CN104971695A - Adsorbent for gas-phase adsorption separation of C8 aromatic hydrocarbon isomer as well as preparation and application - Google Patents
Adsorbent for gas-phase adsorption separation of C8 aromatic hydrocarbon isomer as well as preparation and application Download PDFInfo
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Abstract
The invention relates to an adsorbent for gas-phase adsorption separation of a C8 aromatic hydrocarbon isomer. The adsorbent comprises 80-99.5% by mass of an adsorption component and 0.5-20% by mass of a binder, wherein the adsorption component is sodium-type MWW zeolite or NaZSM-5 or sodium-type MWW zeolite which is modified by silicon, and the mole ratio of silicon oxide to aluminum oxide of NaZSM-5 zeolite is 350-800, the mole ratio of silicon oxide to aluminum oxide of the sodium-type MWW zeolite is at least 40, an organic silicon compound for silicon modification is selected from octamethylcyclotetrasiloxane, polydimethylsiloxane, polymethylhydroxysiloxane and polyhydroxysiloxane. The adsorbent has high selectivity and adsorption capacity on p-xylene and ethylbenzene.
Description
Technical field
The present invention is a kind of adsorbent for adsorbing separation alkylaromatic isomer and preparation method and application, specifically, is a kind of for pressure-variable adsorption separation of C
8the adsorbent of arene isomer and preparation method and application.
Background technology
Paraxylene and ethylbenzene are all important basic chemical industry raw materials, and paraxylene mainly for the production of p-phthalic acid (PTA) and dimethyl terephthalate (DMT) (DMT), and then produces polyester, and p-xylene purity requires to be at least 99.5%, is preferably greater than 99.7%.Ethylbenzene is mainly for the production of styrene, and styrene is the important monomer of three large synthetic materials, mainly for the production of polystyrene, ABS resin etc.
Simulated Moving Bed Adsorption Separation Technology production high-purity paraxylene is widely used in prior art, utilize the adsorption selection ability that adsorbent is different to mixed xylenes Isomers, through countercurrent mass transfer exchange repeatedly, make paraxylene concentrate, again by strippant desorb paraxylene, Extract obtains high-purity para-xylene product after being separated strippant by rectifying column; Raffinate oil as the logistics of rich ethylbenzene, meta-xylene, ortho-xylene, send into isomerization unit and make wherein part ethylbenzene, meta-xylene and ortho-xylene be converted into paraxylene, recycle back moving-bed adsorption separative element.USP2985589 discloses the method adopting the simulation moving-bed separating paraxylene of adverse current; USP3686342, USP3734974, CN1137770C disclose X or the Y zeolite that adsorbent that adsorbing separation uses is barium type or potassium barium type; USP3558732, USP3686342 use toluene and p-Diethylbenzene as the desorbing agent of adsorbing separation respectively.
Industrial ethylbenzene is produced primarily of benzene alkylation with ethylene method.USP4169111A discloses the method that vapor-phase alkylation produces ethylbenzene, benzene enters alkylation reactor with gas phase, alkylate is Returning reactor after isolating ethylbenzene, makes the many ethylbenzene of the accessory substance of generation and benzene carry out transalkylation reaction and generates object product ethylbenzene.USP8217214B2 adopts liquid-phase alkylation and vapor-phase transalkylation explained hereafter ethylbenzene, benzene enters alkylation reactor with liquid phase, product is the mixture of ethylbenzene and the many ethylbenzene of accessory substance, after isolating ethylbenzene, many ethylbenzene is sent into transalkylation reactor, under gas phase, carry out transalkylation reaction with benzene and generate object product ethylbenzene.
