CN106478337A - A kind of detached method of C4 olefin/paraffin - Google Patents
A kind of detached method of C4 olefin/paraffin Download PDFInfo
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- CN106478337A CN106478337A CN201510557360.6A CN201510557360A CN106478337A CN 106478337 A CN106478337 A CN 106478337A CN 201510557360 A CN201510557360 A CN 201510557360A CN 106478337 A CN106478337 A CN 106478337A
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Abstract
The invention discloses a kind of employing absorbing process separates the method for mixing C4 mixture of olefins/paraffins, which it is critical only that the adsorbent of high selectivity, and the adsorptive separation technology condition for optimizing, isobutene and 1- butylene product of the purity for 99wt.%～99.5wt% are obtained by the separation of absorption-rectifying coupling technique.The selective high, favorable regeneration effect of this method adsorbent, compared with the production method that reports, energy consumption is low, product purity and yield are all higher.
Description
Technical field
The present invention relates to a kind of method of separation containing C4 mixture of olefins/paraffins, its process is using absorption-essence
The technique for evaporating integrated separation.
Background technology
C-4-fraction is important petrochemical industry resource, and its utilization ways mainly includes to be used as fuel and chemical utilization.
Fuel utilization refers to the liquefied petroleum gas used directly as fuel without processing, mixes gasoline regulation vapour pressure
With through chemical process production high octane gasoline component etc., greatly waste is caused；Chemical utilization is referred to wherein
Including butadiene, 1- butylene, 2- butylene, isobutene, multiple chemical constituents such as normal butane and iso-butane profit
With, such as high-purity isobutylene be used for producing butyl rubber, methyl methacrylate, polyisobutene, nonyl phenol,
Multiple Organic Chemicals such as octyl phenol and fine chemistry product；And highly purified butene-1, can be used as high density
Polyethylene (HDPE) and polypropylene, the particularly comonomer of LLDPE (LLDPE), in state
Inside and outside have sizable demand.
As in C 4 fraction, each component boiling point is close to, rectification method is difficult to realize the separation of each component (as 1 institute of table
Show).Adsorptive separation technology can carry out selective absorption according to the adsorption selectivity of adsorbent to a certain component,
Then desorbed by methods such as intensification, step-down, inert media displacements, so as to realize the height between component
Degree is separated.Said method patent US 3723561, US4119678, US5365011, CN 200880010697.3,
CN 201110211936.5, CN 201110212879.2, CN200880024245.0 etc. with being reported,
But all there is complex process, energy consumption relatively.
The typical C 4 fraction physical property of table 1
| Component | Boiling point/DEG C | Relative volatility |
| Iso-butane | -11.73 | 1.13 |
| Isobutene | -6.9 | 1.005 |
| 1- butylene | -6.26 | 1.00 |
| 1,3-butadiene | -4.41 | 0.975 |
| Normal butane | -0.5 | 0.863 |
| Trans-2-butene | 0.88 | 0.830 |
| Cis-2-butene | 3.74 | 0.80 |
Content of the invention
The present invention is separated for C4 mixture of olefins/paraffins and obtains the problems of C4 monomer, it is desirable to provide
A kind of separation method of improved mixing C4 olefin/paraffin.The present invention can obtain highly purified isobutene and
1- butylene product.
The inventive method first by C4 mixture of olefins/paraffins pass through adsorption separation unit, linear alkene therein,
Alkane is adsorbed by the adsorbent of high selectivity, and branched-chain alkene not to be adsorbed, alkane are flowed out from adsorption separation unit；
To be adsorbed and the linear alkene on adsorbent, alkane desorption using the method for decompression, inert gas purge or displacement
Out；The branched-chain alkene obtained by adsorbing separation/alkane stream stock and linear alkene/alkane stream stock are due to each component
Between relative volatility increase, then carry out respectively rectifying separation can obtain highly purified isobutene and 1- butylene product.
