CN1339334A - Preparing method for adsorbeng for selectively adsorbing and separating aromatic isomer - Google Patents
Preparing method for adsorbeng for selectively adsorbing and separating aromatic isomer Download PDFInfo
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- CN1339334A CN1339334A CN 00123514 CN00123514A CN1339334A CN 1339334 A CN1339334 A CN 1339334A CN 00123514 CN00123514 CN 00123514 CN 00123514 A CN00123514 A CN 00123514A CN 1339334 A CN1339334 A CN 1339334A
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Abstract
The present invention process of adsorbent for selectively adsorbing and sepearating aromatic isomer includes mixing X or Y type molecular sieve, IA or IIA metal salt and small amount of adhesive, grinding, into smaller than 300 micron particles, rolling to form, roasting at 500-580 deg.c, and final washing with deionzied water to a sodium iron mass fraction less than 0.5 %. The adsorbent thus prepared is suitable for adsorption and separation of paraxylene from C8 arene.
Description
The present invention is the preparation of adsorbent method of selective absorption separating aromatic isomer, specifically, be a kind of be the preparation of adsorbent method of active component with the crystal aluminosilicate.
As everyone knows, in isolation technics, the alumino-silicate of some crystallization changes the electrochemical properties of its crystal through cation exchange, or the acid-base value of having said modulation, thereby is used to separate the isomers of some hydro carbons.Wherein typical example is that X or Y zeolite are through Ba
2+, K
+Cation exchange is from C
8Separating paraxylene in the aromatic hydrocarbons.The for example USP3626020 of Neuzil, USP3686342, USP3734974 and USP3997620, the USP3665046 of De Rosset, the USP3668266 of Chen, the USP3700744 of Berger and the USP3894109 of Rosback all discuss to some extent.Prior art is generally acknowledged, C
8The difference of the electrochemistry absorption affinity of each isomers and adsorbent is depended in the separation of arene isomer significantly, rather than the difference of each isomer molecule overall dimensions.
USP3,969,276, USP3,878,127 and USP3,878,129 all disclose a kind of preparation method who is used for the zeolite adsorbents that aromatic hydrocarbons separates.This method is handled X or Y zeolite earlier with fluorine-containing sodium hydroxide solution, its objective is molecular screen primary powder is carried out sufficient sodium exchange, so that more effective the carrying out of follow-up barium exchange.After carrying out sodium exchange, adopt two step exchange processes to carry out barium again and potassium ion exchange system gets adsorbent.
In above-mentioned prior art, Ba
2+, K
+Exchange use the aqueous solution and the sodium type molecular screen primary powder of solubility Ba salt or K salt to carry out ion-exchange, wherein the X type molecular sieve with the barium exchange is the most commonly used, if use Ba
2+, K
+Two kinds of ions exchange, and need solubility barium, sylvite are mixed and made into solution, and one step of cycling finishes, and also can prepare two kinds of ion solution, exchanges several times in succession and finishes.The exchange ratio of two kinds of ions should make in the molecular sieve oxide expression formula, BaO/K
2The mol ratio of O reaches 0.6～1.2: 1, be preferably 0.9～1.1: 1.Solion give-and-take conditions such as USP3,878,127, USP3,878,129 provide: 60～160 ℃ of temperature of exchange, pressure 0.1～3.4MPa.
Owing to adopt solwution method to carry out ion-exchange, for guaranteeing that solution fully is penetrated into molecular sieve inside, the exchange liquid concentration of preparation can not be too high, and the concentration that generally exchanges liquid is controlled at 0.1～0.3 mol.Under the certain condition of exchange liquid concentration, solution usage should make wherein cations be slightly more than sodium content in the molecular sieve, usually the exchange ratio of control exchange liquid is just can make molecular sieve residual sodium ion mass fraction exchange after less than 0.5% at 1.5～2.0: 1, that is to say, adopt salting liquid to carry out ion-exchange and will use excessive exchange liquid inevitably, the sodium ion in the molecular sieve is exchanged substantially fully.Often containing excessive barium or potassium, particularly barium salt in the exchange raffinate is the restriction that its discharge capacity of poisonous substance is subjected to environmental protection, must reclaim and could discharge, and this has increased post-processing step undoubtedly.In addition, for improving the utilization rate of exchange ion, mother liquor need recycle, and makes ion-exchange step become comparatively complicated.
The purpose of this invention is to provide and a kind of directly molecular sieve the mixing with slaine carry out the method that ion-exchange prepares adsorbent.