USP6627783B
2disclose a kind of pressure swing adsorption that uses from C
8the method of separating paraxylene in aromatic hydrocarbons.This method by pressure-variable adsorption by C
8aromatic hydrocarbons is divided into the logistics containing meta-xylene and ortho-xylene, and in this logistics, paraxylene content is less than C
8the 20mol% of contained paraxylene amount in aromatic hydrocarbons; Namely the paraxylene of absorption and ethylbenzene desorption are obtained the logistics being rich in paraxylene, and wherein contained meta-xylene and the amount of ortho-xylene are less than C
8the 50mol% of the two total amount in aromatic hydrocarbons.
CN200480011667.6 discloses a kind of Selectivity for paraxylene adsorbent composition and method, and the sorbent used molecular sieve comprising catalytically inactive, has
or
the hole size of scope, the macropore pore volume that in composition, radius is greater than 60nm is at least 0.2ml/g, preferred 0.35ml/g, the mesopore volume that radius is less than 60nm is less than 0.2ml/g, the two volume ratio is at least 2, most preferably be greater than 10, binding agent is selected from the materials such as clay, silica, zirconia, binder content preferably 20 % by weight.
Above-mentioned pressure-variable adsorption is separated mixed C
8aromatic hydrocarbons technology Problems existing is: due to C
8aromatic hydrocarbons four kinds of isomer molecule sizes are close, and the separation of adsorbent to paraxylene, ethylbenzene and meta-xylene, ortho-xylene is lower, the meta-xylene in pressure-variable adsorption desorption thing and ortho-xylene content higher, the adsorption capacity of adsorbent is lower.
Summary of the invention
The object of this invention is to provide a kind of for pressure-variable adsorption separation of C
8the adsorbent of arene isomer and method of modifying thereof, this adsorbent has higher paraxylene and ethylbenzene selectivity and adsorption capacity.
Gas Phase Adsorption separation of C provided by the invention
8the adsorbent of arene isomer, comprise the absorbed component of 80 ~ 99.5 quality % and the binding agent of 0.5 ~ 20 quality %, described absorbed component is sodium form MWW zeolite, through the NaZSM-5 of Si modification or sodium form MWW zeolite, the silica of described NaZSM-5 and alumina molar ratio are 350 ~ 800, silica and the alumina molar ratio of described sodium form MWW zeolite are at least 40, and Si modification organo-silicon compound used are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly-methylhydroxy siloxanes, poly-hydrosiloxane.
Adsorbent of the present invention with sodium form MWW zeolite or through the NaZSM-5 of Si modification or sodium form MWW zeolite for absorbed component, for C
8the Gas Phase Adsorption of arene isomer is separated, and has higher paraxylene and the adsorptive selectivity of ethylbenzene, substantially not containing in the raw material of paraxylene, has better adsorptive selectivity to ethylbenzene.
Detailed description of the invention
The present invention with sodium form MWW zeolite or through the NaZSM-5 of Si modification or sodium form MWW zeolite for absorbed component, be equipped with binding agent and make adsorbent.For the zeolite component through Si modification, owing to having selected suitable silica modifier, effectively can improve the port size of zeolite, make it to be more suitable for adsorbing C
8ethylbenzene in aromatic hydrocarbons and paraxylene, improve adsorptive selectivity and the adsorption capacity of adsorbent.
Absorbed component described in adsorbent of the present invention is sodium form MWW zeolite or through the NaZSM-5 of Si modification or sodium form MWW zeolite.Described MWW zeolite comprises MCM-22, ITQ-1, SSZ-25, PSH-3, MCM-49 zeolite and containing heteroatomic ERB-1, [Ga-Si-O]-MWW, a kind of in [Ti-Si-O]-MWW zeolite or their mixture, preferred MCM-22, ITQ-1 zeolite.
The preferred NaMCM-22 zeolite of sodium form MWW zeolite of the present invention, wherein the silica/alumina molar ratio of NaMCM-22 zeolite is preferably 40 ~ 200, more preferably 40 ~ 100.The described NaZSM-5 zeolite through Si modification is the NaZSM-5 zeolite of high silica alumina ratio, and its silica/alumina molar ratio is preferably 350 ~ 650.