A kind of detached method of C4 olefin/paraffin, its step are as follows：
(1) C4 mixture of olefins/paraffins initially enters adsorption separation unit, using multitower adsorption process, has
Body step is as follows：1. adsorb, under C4 mixture of olefins/paraffins gaseous state, enter the ADSORPTION IN A FIXED BED equipped with adsorbent
Tower, the linear alkene in charging, alkane are adsorbed the adsorbent absorption that load in tower, and not to be adsorbed props up alkene
Hydrocarbon, alkane are flowed out from adsorption column outlet, and the logistics is referred to as inhaling extraction raffinate；2. desorb, adsorption step is completed to above-mentioned
Adsorption tower desorbed, the logistics for desorbing is referred to as Extract；
It is that imidazate metalloid is organic that adsorption tower in the above-mentioned multitower absorbing unit for referring to is the adsorbent for loading
Framework material, metal ion include at least zinc, cobalt, iron, copper, chromium mercury and indium one kind therein, at least one
Described metal ion forms metal with least one described imidazoles, imdazole derivatives or purine coordination bonding to be had
Machine framework material, at least one imdazole derivatives have one or more independently selected from halogen, C1-C6
Alkyl, nitro, amino, NH (C1-6 alkyl), N (C1-6 alkyl)2, hydroxyl, phenyl, O- phenyl, O-C1-6
The substituent of alkyl, wherein substituent C1-C6 alkyl, phenyl are unsubstituted or only with least one or more
Halogen, amino, NH (C1-6 alkyl), N (C1-6 alkyl) are on the spot selected from2, hydroxyl, O- phenyl and O-C1-6
The substituent of alkyl；
(2) the suction extraction raffinate in step 1 is entered and inhales extraction raffinate knockout tower, and tower top obtains iso-butane component, and tower reactor is
Isobutyl olefinic constituent；
(3) Extract in step 1 enters Extract knockout tower, and tower top obtains 1- butene component, and tower reactor is
Heavy constituent.
Described C4 mixture of olefins/paraffins be steam cracking residual C4, catalytic cracking C4, coking C4,
After C4, MTBE ether of oil field, C4 contains the mixture of C4 olefin/paraffin component, and mixture at most contains
There is the 1,3-butadiene of 2000ppm weight.
Described adsorbent is the metal-organic framework materials of zinc ion and imidazoles coordination；Zinc ion and 2- hydroxyl miaow
The metal-organic framework materials of azoles coordination；The metallic organic framework of zinc ion, indium ion and 2-methylimidazole coordination
Material；The metal-organic framework materials that zinc ion is coordinated with 2- aminooimidazole；Cobalt ions is coordinated with 2- methyl azoles
Metal-organic framework materials；The metal-organic framework materials that indium ion is coordinated with purine；Mercury ion and 5- chlorobenzene
And the metal-organic framework materials of imidazoles coordination；The metallic organic framework material that chromium ion is coordinated with 4,5- dichloro-imidazole
Material；The metal-organic framework materials that copper ion is coordinated with benzimidazole.
Above-mentioned multitower adsorption separation process is constant temperature process, and operation temperature is 0-200 DEG C, adsorptive pressure 0
5MPa (absolute pressure), desorption pressures are 0 0.5MPa (absolute pressure), and the sorption cycle cycle is 0 60min；
The desorption method adopted by adsorption separation unit is：
(1) desorption is vacuumized；
(2) vacuumize while being desorbed with incoagulable gas purging, incoagulable gas is N2、H2、Ar、He、
CH4、CO2；
(3) vacuumize while with ammonia, vapor or ammonia and water vapour；
(4) C5～C8 linear paraffin displacement desorption is adopted.
In described C4 mixture of olefins/paraffins separating technology flow process, adsorption separation unit is multitower adsorbing separation
Flow process, at least provided with four ADSORPTION IN A FIXED BED towers.
Described step (1) is additionally included in absorption and increases equal pressure drop/all pressures between desorbing and rises and inverse put step,
Increase pressurising step after desorption procedure；
It is will to complete adsorption step and complete two adsorption towers of regeneration step that described equal pressure drop/all pressure rises step
UNICOM, the component remained in the former dead space is entered in the latter, until two pressure towers are of substantially equal, at this
During, the adsorption tower for completing adsorption step is equal pressure drop, and the adsorption tower for completing regeneration step is risen for all pressures；
After described inverse put step completes equal pressure drop for above-mentioned adsorption tower, against absorption direction by the absolute pressure of adsorption tower
Pressure is down to normal pressure 0.1MPa, described pressurising, completes, to above-mentioned, the absorption that all pressures rise step using extraction raffinate is inhaled
Tower carries out pressurising, and its pressure is risen to adsorptive pressure.