The basic principle of solid ionic exchange is that many salts or metal oxide can be in the molecular sieve spontaneous dispersions in surface, form a kind of monolayer dispersed, this dispersion can make the negative ions of salt or metal oxide attract mutually with the different in nature ion of molecular sieve surfaces externally and internally, form stronger surface ion key, the result descends the free energy of system.The individual layer dispersion process also makes molecular sieve become comparatively unordered surperficial decentralized photo by orderly crystalline phase, the entropy of system is increased greatly promptly follow the gibbs law: Δ G=Δ H-T Δ S＜0 is the thermodynamics spontaneous process so salt or metal oxide form the monolayer dispersed on the molecular sieve surface.Test finds that slaine can also carry out ion-exchange reactions when the molecular sieve surface disperses.The order of ion-exchange be multivalent ion than the preferential exchange of monovalention, for alkali metal and alkaline-earth metal ions, its affinity increases with the increase of atomic number, that is:
Na
+＜Ca
2+＜La
2+＜Th
4+；Li
+＜Na
+＜K
+＜Rb
+＜Cs
+；Mg
2+＜Ca
2+＜Sr
2+＜Ba
2+
For NaX or NaY type molecular screen primary powder, Ba
2+Ion and Na
+Exchange than K
+Ion and Na
+Exchange be easy to many.Finished the present invention based on above-mentioned principle and result of the test.
Method employing solid ionic exchange process provided by the invention is carried out ion-exchange and is prepared adsorbent, specifically, comprises the steps:
(1) will wear into after X or Y zeolite, IA and/or IIA slaine and the small amount of binder mixing
Particle diameter is less than 300 microns particulate, again through rolling moulding, 500～580 ℃ of roastings, wherein IA
And/or the mixing quality ratio of IIA slaine and molecular sieve is 0.6～0.8: 1, binding agent and molecule
The mixing quality ratio of sieve is 0.08～0.20: 1,
(2) material that obtains after the roasting is spent deionised water to the mass fraction of sodium ion less than
0.5％。
Used molecular sieve, IA or IIA slaine and binding agent all should be worn into the particulate less than 300 microns in the above-mentioned preparation process, so that slaine forms monolayer on molecular sieve.This levigate can be after earlier raw material being mixed, to wear into particulate again less than 300 microns, also can be that each component is worn into particulate less than 300 microns respectively, mix again.After comparatively preferably earlier each component being mixed, regrind into fine powder.
The general expression that X type molecular sieve has in the described preparation raw material is:
(0.9±0.2)M
2/nO·Al
2O
3·(2.5±0.5)SiO
2·yH
2O (1)
On behalf of at least a chemical valence, M be not more than 3 cation in the formula (1), can be hydrogen, sodium or calcium, and n is the chemical valence of M, and the value of y is about below 8, and the value of determining depends on the concrete cation of M representative and the degree of hydrogenation of molecular sieve.The preferred molecular sieve raw material of the present invention is a NaX type molecular sieve.
Except using X type molecular sieve, also can select for use the NaY molecular sieve to prepare adsorbent, its general expression that has as the formula (2), wherein the value of y is not more than 9.
(0.9±0.2)Na
2O·Al
2O
3·(3.0～8.0)SiO
2·yH
2O (2)
The preferred IA of slaine that the inventive method is selected and/or the hydrochloride or the nitrate of IIA metal, preferred IIA slaine is barium nitrate or barium chloride, preferred IA slaine is potassium nitrate or potassium chloride.If when using IA and IIA slaine simultaneously, the mol ratio of IIA and IA slaine is 0.9～1.1: 1.
Also should add an amount of binding agent when preparing adsorbent of the present invention to improve adsorbent intensity, preferred binding agent is kaolin, Ludox, aluminium oxide or they mixture of the two arbitrarily, as to adopt two kinds of materials be binding agent, and then the mixed proportion of the two can be arbitrarily.
Prepare adsorbent of the present invention and at first raw material will be worn into particulate less than 300 microns, so just more help slaine and form monolayer on the molecular sieve surface, in addition, the mixed material granularity is more little, its mixture homogeneity is just high more, should be 280～350 microns so prepare the raw materials used suitable particle diameter of adsorbent in the present invention, excessive raw material particle size obviously is unfavorable for the ion-exchange on molecular sieve surface.
After raw material being milled to less than 300 microns particulate, it is 0.3～0.8 millimeter bead that the promptly available rolling method of forming is made particle diameter with described raw material.Will add an amount of water during the rolling moulding, so that mixed material forms the bead of certain particle diameter in the rotation of bowling machine rotating disk, the addition of water should be 0.05～0.3 times of raw material gross mass.