Described binding agent is selected from least one in kaolin, bentonite, attapulgite, aluminium oxide, magnesia, zirconia, titanium dioxide, boron oxide and silica, also can be in described material any two or more.
Described adsorbent preferably includes the absorbed component of 85 ~ 99.5 quality % and the binding agent of 0.5 ~ 15 quality %.
In the inventive method, when the absorbed component of described adsorbent is sodium form MWW zeolite, its preparation method comprises after sodium form MWW zeolite and binding agent mixed-forming, and dry, roasting, the described silica of sodium form MWW zeolite and the mol ratio of aluminium oxide are at least 40.
When the absorbed component of described adsorbent is through the NaZSM-5 of Si modification or sodium form MWW zeolite, the preparation method of adsorbent preferably includes sodium form MWW zeolite or NaZSM-5 and binding agent mixed-forming, flood with organo-silicon compound after drying, roasting, gained solid drying after flooding, in 200 ~ 600 DEG C of roastings in air atmosphere, the volume of air air speed that roasting passes into is 90 ~ 300h
-1described organo-silicon compound are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly-methylhydroxy siloxanes, poly-hydrosiloxane, the silica of described NaZSM-5 and alumina molar ratio are 350 ~ 800, and the described silica of sodium form MWW zeolite and the mol ratio of aluminium oxide are at least 40.
In said method, the baking temperature of shaping rear adsorbent preferably 80 ~ 120 DEG C, sintering temperature is 500 ~ 650 DEG C.
Adsorbent-shaping method of the present invention can be arbitrary adsorbent-shaping method in prior art, and comprise extrusion, compressing tablet, spin, forming oil column, the present invention does not limit this.
The organo-silicon compound that the present invention is used for Si modification are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly-methylhydroxy siloxanes, poly-hydrosiloxane.The molecular weight of described dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane preferably 800 ~ 4000, more preferably 1000 ~ 3000.
In above-mentioned Si modification method, 15 ~ 40 DEG C are preferably by the temperature of adsorbent after shaping described in organo-silicon compound dipping, Gu liquid/volume ratio is 1 ~ 2:1, preferably 1.0 ~ 1.5:1 during dipping, the baking temperature preferably 90 ~ 120 DEG C of gained solid after dipping, after drying, in 200 ~ 600 DEG C of roastings in air atmosphere, volume of air air speed preferably 95 ~ 250h that roasting passes into
-1.Preferred method is by with gained solid drying after organo-silicon compound dipping, then divides two-stage roasting, prior to 200 ~ 300 DEG C of roastings, then is warming up to 450 ~ 600 DEG C and carries out two-stage calcination.Roasting time preferably 1 ~ 6 hour, more preferably 1 ~ 3 hour.
The present invention reaches best for making adsorbent separating property, needs the para-selectivity and the adsorption capacity that consider adsorbent, to different silica modifiers, can adopt different silicon dipping modification number of times.
When carrying out modification with octamethylcy-clotetrasiloxane, dipping number of times preferably 2 ~ 3 times, after each dipping, gained solid all needs roasting in atmosphere, sintering temperature preferably 200 ~ 600 DEG C, preferably adopts above-mentioned two-stage roasting.
When carrying out modification with dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane, dipping number of times preferably 1 ~ 2 time, after each dipping, gained solid all needs roasting in atmosphere, sintering temperature preferably 200 ~ 600 DEG C, preferably adopts above-mentioned two-stage roasting.
Carry out pressure-variable adsorption separation operating method with adsorbent provided by the invention, comprise C
8aromatic hydrocarbons passes into the adsorption bed that adsorbent of the present invention is housed with gas phase state, 170 ~ 330 DEG C, adsorb paraxylene wherein and ethylbenzene or ethylbenzene under the condition of 0.4 ~ 1.3MPa, obtain the suction excess containing meta-xylene and ortho-xylene, use inert gas for sweep gas purge adsorbent bed, using the component blowout in non-selective for bed volume as intermediate species, be depressurized to 0.1 ~ 0.3MPa, obtain extract.
