CN104971695B - A kind of Gas Phase Adsorption separates C8The adsorbent of arene isomer and preparation and application - Google Patents
A kind of Gas Phase Adsorption separates C8The adsorbent of arene isomer and preparation and application Download PDFInfo
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Abstract
A kind of Gas Phase Adsorption separates C8The adsorbent of arene isomer, the binding agent of absorbed component and 0.5~20 mass % including 80~99.5 mass %, described absorbed component is sodium form MWW zeolites or NaZSM 5 or sodium form MWW zeolites through Si modification, described NaZSM 5 silica is 350~800 with alumina molar ratio, the silica of described sodium form MWW zeolites is at least 40 with alumina molar ratio, and the organo-silicon compound used in Si modification are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly- methylhydroxy siloxanes, poly- hydrosiloxane.The adsorbent has higher paraxylene and ethylbenzene selectivity and adsorption capacity.
Description
Technical field
The present invention is a kind of adsorbent and preparation method and application for adsorbing separation alkylaromatic isomer, specifically
Say, be that a kind of pressure-variable adsorption that is used for separates C8The adsorbent and preparation method of arene isomer and application.
Background technology
Paraxylene and ethylbenzene are all important basic chemical industry raw materials, and paraxylene is mainly for the production of p-phthalic acid
（PTA）And dimethyl terephthalate (DMT)（DMT）, and then polyester is produced, p-xylene purity requirement is at least 99.5%, preferably greatly
In 99.7%.For ethylbenzene mainly for the production of styrene, styrene is the important monomer of three big synthetic materials, mainly for the production of poly-
Styrene, ABS resin etc..
Simulated Moving Bed Adsorption Separation Technology production high-purity paraxylene is widely used in the prior art, utilizes adsorbent
The selection adsorption capacity different to mixed xylenes Isomers, exchanged by countercurrent mass transfer repeatedly, make paraxylene concentrate, then
Paraxylene is desorbed by strippant, Extract obtains high-purity para-xylene product after separating strippant by rectifying column；Take out
Excess oil be rich ethylbenzene, meta-xylene, ortho-xylene logistics, be sent into isomerization unit make which part ethylbenzene, meta-xylene and
Ortho-xylene is converted into paraxylene, is recirculated back to moving-bed adsorption separative element.USP2985589 is disclosed using inverse
The method of flow field simulation moving bed separating paraxylene；USP3686342, USP3734974, CN1137770C disclose adsorbing separation
The adsorbent used is X the or Y zeolites of barium type or potassium barium type；USP3558732, USP3686342 are respectively using toluene and to two
Desorbing agent of the ethylbenzene as adsorbing separation.
Industrial ethylbenzene is mainly produced by benzene alkylation with ethylene method.USP4169111A discloses vapor-phase alkylation production
The method of ethylbenzene, benzene enter alkylation reactor with gas phase, alkylate Returning reactor after isolating ethylbenzene, make generation
The more ethylbenzene of accessory substance and benzene carry out transalkylation reaction generation purpose product ethylbenzene.USP8217214B2 uses liquid-phase alkylation
With vapor-phase transalkylation technique productions ethylbenzene, benzene enters alkylation reactor with liquid phase, and product is ethylbenzene and the more ethylbenzene of accessory substance
Mixture, isolate and more ethylbenzene be sent into transalkylation reactor after ethylbenzene, transalkylation reaction is carried out under gas phase with benzene
Generate purpose product ethylbenzene.
USP6627783B2Disclose one kind and use pressure swing adsorption from C8The method of separating paraxylene in aromatic hydrocarbons.Should
Method is by pressure-variable adsorption by C8Aromatic hydrocarbons is divided into the logistics containing meta-xylene and ortho-xylene, and paraxylene content is less than in the logistics
C8The 20mol% of contained paraxylene amount in aromatic hydrocarbons；The paraxylene of absorption and ethylbenzene are desorbed and produce the thing rich in paraxylene
The amount of stream, meta-xylene contained therein and ortho-xylene is less than C8The 50mol% of the two total amount in aromatic hydrocarbons.
CN200480011667.6 discloses a kind of Selectivity for paraxylene adsorbent composition and method, sorbent used
Molecular sieve including catalytically inactive, hasOrThe hole size of scope, radius is more than 60nm macropore hole in composition
Volume is at least 0.2ml/g, preferably 0.35ml/g, and mesopore volume of the radius less than 60nm is less than 0.2ml/g, the two volume ratio
At least 2, most preferably greater than 10, binding agent are selected from the materials such as clay, silica, zirconium oxide, binder content preferably 20 weights
Measure %.