Beneficial effect：
The invention provides a kind of separate high added value component (isobutene and 1- butylene) in C 4 fraction.Isobutyl
Alkene and the method for 1- butylene, the method select type absorption property using adsorbent, first pass through adsorption separation unit reality
Clear separation between the existing close component of boiling point, further by the method for rectifying obtain highly purified isobutene with
1- butylene product.Compared with the detached adsorbent of the C4 having been reported, the present invention using imidazate metal have
Machine framework material adsorbent has aperture, structure is adjustable, specific surface is big, absorption big to C 4 fraction adsorbance
Feature can effectively improve the separative efficiency of C 4 fraction and the yield of product and purity to speed faster.
The adsorbent that prior art is adopted is substantially molecular sieve, the metallic organic framework adopted with the present invention
There is obvious difference in material sorbent.
The present invention obtains isobutene product content for 99wt.%～99.5wt.% by absorption-rectifying coupling technique,
N-butene product content is 99wt.%～99.5wt.%.
Description of the drawings
Fig. 1 is the detached schematic flow sheet of C4 olefin/paraffin of the present invention, wherein：A1 is adsorbing separation list
Unit；D1 inhales extraction raffinate knockout tower；D2 is Extract knockout tower；Stream stock 1 is C4 mixture of olefins/paraffins；2
For inhaling extraction raffinate；3 is Extract；4 is iso-butane component；5 is high-purity isobutylene product；6 is high-purity
1- butylene product；7 is Extract knockout tower tower reactor heavy constituent.
Specific embodiment
The technical process of 1 couple of present invention is illustrated below in conjunction with the accompanying drawings.C4 olefin/paraffin mixing 1 is entered first
Enter adsorption separation unit A1, under the conditions of 10～200 DEG C, 0.1～6MPa (absolute pressure), straight chain in charging
Alkene, alkane are adsorbed by adsorbent, and branched-chain alkene/alkane, i.e. suction excess oil 2 not to be adsorbed is entered and inhale excess oil
Knockout tower D1；Inhale excess oil knockout tower D1 tower top and iso-butane component 4 is obtained, bottom of towe obtains high-purity isobutylene 5；
In adsorption separation unit A1, the adsorption tower for completing adsorption process and two adsorption towers for completing regeneration step enter
Row all presses step, then adsorption column pressure is down to normal pressure 0.1MPa (absolute pressure) through inverse put step, then through taking out
Vacuum, or vacuumize while purge, or adsorbed linear alkene/alkane is desorbed by the mode of displacement desorption
Come, i.e., Extract 3 enters Extract knockout tower D2, Extract separates tower top and obtains highly purified 1- butylene product
Product 6, tower reactor produce heavy constituent 7；Pressurising is carried out to the above-mentioned adsorption tower for completing all pressure liter steps using extraction raffinate is inhaled,
Its pressure is risen to adsorptive pressure, is prepared to enter into next adsorption process.
Below by the example in detail present invention, but the range of application of the present invention is not limited by the following example
System.
Embodiment 1
It is raw material using the C4 mixture of olefins/paraffins shown in table 1, adsorbent is that zinc ion is coordinated with imidazoles
Metal-organic framework materials.
1 C4 mixture of olefins/paraffins of table constitutes
| Ingredient names | Composition wt./% |
| Iso-butane | 34 |
| Normal butane | 10 |
| Isobutene | 15 |
| 1- butylene | 13 |
| 2- butylene | 28 |
| Butadiene | <2000ppm |
Adsorption separation unit adopts four tower pressure-swing absorption processes, and the time of pressure swing adsorption cycles is 20min,
Wherein absorption 5min, equal pressure drop 2.5min, inverse put 2.5min, desorption 5min, all pressures rise 2.5min, pressurising
2.5min.Sorption cycle is constant temperature process, and temperature is 30 DEG C, adsorptive pressure 0.2MPa, desorbs true using taking out
Empty desorption, desorption pressures are 0.05MPa, inhale extraction raffinate and Extract respectively through suction extraction raffinate knockout tower and Extract
Knockout tower obtains the isobutene of 99.2wt.% and the 1- butylene product of 99.3wt.% after separating.