The adsorption temp preferably 190 ~ 300 DEG C of above-mentioned pressure-variable adsorption, more preferably 210 ~ 280 DEG C, adsorptive pressure is 0.4 ~ 1.0MPa preferably, and under adsorptive pressure, temperature will ensure that charging is gas phase state, feedstock quality air speed preferably 0.2 ~ 30h
-1, more preferably 3 ~ 6h
-1.
The inert gas preferred nitrogen of described purging bed, hydrogen, carbon dioxide, methane, ethane, propane or argon gas, more preferably nitrogen, sweep gas consumption is 1 ~ 20 times, preferably 3 ~ 10 times of non-selective volume in adsorbent bed.Desorption pressure is 0.1 ~ 0.2MPa preferably.The intermediate species purging adsorbent bed gained is feed composition substantially, the charging as pressure-variable adsorption capable of circulation.
Above-mentioned C
8aromatic hydrocarbons can for the mixed C obtained by catalytic reforming, steam cracking or the device such as disproportionation and transalkylation
8aromatic hydrocarbons also can be by above-mentioned mixed C
8remaining ingredient after aromatics seperation paraxylene, described C
8in aroamtic hydrocarbon raw material, non-aromatics content is preferably less than 20 quality %.
When with mixed C
8when aromatic hydrocarbons is as raw material, paraxylene and ethylbenzene are extracted out as extract jointly, inhale in excess and substantially do not contain paraxylene and ethylbenzene, use the advantage of adsorbent of the present invention to be to improve the content of paraxylene and ethylbenzene in extract, reduce the content of meta-xylene, ortho-xylene.Extract can be used as the raw material of moving-bed adsorption separation or Crystallization Separation p-Xylene unit, due to the raising of paraxylene content in extract, be conducive to adsorbing separation or crystallization process, and inhale in excess substantially not containing paraxylene and ethylbenzene, the severity of xylene isomerization process reaction can be reduced, reduce hydrogen/hydrocarbon ratio, and reduce the internal circulating load in Aromatic Hydrocarbon United Plant, reduce energy consumption.
When with the C after separating paraxylene
8when aromatic hydrocarbons is raw material, use adsorbent of the present invention significantly can reduce the content of meta-xylene and ortho-xylene in extract, extract can obtain high purity ethylbenzene product after being separated a small amount of non-aromatics.
Further illustrate the present invention below by example, but the present invention is not limited to this.
Example 1
Get silica/alumina molar ratio be 50 NaMCM-22 zeolite powder mix with the mass ratio of kaolin by 96:4, roller forming, get the spheric granules that particle diameter is 0.3 ~ 0.8 millimeter, 90 DEG C of dryings 4 hours, 520 DEG C of roastings 6 hours, obtain adsorbent A, wherein containing the NaMCM-22 zeolite of 96 quality %, the kaolin of 4 quality %.
Example 2
Getting adsorbent A, is modifier with octamethylcy-clotetrasiloxane, floods 12 hours in 25 DEG C.Gu the liquid/volume ratio of octamethylcy-clotetrasiloxane used and adsorbent A is 1.3:1, filter after dipping, gained solid in 95 DEG C of dryings 5 hours, then is placed in activation furnace, passes into air, is 95h in volume of air air speed
-1condition under in 250 DEG C of roastings 2 hours, then be warming up to 530 DEG C of roastings 2 hours, obtained adsorbent A-1.
Get adsorbent A-1 and repeat above-mentioned Si modification step, obtained modification number of times is the adsorbent A-2 of 2.
Repeat above-mentioned Si modification step twice, obtained modification number of times is the adsorbent A-3 of 3.