Above-mentioned pressure-variable adsorption separation mixing C8The problem of aromatic hydrocarbons technology is present be：Due to C8Four kinds of isomer molecule chis of aromatic hydrocarbons
Very little close, adsorbent is relatively low to the separation of paraxylene, ethylbenzene and meta-xylene, ortho-xylene, pressure-variable adsorption desorption thing
In meta-xylene and ortho-xylene content it is higher, the adsorption capacity of adsorbent is relatively low.
The content of the invention
It is an object of the invention to provide one kind to be used for pressure-variable adsorption separation C8The adsorbent of arene isomer and its modification side
Method, the adsorbent have higher paraxylene and ethylbenzene selectivity and adsorption capacity.
Gas Phase Adsorption provided by the invention separates C8The adsorbent of arene isomer, include 80~99.5 mass % absorption
The binding agent of component and 0.5~20 mass %, described absorbed component are sodium form MWW zeolites, NaZSM-5 or sodium through Si modification
Type MWW zeolites, described NaZSM-5 silica and alumina molar ratio are 350~800, the oxygen of described sodium form MWW zeolites
SiClx is at least 40 with alumina molar ratio, and the organo-silicon compound used in Si modification are selected from octamethylcy-clotetrasiloxane, poly- two
Methylsiloxane, poly- methylhydroxy siloxanes, poly- hydrosiloxane.
NaZSM-5 or sodium form MWW zeolite of the adsorbent of the present invention using sodium form MWW zeolites or through Si modification as absorbed component,
For C8The Gas Phase Adsorption separation of arene isomer, there is the adsorptive selectivity of higher paraxylene and ethylbenzene, substantially not
In raw material containing paraxylene, there is more preferable adsorptive selectivity to ethylbenzene.
Embodiment
The present invention is using sodium form MWW zeolites or the NaZSM-5 through Si modification or sodium form MWW zeolites is absorbed components, is equipped with viscous
Adsorbent is made in knot agent.For the zeolite component through Si modification, due to having selected suitable silica modifier, zeolite can be effectively improved
Port size, be allowed to be more suitable for adsorb C8Ethylbenzene and paraxylene in aromatic hydrocarbons, improve adsorptive selectivity and the suction of adsorbent
Attached capacity.
Absorbed component described in adsorbent of the present invention is sodium form MWW zeolites or the NaZSM-5 through Si modification or sodium form MWW boilings
Stone.Described MWW zeolites include MCM-22, ITQ-1, SSZ-25, PSH-3, MCM-49 zeolite and containing heteroatomic ERB-1,
[Ga-Si-O]-MWW, one kind in [Ti-Si-O]-MWW zeolites or their mixture, preferably MCM-22, ITQ-1 zeolite.
The preferred NaMCM-22 zeolites of sodium form MWW zeolites of the present invention, wherein silica/oxidation of NaMCM-22 zeolites
Al mole ratio is preferably 40~200, more preferably 40~100.The described NaZSM-5 zeolites through Si modification are high silica alumina ratio
NaZSM-5 zeolites, its silica/alumina molar ratio are preferably 350~650.
Described binding agent be selected from kaolin, bentonite, attapulgite, aluminum oxide, magnesia, zirconium oxide, titanium dioxide,
In at least one of boron oxide and silica or the material it is any two or more.
Described adsorbent preferably includes 85~99.5 mass % absorbed component and 0.5~15 mass % binding agent.
In the inventive method, when the absorbed component of the adsorbent is sodium form MWW zeolites, its preparation method is included sodium
Type MWW zeolites are with after binding agent mixed-forming, drying, roasting, the described silica of sodium form MWW zeolites and mole of aluminum oxide
Than being at least 40.
When the absorbed component of the adsorbent is the NaZSM-5 or sodium form MWW zeolites through Si modification, the preparation of adsorbent
Method preferably includes, by sodium form MWW zeolites or NaZSM-5 and binding agent mixed-forming, to dry, use organo-silicon compound after roasting
Dipping, gained solid after dipping is dried, is calcined in 200~600 DEG C in air atmosphere, is calcined the volume of air air speed being passed through
For 90~300h-1, described organo-silicon compound are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly- methylhydroxy
Siloxanes, poly- hydrosiloxane, described NaZSM-5 silica and alumina molar ratio are 350~800, described sodium form
The silica of MWW zeolites and the mol ratio of aluminum oxide are at least 40.