Embodiment 2
With embodiment 1, the metal that except for the difference that adsorbent is cobalt ions with 2- methyl azoles is coordinated is organic for other conditions
Framework material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.2wt.% and 99.3wt.%.
Embodiment 3
With embodiment 1, the metal that except for the difference that adsorbent is iron ion with 2- nitro azoles is coordinated is organic for other conditions
Framework material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.2wt.% and 99.3wt.%.
Embodiment 4
With embodiment 1, the metal that except for the difference that adsorbent is copper ion with benzimidazole is coordinated is organic for other conditions
Framework material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.2wt.% and 99.3wt.%.
Embodiment 5
Other conditions are the metal that chromium ion and 4,5- dichloro-imidazole are coordinated with embodiment 1, except for the difference that adsorbent
Organic framework material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
To the isobutene of 99.2wt.% and the 1- butylene product of 99.3wt.%.
Embodiment 6
Other conditions are the metal of mercury ion and the coordination of 5- chloro benzimidazole with embodiment 1, except for the difference that adsorbent
Organic framework material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
To the isobutene of 99.2wt.% and the 1- butylene product of 99.3wt.%.
Embodiment 7
Other conditions are the metallic organic framework of indium ion and purine coordination with embodiment 1, except for the difference that adsorbent
Material, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.2wt.% and 99.3wt.%.
Embodiment 8
Other conditions are the coordination of zinc ion, indium ion and 2-methylimidazole with embodiment 1, except for the difference that adsorbent
Metal-organic framework materials, the desorption of adsorption separation unit using vacuumizing while by the way of N2 purging, solution
Suction pressure power is 0.0.08MPa, inhales extraction raffinate and Extract and divides respectively through suction extraction raffinate knockout tower and Extract knockout tower
From after obtain the isobutene of 99.1wt.% and the 1- butylene product of 99.2wt.%.
Embodiment 9
Other conditions have with embodiment 1, the metal that except for the difference that adsorbent is coordinated with 2- aminooimidazole for zinc ion
Machine framework material, the desorption of adsorption separation unit using vacuumizing while by the way of steam purging, desorption pressures
For 0.1MPa, inhale extraction raffinate and Extract and obtain after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.4wt.% and 99.5wt.%.
Embodiment 10
Other conditions have with embodiment 1, the metal that except for the difference that adsorbent is coordinated with 2- hydroxy imidazole for zinc ion
Machine framework material, by the way of n-hexane displacement desorption, desorption pressures are for the desorption of adsorption separation unit
0.3MPa, inhales extraction raffinate and Extract and obtains after extraction raffinate knockout tower and the separation of Extract knockout tower respectively through inhaling
The 1- butylene product of the isobutene of 99.5wt.% and 99.5wt.%.
Claims (6)
1. a kind of detached method of C4 olefin/paraffin, its step are as follows：
(1) C4 mixture of olefins/paraffins initially enters adsorption separation unit, using multitower adsorption process, has
Body step is as follows：1. adsorb, under C4 mixture of olefins/paraffins gaseous state, enter the ADSORPTION IN A FIXED BED equipped with adsorbent
Tower, the linear alkene in charging, alkane are adsorbed the adsorbent absorption that load in tower, and not to be adsorbed props up alkene
Hydrocarbon, alkane are flowed out from adsorption column outlet, and the logistics is referred to as inhaling extraction raffinate；2. desorb, adsorption step is completed to above-mentioned
Adsorption tower desorbed, the logistics for desorbing is referred to as Extract；
It is imidazate metalloid organic backbone that adsorption tower in described multitower absorbing unit is the adsorbent for loading
Material, metal ion include at least zinc, cobalt, iron, copper, chromium mercury and indium one kind therein, at least one described
Metal ion and at least one described imidazoles, imdazole derivatives or purine coordination bonding form the organic bone of metal
Frame material, described at least one imdazole derivatives have one or more independently selected from halogen, C1-C6 alkyl,
Nitro, amino, NH (C1-6 alkyl), N (C1-6 alkyl)2, hydroxyl, phenyl, O- phenyl, O-C1-6 alkane
The substituent of base, wherein substituent C1-C6 alkyl, phenyl unsubstituted or carry at least one or more independence
Ground is selected from halogen, amino, NH (C1-6 alkyl), N (C1-6 alkyl)2, hydroxyl, O- phenyl and O-C1-6 alkane
The substituent of base；
(2) the suction extraction raffinate in step 1 is entered and inhales extraction raffinate knockout tower, and tower top obtains iso-butane component, and tower reactor is
Isobutyl olefinic constituent；
(3) Extract in step 1 enters Extract knockout tower, and tower top obtains 1- butene component, and tower reactor is
Heavy constituent.