Example 3
Adsorbent B is prepared by the method for example 1, the NaMCM-22 zeolite powder being 80 unlike the use of silica/alumina molar ratio prepares adsorbent, and NaMCM-22 zeolite powder is mixed with the mass ratio of kaolin by 94:6, the adsorbent B obtained is containing the NaMCM-22 zeolite of 94 quality %, the kaolin of 6 quality %.
Example 4
Getting adsorbent B, is silica modifier with the dimethyl silicone polymer that molecular weight is 1300, floods 12 hours in 25 DEG C.Gu the liquid/volume ratio of dimethyl silicone polymer used and adsorbent B is 1.2:1, filter after dipping, gained solid in 110 DEG C of dryings 5 hours, then is placed in activation furnace, passes into air, is 150h in volume of air air speed
-1condition under in 250 DEG C of roastings 2 hours, then be warming up to 530 DEG C of roastings 2 hours, obtained adsorbent B-1.
Repeat above-mentioned Si modification step, obtained modification number of times is the adsorbent B-2 of 2 times.
Comparative example 1
By silica/alumina molar ratio be 450 NaZSM-5 zeolite powder mix with the mass ratio of kaolin by 90:10, roller forming, get the spheric granules that particle diameter is 0.3 ~ 0.8 millimeter, 90 DEG C of dryings 4 hours, 520 DEG C of roastings obtain adsorbent C in 6 hours, wherein containing the NaZSM-5 zeolite of 90 quality %, the kaolin of 10 quality %.
Example 5
By the method for example 2, modification is carried out to adsorbent C, carry out 1 Si modification with octamethylcy-clotetrasiloxane and obtain adsorbent C-1, carry out 2 Si modification and obtain adsorbent C-2.
Comparative example 2
Adsorbent is prepared by the method for comparative example 1, the Na-ZSM-5 zeolite powder being 600 unlike the use of silica/alumina molar ratio prepares adsorbent, and NaZSM-5 zeolite powder is mixed with the mass ratio of kaolin according to 85:15, obtained adsorbent D is containing the NaZSM-5 zeolite of 85 quality %, the kaolin of 15 quality %.
Example 6
Getting adsorbent D, is silica modifier with the poly-hydrosiloxane that molecular weight is 2500, floods 8 hours in 25 DEG C.Gu the liquid/volume ratio of poly-hydrosiloxane used and adsorbent D is 1.3:1, filter after dipping, gained solid in 115 DEG C of dryings 6 hours, then is placed in activation furnace, passes into air, is 200h in volume of air air speed
-1condition under in 300 DEG C of roastings 3 hours, then be warming up to 530 DEG C of roastings 2 hours, obtained adsorbent D-1.
Comparative example 3
Silicalite-1 zeolite powder is mixed with the mass ratio of kaolin by 95:5, roller forming, gets the spheric granules that particle diameter is 0.3 ~ 0.8 millimeter, 90 DEG C of dryings 4 hours, 520 DEG C of roastings, 6 hours obtained adsorbent E, wherein containing the Silicalite-1 zeolite of 95 quality %, the kaolin of 5 quality %.
Example 7 ~ 15
Following instance evaluates adsorbent of the present invention and the absorption property contrasting adsorbent.
It is in the adsorption column of 15 that 69 grams of adsorbents are filled in ratio of height to diameter, temperature 250 DEG C, pressure be 0.70MPa, mass space velocity is 4.5h
-1condition under, pass into adsorption column by after material gasification, collect not by the component of adsorbing for inhaling excess.Purge bed with the nitrogen that pressure is 0.70MPa, purge 6 times that nitrogen used is non-selective volume in adsorption bed, be depressurized to 0.1MPa, and purge adsorption bed with nitrogen, make by absorbed component desorption, the desorption component of collection is extract.Absorption raw material used consist of ethylbenzene 12.24 quality %, paraxylene 18.65 quality %, meta-xylene 45.73 quality %, ortho-xylene 21.58 quality %, non-aromatics be 1.8 quality %.Selective and the adsorption capacity of the sorbent used numbering of each example, adsorbent is in table 1.