In the above method, preferably 80~120 DEG C of the drying temperature of adsorbent after shaping, sintering temperature is 500~650 DEG C.
Adsorbent-shaping method of the present invention can be arbitrary adsorbent-shaping method, including squeeze in the prior art
Bar, tabletting, spin, forming oil column, the present invention are without limitation.
The organo-silicon compound that the present invention is used for Si modification are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, gathered
Methylhydroxy siloxanes, poly- hydrosiloxane.Described dimethyl silicone polymer, poly- methylhydroxy siloxanes or poly- hydroxyl silica
The molecular weight of alkane preferably 800~4000, more preferably 1000~3000.
In above-mentioned Si modification method, the temperature that the adsorbent after described shaping is impregnated with organo-silicon compound is preferably 15
~40 DEG C, liquid/solid volume ratio is 1~2 during dipping：1st, preferably 1.0~1.5：1, the drying temperature of gained solid is preferred after dipping
90~120 DEG C, after drying, be calcined in 200~600 DEG C in air atmosphere, be calcined the volume of air air speed preferably 95 that is passed through~
250h-1.Preferable method is that gained solid is dried after being impregnated with organo-silicon compound, then divides two-stage roasting, prior to 200~
300 DEG C of roastings, then it is warming up to 450~600 DEG C of progress two-stage calcinations.Roasting time preferably 1~6 hour, more preferably 1~3 hour.
The present invention is adsorbent separating property is reached optimal, it is necessary to consider para-selectivity and the absorption of adsorbent
Capacity, to different silica modifiers, the different modified numbers of silicon dipping can be used.
When being modified with octamethylcy-clotetrasiloxane, dipping time preferably 2~3 times, gained solid after impregnating every time
It is both needed to be calcined in atmosphere, preferably 200~600 DEG C of sintering temperature, it is preferred to use above-mentioned two-stage roasting.
When being modified with dimethyl silicone polymer, poly- methylhydroxy siloxanes or poly- hydrosiloxane, dipping time
It is preferred that 1~2 time, gained solid is both needed to be calcined in atmosphere after dipping every time, preferably 200~600 DEG C of sintering temperature, it is preferred to use
Above-mentioned two-stage roasting.
Pressure-variable adsorption separation operating method is carried out with adsorbent provided by the invention, including by C8Aromatic hydrocarbons is led to gas phase state
Enter the adsorption bed of adsorbent of the present invention is housed, adsorbed under conditions of 170~330 DEG C, 0.4~1.3MPa therein to diformazan
Benzene and ethylbenzene or ethylbenzene, the suction excess containing meta-xylene and ortho-xylene is obtained, the use of inert gas is purge gass purging absorption
Agent bed, the component in the non-selective volume of bed is blown out as intermediate species, 0.1~0.3MPa is depressurized to, is extracted out
Thing.
Preferably 190~300 DEG C, more preferably 210~280 DEG C of the adsorption temp of above-mentioned pressure-variable adsorption, adsorptive pressure preferably 0.4
~1.0MPa, under adsorptive pressure, temperature will ensure that charging is gas phase state, feedstock quality air speed preferably 0.2~30h-1, it is more excellent
Select 3~6h-1。
The preferred nitrogen of inert gas, hydrogen, carbon dioxide, methane, ethane, propane or the argon gas of described purging bed,
More preferably nitrogen, purge gass dosage are 1~20 times, preferably 3~10 times of non-selective volume in adsorbent bed.Desorption pressure is preferred
0.1~0.2MPa.The intermediate species for purging adsorbent bed gained is essentially feed composition, is recycled entering as pressure-variable adsorption
Material.
Above-mentioned C8Aromatic hydrocarbons can be the mixing C obtained by catalytic reforming, steam cracking or disproportionation with devices such as transalkylations8
Aromatic hydrocarbons or by above-mentioned mixing C8Remaining ingredient after aromatics seperation paraxylene, the C8Non-aromatics contains in aroamtic hydrocarbon raw material
Amount is preferably smaller than 20 mass %.