2. method according to claim 1, it is characterised in that：Described C4 mixture of olefins/paraffins
Contain C4 for C4 after steam cracking residual C4, catalytic cracking C4, coking C4, oil field C4, MTBE ether
The mixture of olefin/paraffin component, and mixture contains up to the 1,3-butadiene of 2000ppm weight.
3. method according to claim 1, it is characterised in that：Described adsorbent is zinc ion and miaow
The metal-organic framework materials of azoles coordination；The metal-organic framework materials that zinc ion is coordinated with 2- hydroxy imidazole；Zinc
The metal-organic framework materials of ion, indium ion and 2-methylimidazole coordination；Zinc ion is joined with 2- aminooimidazole
The metal-organic framework materials of position；The metal-organic framework materials that cobalt ions is coordinated with 2- methyl azoles；Indium ion with
The metal-organic framework materials of purine coordination；The metal-organic framework materials that mercury ion is coordinated with 5- chloro benzimidazole；
The metal-organic framework materials that chromium ion is coordinated with 4,5- dichloro-imidazole；The metal that copper ion is coordinated with benzimidazole
Organic framework material.
4. according to method according to claim 1, it is characterised in that：Above-mentioned multitower adsorption separation process
For constant temperature process, operation temperature is 0-200 DEG C, and the absolute pressure of adsorptive pressure is 0 5MPa, desorption pressures
Absolute pressure is 0 0.5MPa, and the sorption cycle cycle is 0 60min；
The desorption method adopted by adsorption separation unit is：
(1) desorption is vacuumized；
(2) vacuumize while being desorbed with incoagulable gas purging, incoagulable gas is N2、H2、Ar、He、
CH4、CO2；
(3) vacuumize while with ammonia, vapor or ammonia and water vapour；
(4) C5～C8 linear paraffin displacement desorption is adopted.
5. method according to claim 1, it is characterised in that：Described C4 mixture of olefins/paraffins
In separating technology flow process, adsorption separation unit is multitower adsorbing separation flow process, at least provided with four ADSORPTION IN A FIXED BED towers.
6. method according to claim 1, it is characterised in that：Described step (1) is additionally included in suction
Echoing increases the pressure of equal pressure drop/all and rises and inverse put step between desorption, increase pressurising step after desorption procedure；
It is will to complete adsorption step and complete two adsorption towers of regeneration step that described equal pressure drop/all pressure rises step
UNICOM, the component remained in the former dead space is entered in the latter, until two pressure towers are of substantially equal, at this
During, the adsorption tower for completing adsorption step is equal pressure drop, and the adsorption tower for completing regeneration step is risen for all pressures；
After described inverse put step completes equal pressure drop for above-mentioned adsorption tower, against absorption direction by the absolute pressure of adsorption tower
Pressure is down to normal pressure 0.1MPa, described pressurising, completes, to above-mentioned, the absorption that all pressures rise step using extraction raffinate is inhaled
Tower carries out pressurising, and its pressure is risen to adsorptive pressure.
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| CN109422616A (en) * | 2017-08-22 | 2019-03-05 | 浙江大学 | A kind of method of the hybridization porous material separation C4 alkene of ultra micro ionic porogen |
| CN113474317A (en) * | 2018-12-18 | 2021-10-01 | 沙特基础工业全球技术公司 | Separation of olefinic components from mixtures of butanes and butenes using rectification and adsorbents |
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| WO2019037317A1 (en) * | 2017-08-22 | 2019-02-28 | 浙江大学 | Method for separating carbon tetraolefin mixture |
| CN109422616A (en) * | 2017-08-22 | 2019-03-05 | 浙江大学 | A kind of method of the hybridization porous material separation C4 alkene of ultra micro ionic porogen |
| CN109422616B (en) * | 2017-08-22 | 2020-09-08 | 浙江大学 | Method for separating C4 olefin from ultramicropore ion hybrid porous material |
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