In table 1, adsorbent is selective to be calculated by following formula.
Example 16 ~ 19
By the method for example 7, performance of the adsorbent is evaluated, unlike be 0.85MPa at temperature 265 DEG C, pressure, mass space velocity is 5.0h
-1condition under, adsorption column is passed into by after absorption material gasification, collect not by the component of adsorbing for inhaling excess, bed is purged with the nitrogen that pressure is 0.85MPa, purge 4 times that nitrogen used is non-selective volume in adsorption bed, be depressurized to 0.1MPa, and purge adsorption bed with nitrogen, make by absorbed component desorption, the desorption component of collection is extract.Selective and the adsorption capacity of the sorbent used numbering of each example, adsorbent is in table 2.
Example 20 ~ 26
Substantially not contain the C of paraxylene
8aromatic hydrocarbons is absorption raw material, raw materials usedly consists of ethylbenzene 18.58 quality %, paraxylene 0.082 quality %, meta-xylene 53.74 quality %, ortho-xylene 24.47 quality %, non-aromatics 3.128 quality %.
It is in the adsorption column of 15 that 69 grams of adsorbents are filled in ratio of height to diameter, temperature 233 DEG C, pressure be 0.55MPa, mass space velocity is 4.0h
-1condition under, adsorption column is passed into by after above-mentioned absorption material gasification, collect not by the component of adsorbing for inhaling excess, purge bed with the nitrogen that pressure is 0.55MPa, purge 5 times that nitrogen used is non-selective volume in adsorption bed, then 0.1MPa is depressurized to, and purge adsorption bed with nitrogen, make by absorbed component desorption, the desorption component of collection is extract, non-aromatics in distillation removing extract, obtains ethylbenzene.The sorbent used numbering of each example, adsorbent are selective, adsorption capacity, extract ethylbenzene purity is in table 3.
In table 3, ethylbenzene selectivity is calculated by following formula.
Table 1
Table 2
Table 3
Claims (18)
1. a Gas Phase Adsorption separation of C
8the adsorbent of arene isomer, comprise the absorbed component of 80 ~ 99.5 quality % and the binding agent of 0.5 ~ 20 quality %, described absorbed component is sodium form MWW zeolite, through the NaZSM-5 of Si modification or sodium form MWW zeolite, the silica of described NaZSM-5 and alumina molar ratio are 350 ~ 800, the described silica of sodium form MWW zeolite and the mol ratio of aluminium oxide are at least 40, and Si modification organo-silicon compound used are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly-methylhydroxy siloxanes, poly-hydrosiloxane.
2., according to adsorbent according to claim 1, it is characterized in that described sodium form MWW zeolite is NaMCM-22 zeolite.
3., according to adsorbent according to claim 2, it is characterized in that the silica of described NaMCM-22 zeolite and alumina molar ratio are 40 ~ 200.
4., according to adsorbent according to claim 1, it is characterized in that described binding agent is at least one in kaolin, bentonite, attapulgite, aluminium oxide, magnesia, zirconia, titanium dioxide, boron oxide and silica.
5., according to adsorbent according to claim 1, it is characterized in that described adsorbent comprises the absorbed component of 85 ~ 99.5 quality % and the binding agent of 0.5 ~ 15 quality %.
6., according to adsorbent according to claim 1, it is characterized in that the molecular weight of described dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane is 800 ~ 4000.
7., according to adsorbent according to claim 4, it is characterized in that the molecular weight of described dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane is 1000 ~ 3000.
8. a preparation method for adsorbent according to claim 1, comprises after sodium form MWW zeolite and binding agent mixed-forming, and dry, roasting, silica and the alumina molar ratio of described sodium form MWW zeolite are at least 40.