When to mix C8When aromatic hydrocarbons is as raw material, paraxylene and ethylbenzene are extracted out collectively as extract, inhale base in excess
This be free of paraxylene and ethylbenzene, using adsorbent of the present invention advantage in it can improve extract paraxylene with
The content of ethylbenzene, reduce meta-xylene, the content of ortho-xylene.Extract, which can be used as moving-bed adsorption separation or crystallize, to be divided
From the raw material of p-Xylene unit, due to the raising of paraxylene content in extract, be advantageous to adsorbing separation or crystallization process,
And inhale and paraxylene and ethylbenzene be substantially free of in excess, can reduce xylene isomerization process reaction severity, reduce hydrogen/
Hydrocarbon ratio, and the internal circulating load in Aromatic Hydrocarbon United Plant is reduced, reduce energy consumption.
C after with separating paraxylene8When aromatic hydrocarbons is raw material, it can be significantly reduced using adsorbent of the present invention
The content of meta-xylene and ortho-xylene in extract, extract can obtain high purity ethylbenzene production after separating a small amount of non-aromatics
Product.
The present invention is further illustrated below by example, but the present invention is not limited thereto.
Example 1
The NaMCM-22 zeolite powders and kaolin that silica/alumina molar ratio is 50 are taken by 96：4 mass ratio mixes
Close, roller forming, it is 0.3~0.8 millimeter of spheric granules to take particle diameter, 90 DEG C of drying 4 hours, 520 DEG C of roastings 6 hours, must be inhaled
Attached dose of A, wherein the NaMCM-22 zeolites containing 96 mass %, 4 mass % kaolin.
Example 2
Adsorbent A is taken, is modifying agent with octamethylcy-clotetrasiloxane, is impregnated 12 hours in 25 DEG C.Prestox ring four used
The liquid/solid volume ratio of siloxanes and adsorbent A is 1.3：1, filter after dipping, gained solid is dried 5 hours in 95 DEG C, then is placed in
In activation furnace, air is passed through, is 95h in volume of air air speed-1Under conditions of be calcined 2 hours in 250 DEG C, then be warming up to 530 DEG C
Roasting 2 hours, adsorbent A -1 is made.
Take adsorbent A -1 to repeat above-mentioned Si modification step, the adsorbent A -2 that modified number is 2 is made.
Repeat above-mentioned Si modification step twice, the adsorbent A -3 that modified number is 3 is made.
Example 3
Adsorbent B is prepared by the method for example 1, the difference is that using the NaMCM- that silica/alumina molar ratio is 80
22 zeolite powders prepare adsorbent, and NaMCM-22 zeolite powders and kaolin are pressed into 94：6 mass ratio mixing, obtained suction
Attached dose of B contains 94 mass % NaMCM-22 zeolites, 6 mass % kaolin.
Example 4
Adsorbent B is taken, the dimethyl silicone polymer for being 1300 with molecular weight is silica modifier, is impregnated 12 hours in 25 DEG C.
The liquid/solid volume ratio of dimethyl silicone polymer used and adsorbent B is 1.2：1, filter after dipping, gained solid is dry in 110 DEG C
Dry 5 hours, then be placed in activation furnace, air is passed through, is 150h in volume of air air speed-1Under conditions of it is 2 small in 250 DEG C of roastings
When, then be warming up to 530 DEG C and be calcined 2 hours, adsorbent B -1 is made.
Above-mentioned Si modification step is repeated, the adsorbent B -2 that modified number is 2 times is made.
Comparative example 1
The NaZSM-5 zeolite powders that silica/alumina molar ratio is 450 are pressed 90 with kaolin：10 mass ratio mixes
Close, roller forming, it is 0.3~0.8 millimeter of spheric granules to take particle diameter, and 90 DEG C of drying 4 hours, 520 DEG C are calcined 6 hours and must adsorb
Agent C, wherein the NaZSM-5 zeolites containing 90 mass %, 10 mass % kaolin.
Example 5
Adsorbent C is modified by the method for example 2, carrying out 1 Si modification with octamethylcy-clotetrasiloxane is made suction
Attached dose of C-1, carry out 2 Si modifications and adsorbent C-2 is made.
Comparative example 2
Adsorbent is prepared by the method for comparative example 1, the difference is that using the Na- that silica/alumina molar ratio is 600
ZSM-5 zeolite original powder prepares adsorbent, and by NaZSM-5 zeolite powders and kaolin according to 85：15 mass ratio mixing, is made
Adsorbent D contain 85 mass % NaZSM-5 zeolites, 15 mass % kaolin.
