drum 7 connection compressor suction tank 8, bottom connection are hydrogenated with
It is hydrogenated with hot knock-out pot 6, hydrogenation hot knock-out pot 6 bottom liquid phases connection dethanizer 10.
It is hydrogenated with the cold top gas phase of knockout drum 7 and returns to hydrogenation reaction charging mostly as circulating hydrogen, and
Periodic off-gases 27 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 28 from out-of-bounds with the top gas body of compressor suction tank 8
Compressor 9 is combined into, enters hydrogenation input and output material heat exchange after being pressurized through compressor 9 together with the raw material of carbon four
Device 2；
(d) hydrogenation hot knock-out pot 6 bottoms material enters dethanizer 10, passes through rectifying separation top point
Go out the light component of carbon two；
(e) bottoms material of dethanizer 10 enters depropanizing tower 13, and top separates the liquid-phase product of carbon three,
Bottoms material is combined into surely after being exchanged heat through stabilizer input and output material heat exchanger 16 with carbon after isomerization reaction four
Determine tower 17；
(f) iso-butane is entered after the bottoms material of stabilizer 17 exchanges heat through stabilizer input and output material heat exchanger 16
Finishing column 20, obtains iso-butane product, tower reactor is obtained by rectifying separation by the top of iso-butane finishing column 20
To light dydrocarbon heavy constituent.
(g) by mixture and boundary of the side take-off of iso-butane finishing column 20 comprising normal butane and iso-butane
Outer fresh hydrogen is that isomerization hydrogen make-up 34 is mixed, by isomerization input and output material heat exchanger 23, isomery
Change feed heater 24 to be heated to after 180 DEG C entering isomerization reactor 25, herein convert normal butane
For iso-butane；
(h) material enters steady through the heat exchange Posterior circle of isomerization input and output material heat exchanger 23 after isomerization reaction
Determine tower 17, separated by rectifying, removed overhead H2、H2The light components such as S, tower reactor obtains positive iso-butane
Mixture.
Using following process conditions：
The hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 250 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 dethanizer includes：Pressure is 2.2MPaG, and tower top operation temperature is 60 DEG C,
The number of plates is 60, and reflux ratio is 10；
The operating condition of depropanizing tower includes：Pressure is 1.5MPaG, and tower top operation temperature is 50 DEG C,
The number of plates is 80, and reflux ratio is 20；
The operating condition of stabilizer includes：Pressure is 2.0MPaG, and tower top operation temperature is 85 DEG C, tower
Plate number is 60, 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 7；
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.In the case of without departing from the scope and spirit of illustrated each embodiment, led for this technology
Many modifications and changes will be apparent from for the those of ordinary skill in domain.
Claims (10)
1. a kind of process units of iso-butane, it is characterised in that：
Described device includes：Hydrogenation reactor, hydrogenation input and output material heat exchanger, hydrogenation feed heater,
Hydrogenation separator, dethanizer, depropanizing tower, stabilizer, iso-butane finishing column, isomerization are entered
Effluent exchanger, isomerization feed heater and isomerization reactor；Wherein,
Connection hydrogenation is anti-after the feeding line of carbon four connection hydrogenation input and output material heat exchanger, hydrogenation feed heater
Answer device top；
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；
Separator bottom connection dethanizer is hydrogenated with, Deethanizer bottom connection depropanizing tower takes off third
Merge company with the discharging pipeline of carbon after isomerization reaction four after alkane tower bottom stable connection tower input and output material heat exchanger
Connect stabilizer；
Connect iso-butane finishing column after stable tower bottom stable connection tower input and output material heat exchanger, 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；
Stable connection tower after isomerization reactor outlet connection isomerization input and output material heat exchanger.
2. the process units of iso-butane as claimed in claim 1, 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 dethanizer.
3. the process units of iso-butane as claimed in claim 1, 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 deethanization
Tower.
4. the process units of the 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 device using as described in any one in claim 1-4 produces the side of iso-butane
Method, it is characterised in that methods described includes：
The raw material of carbon four enters described device via the feeding line of carbon four, and isobutyl is made after hydrogenated, separation
Iso-butane is made after isomerization reaction, separation in alkane and normal butane, wherein normal butane, while by-product carbon
Three products.
6. the method for iso-butane is produced as claimed in claim 5, it is characterised in that methods described bag
Include：
(a) hydrogenation reactor is entered after the hydrogenated input and output material heat exchanger heat exchange of the raw material of carbon four out-of-bounds come
By olefins hydrogenation 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 enters dethanizer, led to
Cross rectifying separation top and separate the light component of carbon two；
(c) Deethanizer bottom material enters depropanizing tower, and top separates the liquid-phase product of carbon three, bottom
Material is combined into stabilizer after being exchanged heat through stabilizer input and output material heat exchanger with carbon after isomerization reaction four；
(d) iso-butane finished product is entered after stabilizer bottoms material exchanges heat through stabilizer 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；
(e) 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；
(f) with depropanizing tower after isomerization reactor bottom discharge exchanges heat through isomerization input and output material heat exchanger
Bottoms material is merged into stabilizer.
7. the method for iso-butane is produced as claimed in claim 6, it is characterised in that：
In step (a), the raw material of carbon four, which is heated to after 160~300 DEG C, enters hydrogenation reactor.
8. the method for iso-butane is produced as claimed in claim 6, 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 for iso-butane is produced as claimed in claim 6, 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 the production iso-butane as described in any one in claim 6-9, it is characterised in that：
The hydrogenation reactor is fixed bed reactors, and reactor inlet temperature is 160~300 DEG C, pressure
Power is 1.5~4.5MPaG, and reaction temperature rising is 5~100 DEG C, and hydrogen/oil mol ratio is 0.2~5, liquid bulk
Product air speed is 0.5~6h-1；
The operating condition of dethanizer includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
80 DEG C, the number of plates is 30~100, and reflux ratio is 1~20；
The operating condition of depropanizing tower includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
80 DEG C, the number of plates is 30~100, and reflux ratio is 1~20；
The operating condition of stabilizer includes：Pressure be 1~3MPaG, tower top operation temperature be 20~
100 DEG C, the number of plates is 30~100, 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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