9. the preparation method of adsorbent described in a claim 1, comprise sodium form MWW zeolite or NaZSM-5 and binding agent mixed-forming, flood with organo-silicon compound after drying, roasting, gained solid drying after flooding, in 200 ~ 600 DEG C of roastings in air atmosphere, the volume of air air speed that roasting passes into is 90 ~ 300h
-1described organo-silicon compound are selected from octamethylcy-clotetrasiloxane, dimethyl silicone polymer, poly-methylhydroxy siloxanes, poly-hydrosiloxane, the silica of described NaZSM-5 and alumina molar ratio are 350 ~ 800, and the described silica of sodium form MWW zeolite and the mol ratio of aluminium oxide are at least 40.
10. according to the method described in claim 8 or 9, it is characterized in that shaping after sintering temperature be 500 ~ 650 DEG C.
11. in accordance with the method for claim 9, it is characterized in that the molecular weight of described dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane is 800 ~ 4000.
12. in accordance with the method for claim 9, it is characterized in that the molecular weight of described dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane is 1000 ~ 3000.
13. in accordance with the method for claim 9, it is characterized in that, by with gained solid drying after organo-silicon compound dipping, in 200 ~ 300 DEG C of roastings, then being warming up to 450 ~ 600 DEG C of roastings.
14. in accordance with the method for claim 9, it is characterized in that when carrying out modification with octamethylcy-clotetrasiloxane, and dipping number of times is 2 ~ 3 times, and after each dipping, gained solid all needs roasting in atmosphere.
15. in accordance with the method for claim 9, and it is characterized in that, when carrying out modification with dimethyl silicone polymer, poly-methylhydroxy siloxanes or poly-hydrosiloxane, dipping number of times is 1 ~ 2 time, after each dipping, gained solid all needs roasting in atmosphere.
16. 1 kinds of Gas Phase Adsorption separation of C
8the method of arene isomer, comprises C
8aromatic hydrocarbons passes into the adsorption bed that adsorbent described in claim 1 is housed with gas phase state, 170 ~ 330 DEG C, adsorb paraxylene wherein and ethylbenzene under the condition of 0.4 ~ 1.3MPa, or ethylbenzene, obtain the suction excess containing meta-xylene and ortho-xylene, use inert gas for sweep gas purge adsorbent bed, using the component blowout in non-selective for bed volume as intermediate species, be depressurized to 0.1 ~ 0.3MPa, obtain extract.
17. in accordance with the method for claim 16, it is characterized in that described inert gas is nitrogen, hydrogen, carbon dioxide, methane, ethane, propane or argon gas.
18. in accordance with the method for claim 16, it is characterized in that sweep gas used is 1 ~ 20 times of non-selective volume in adsorbent bed.
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| CN107922291A (en) * | 2015-06-17 | 2018-04-17 | 巴斯夫公司 | For recycling the adsorbent of hydrocarbon |
| CN107922291B (en) * | 2015-06-17 | 2021-07-20 | 巴斯夫公司 | Adsorbent for recovery of hydrocarbons |
| CN110267739A (en) * | 2017-02-13 | 2019-09-20 | 普莱克斯技术有限公司 | Adjustable adsorbent |
| CN112334225A (en) * | 2018-07-02 | 2021-02-05 | 普莱克斯技术有限公司 | Large crystal adjustable adsorbent |
| CN112334225B (en) * | 2018-07-02 | 2023-09-29 | 普莱克斯技术有限公司 | Large crystal adjustable adsorbent |
| CN114160096A (en) * | 2022-02-08 | 2022-03-11 | 中海油天津化工研究设计院有限公司 | Adsorbent for separating ethylbenzene in carbon octaaromatic hydrocarbon and preparation method thereof |
| 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 |
| WO2023151561A1 (en) * | 2022-02-08 | 2023-08-17 | 中海油天津化工研究设计院有限公司 | Adsorbent for separating ethylbenzene from c8 aromatic hydrocarbons and preparation method therefor |
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