Example 6
Adsorbent D is taken, the poly- hydrosiloxane for being 2500 with molecular weight is silica modifier, is impregnated 8 hours in 25 DEG C.It is used
Poly- hydrosiloxane and adsorbent D liquid/solid volume ratio are 1.3：1, filter after dipping, it is small that gained solid in 115 DEG C dries 6
When, then be placed in activation furnace, air is passed through, is 200h in volume of air air speed-1Under conditions of be calcined 3 hours in 300 DEG C, then rise
Warm to 530 DEG C are calcined 2 hours, and adsorbent D-1 is made.
Comparative example 3
Silicalite-1 zeolite powders and kaolin are pressed 95：5 mass ratio mixing, roller forming, it is 0.3 to take particle diameter
~0.8 millimeter of spheric granules, 90 DEG C of dryings 4 hours, 520 DEG C of roastings, 6 hours obtained adsorbent E, wherein containing 95 mass %'s
The kaolin of Silicalite-1 zeolites, 5 mass %.
Example 7~15
Following instance evaluates the absorption property of adsorbent of the present invention and contrast adsorbent.
69 grams of adsorbents are loaded in the adsorption column that ratio of height to diameter is 15, in 250 DEG C of temperature, pressure 0.70MPa, quality
Air speed is 4.5h-1Under conditions of, adsorption column will be passed through after material gasification, collects component not to be adsorbed to inhale excess.Use pressure
Bed is purged for 0.70MPa nitrogen, nitrogen used in purging is 6 times of non-selective volume in adsorption bed, is depressurized to
0.1MPa, and adsorption bed is purged with nitrogen, make adsorbed component desorption, the desorption component of collection is extract.Absorption used
The composition of raw material is the mass % of ethylbenzene 12.24, the mass % of paraxylene 18.65, the mass % of meta-xylene 45.73, ortho-xylene
21.58 mass %, non-aromatics are 1.8 mass %.Each example sorbent used numbering, adsorbent selectivity and adsorption capacity are shown in Table 1.
In table 1, adsorbent is selectively calculated by following formula.
Example 16~19
Performance of the adsorbent is evaluated by the method for example 7, unlike 265 DEG C of temperature, pressure 0.85MPa,
Mass space velocity is 5.0h-1Under conditions of, adsorption column will be passed through after absorption material gasification, it is more than suction to collect component not to be adsorbed
Thing, the nitrogen for being 0.85MPa with pressure purge bed, and nitrogen used in purging is 4 times of non-selective volume in adsorption bed, is dropped
0.1MPa is depressed into, and adsorption bed is purged with nitrogen, makes adsorbed component desorption, the desorption component of collection is extract.Each reality
Example sorbent used numbering, adsorbent selectivity and adsorption capacity are shown in Table 2.
Example 20~26
To be substantially free of the C of paraxylene8Aromatic hydrocarbons is absorption raw material, and raw materials used composition is the mass % of ethylbenzene 18.58, right
The mass % of dimethylbenzene 0.082, the mass % of meta-xylene 53.74, the mass % of ortho-xylene 24.47, the mass % of non-aromatics 3.128.
69 grams of adsorbents are loaded in the adsorption column that ratio of height to diameter is 15, in 233 DEG C of temperature, pressure 0.55MPa, quality
Air speed is 4.0h-1Under conditions of, adsorption column will be passed through after above-mentioned absorption material gasification, it is more than suction to collect component not to be adsorbed
Thing, the nitrogen for being 0.55MPa with pressure purge bed, and nitrogen used in purging is 5 times of non-selective volume in adsorption bed, so
After be depressurized to 0.1MPa, and purge adsorption bed with nitrogen, make adsorbed component desorption, the desorption component of collection is extract,
The non-aromatics in extract is distilled off, obtains ethylbenzene.The sorbent used numbering of each example, adsorbent selectivity, adsorption capacity,
Extract ethylbenzene purity is shown in Table 3.
In table 3, ethylbenzene selectivity is calculated by following formula.
Table 1
Table 2
Table 3
Claims (16)
1. a kind of Gas Phase Adsorption separates C8The adsorbent of arene isomer, including 80~99.5 mass % absorbed component and 0.5~
20 mass % binding agent, described absorbed component are NaMCM-22 zeolites, the NaZSM-5 through Si modification or NaMCM-22 boilings
Stone, described NaZSM-5 silica are 350~800 with alumina molar ratio, the silica of described NaMCM-22 zeolites with
The mol ratio of aluminum oxide is 40~100, and the organo-silicon compound used in Si modification are selected from octamethylcy-clotetrasiloxane, poly dimethyl
The molecular weight of siloxanes, poly- hydrosiloxane, described dimethyl silicone polymer or poly- hydrosiloxane is 800~4000.