Above-mentioned article shaped needs just can finish ion-exchange at given roasting temperature, and the temperature of roasting is preferably 540～580 ℃, and the time is 1～10 hour, preferred 2～6 hours.Article shaped will be 110～240 ℃ of dryings before the roasting, and be 2～10 hours drying time, is preferably 4～8 hours.
Through the roasting of certain hour, the sodium ion of molecular sieve is broken away from framework of molecular sieve by the cation replacement in the slaine, need this moment with the sodium ion in the deionized water flush away molecular sieve, up to the mass fraction of sodium ion less than 0.5%.The temperature of water preferably is controlled to be 80～90 ℃ during washing.
Above-mentioned article shaped promptly gets adsorbent after roasting, washing, this agent can be used for the separation of arene isomer after 110～240 ℃ of dryings, and be 2～10 hours drying time, is preferably 4～8 hours.
The adsorbent of the inventive method preparation is applicable to the adsorption separation process of arene isomer, the arene isomer that particularly separates contraposition from described isomers is as adsorbing separation paraxylene from the mixture of ortho-xylene, meta-xylene, paraxylene and ethylbenzene.
When described adsorbent is used for adsorbing separation, can adopt the multicolumn serial arrangement to operate, also can adopt simulation moving-bed mode to operate.Answering controlled pressure during operation is 0.5～1.0MPa, and temperature is 170～200 ℃.
The adsorption capacity of adsorbent depends primarily on amorphous component such as the relative crystallinity of contained molecular sieve and binding agent shared ratio in adsorbent.The relative crystallinity of molecular sieve is high more, and amorphous component amounts such as binding agent are few more, and the adsorption capacity of adsorbent is just big more.
The selectivity of adsorbent is the ability of each isomers component in the separating mixed dimethyl.Selectivity promptly is when reaching adsorption equilibrium, the ratio of the ratio of the quality of these two kinds of components or volume in the ratio of the quality of two kinds of components or volume and the non-absorption mutually in the absorption mutually.When the contact of the adsorbent in dimethylbenzene charging and adsorbent bed back component no longer changes i.e. absorption mutually and the net transfer of component does not take place between the non-absorption phase, equilibrium condition is determined at this moment.Selectivity β is calculated by following formula:
A in the formula
CAnd A
DThe quality or the volume fraction of C, D two components during expression is adsorbed mutually respectively, U
C, U
DQuality or the volume fraction of representing C during non-absorption mutually, D two components respectively.When two kinds of components selection β ≈ 1, there is not wherein a kind of preferential adsorption of component in the degree that they are adsorbed each other or are not adsorbed much at one.When β＞1 or＜wherein a kind of component appears by the separable process of preferential adsorption 1 the time.Specifically, when β＞1, show that adsorbent is to the preferential adsorption of C component; When β＜1, show that adsorbent is to the preferential adsorption of D component.Consider from the complexity of separating, preferably make selectivity β＞2, the β value more high score from carrying out with regard to easy more.Obviously selectivity is good more, and the amount of the adsorbent that production equivalent purpose product is used is few more.In addition, theoretically, extract component relatively, must be equal to or less than 1 the selectivity of strippant.
Adsorbent also is to investigate an important indicator of performance of the adsorbent to extracting component desorption rate value under the effect of certain strippant.Desorption rate can reduce the desorb dosage of use faster, improves the production capacity of purpose product, reduces the operating cost of separator.Under the condition that strippant is determined, desorption rate depends on the cation type of adsorbent and the exchange degree in framework of molecular sieve, and is also relevant with the silica alumina ratio of the water content of adsorbent, molecular sieve simultaneously.
Be the absorption of test adsorbent and the characteristic of desorb, use a kind of dynamic testing arrangement to measure adsorption capacity, selectivity and desorption rate.This device is that 45 milliliters helical disk tubular type adsorption column is formed by volume, and spiral coil is made by the stainless steel tube of 8 * 1 * 1200 millimeters of φ, manages high 18 centimetres.Adsorption column is placed in to have in the temperature controlled vertical electric furnace and heats.End entrance links to each other with nitrogen system with feed pump on the adsorption column, and the lower end outlet connects pressure-control valve and is connected with the effluent gatherer.The liquid efflunent gas chromatographic analysis.