2. according to the adsorbent described in claim 1, it is characterised in that described binding agent is kaolin, bentonite, concave convex rod
At least one of soil, aluminum oxide, magnesia, zirconium oxide, titanium dioxide, boron oxide and silica.
3. according to the adsorbent described in claim 1, it is characterised in that described adsorbent includes 85~99.5 mass % suction
The binding agent of attached component and 0.5~15 mass %.
4. according to the adsorbent described in claim 1, it is characterised in that described dimethyl silicone polymer or poly- hydrosiloxane
Molecular weight be 1000~3000.
5. according to the adsorbent described in claim 1 or 4, it is characterised in that described poly- hydrosiloxane is poly- methylhydroxy silicon
Oxygen alkane.
6. a kind of preparation method of the adsorbent described in claim 1, including by NaMCM-22 zeolites and binding agent mixed-forming
Afterwards, dry, be calcined, silica and the alumina molar ratio of described NaMCM-22 zeolites are 40~100.
7. the preparation method of adsorbent described in a kind of claim 1, including NaMCM-22 zeolites or NaZSM-5 are mixed with binding agent
Synthesis type, dry, impregnated after roasting with organo-silicon compound, gained solid after dipping is dried, in 200~600 DEG C in air
It is calcined in atmosphere, it is 90~300h to be calcined the volume of air air speed being passed through-1, described organo-silicon compound are selected from prestox ring four
Siloxanes, dimethyl silicone polymer, poly- hydrosiloxane, described NaZSM-5 silica and alumina molar ratio be 350~
800, the silica of described NaMCM-22 zeolites and the mol ratio of aluminum oxide are 40~100, described dimethyl silicone polymer
Or the molecular weight of poly- hydrosiloxane is 800~4000.
8. according to the method described in claim 6 or 7, it is characterised in that the sintering temperature after shaping is 500~650 DEG C.
9. in accordance with the method for claim 7, it is characterised in that described dimethyl silicone polymer or poly- hydrosiloxane
Molecular weight is 1000~3000.
10. in accordance with the method for claim 7, it is characterised in that gained solid is dried after being impregnated with organo-silicon compound,
In 200~300 DEG C of roastings, then it is warming up to 450~600 DEG C of roastings.
11. in accordance with the method for claim 7, it is characterised in that when being modified with octamethylcy-clotetrasiloxane, dipping
Number is 2~3 times, and gained solid is both needed to be calcined in atmosphere after dipping every time.
12. in accordance with the method for claim 7, it is characterised in that carried out when with dimethyl silicone polymer or poly- hydrosiloxane
When modified, dipping time is 1~2 time, and gained solid is both needed to be calcined in atmosphere after dipping every time.
13. according to the method described in claim 7,9 or 12, it is characterised in that described poly- hydrosiloxane is poly- methylhydroxy
Siloxanes.
14. a kind of Gas Phase Adsorption separates C8The method of arene isomer, including by C8Aromatic hydrocarbons is passed through with gas phase state will equipped with right
Seek the adsorption bed of 1 adsorbent, adsorbed under conditions of 170~330 DEG C, 0.4~1.3MPa paraxylene therein and
Ethylbenzene, or ethylbenzene, obtain the suction excess containing meta-xylene and ortho-xylene, purged using purge gass it is adsorbent bed, by bed
Component blowout in non-selective volume is used as intermediate species, is depressurized to 0.1~0.3MPa, obtains extract.
15. in accordance with the method for claim 14, it is characterised in that described purge gass are nitrogen, hydrogen, carbon dioxide, first
Alkane, ethane, propane or argon gas.
16. in accordance with the method for claim 14, it is characterised in that purge gass used are 1 of non-selective volume in adsorbent bed
~20 times.
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| US10717035B2 (en) * | 2017-02-13 | 2020-07-21 | Praxair Technology, Inc. | Tunable adsorbents |
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| CN114160096B (en) * | 2022-02-08 | 2022-05-17 | 中海油天津化工研究设计院有限公司 | Adsorbent for separating ethylbenzene from carbon octa-aromatic hydrocarbons and preparation method thereof |
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