Use said apparatus to carry out selectivity and other data that conventional pulse testing is measured absorption system.Pack into the adsorption column concussion of load weighted adsorbent is tamped, and in 180～200 ℃ of activation dehydrations down, the control water content is not more than 5 and weighs % in the presence of nitrogen.Earlier drain nitrogen, be warming up to 180 ℃, boost to 0.8MPa with strippant toluene or p-Diethylbenzene.Pump into raw material after 10 minutes by liquid hour air speed 1.0, feed strippant with same air speed again, form with the gas chromatographic analysis effluent simultaneously.Strippant contains 70% the tracer that is not adsorbed, and at first goes out the peak, and it can provide the dead volume of adsorption column.The mid point of tracer half-peak breadth as zero point, is measured each component half-peak breadth mid point to the net retention volume R at zero point, and the distribution coefficient of net retention volume when balance of component is directly proportional arbitrarily, and it has reflected the character of adsorption equilibrium.Net retention volume be selectivity β value than promptly.Chromatogram draws the envelope of each component respective peaks, and its half-peak breadth W provides the information of each constituent mass transfer rate, and the half-peak breadth W of certain component can show with the milliliter numerical table of the strippant that is pumped at interval during this period of time.The half-peak breadth of certain component is narrow more, shows that adsorbent is fast more to the speed of the absorption of this component and desorb.
The present invention adopts a kind of solid metallic ion exchange technique to prepare adsorbent, promptly directly slaine is become the fine grained of certain particle diameter with the molecular sieve mixed grinding, obtains having the adsorbent of molecular sieve of setting metal cation content after roasting, washing.Compare with liquid ion-exchange process, have simple to operate, the advantage that amount of metal salts is few also can avoid containing the discharging of the exchange mother liquor of barium ions simultaneously, and a spot of barium ions is easy to form barium sulfate or barium carbonate sediment and reclaim through acid treatment in the cleaning solution.
Below by example in detail the present invention, but the present invention is not limited to this.
The adsorption capacity of adsorbent is represented with C in the example, and selectivity represents that with β desorption rate is with reaching interior strippant suction body product representation of paraxylene half-peak breadth time.
In the adsorbent preparation process, than expression, it is defined as the consumption of slaine with exchange:
Mn in the following formula
+Be the molal quantity of certain component in the exchange media, n is a cationic chemical valence in this component, and exchange media refers to be used for the metal salt solution or the slaine of ion-exchange.
Example 1
This example prepares adsorbent with the solid ionic exchange process.
With 90 kilograms of 13X molecular screen primary powders (Wenzhou catalyst head factory), 10 kilograms of kaolin and 81.70 kilograms of Ba (NO
3)
2Mix; exchange is than being 1.0; mixed material is worn into particle less than 300 microns on centrifugal mill, spray 18 kilograms deionized water on rolling limit, rolling granulator top, prepare 0.3～0.8 millimeter bead; 4 hours, 540 ℃ roastings of 120 ℃ of dryings 4 hours; naturally be cooled to 85 ℃, do not have sodium ion to flowing out liquid, 120 ℃ of dryings 8 hours with the washing of synthermal deionized water; make adsorbent A, its water content is 5 heavy %.The sodium ion Corning035 flame spectrophotometer measuring of washing effluent.Molecular screen primary powder and adsorbent are formed with x-ray fluorescence analysis, down together.
Used 13X molecular screen primary powder relative crystallinity 105%, framework si-al ratio in the above-mentioned preparation: 2.24, crystallite dimension is about 1 micron, and the mass fraction of its chemical element composition analysis is: Na
2O 16.0%, SiO
251.0%, Al
2O
332.0%, K
2O 0.54%.
The bright basic bulk density of adsorbent A is 0.82 grams per milliliter, and chemical element composition analysis mass fraction is: Na
2O 0.32%, BaO 34.0%, SiO
239.0%, Al
2O
323.0%, K
2O 0.35%.
Get 45 gram adsorbent A, place the helical disk tubular type adsorption column of the described dynamic checkout unit of specification, concussion is tamped.With toluene is that strippant, nonane are that tracer is tested, and the absorption raw material consists of: ethylbenzene 16.36%, paraxylene 17.61%, meta-xylene 44.74%, ortho-xylene 21.17%.The performance measurement of adsorbent A the results are shown in Table 1.
Example 2
Method by example 1 prepares adsorbent B and carries out the absorption property evaluation, and different is with 64.8 kilograms of BaCl when preparing adsorbent
2Replace Ba (NO
3)
2
The bright basic bulk density of adsorbent B is 0.82 grams per milliliter, water content 5%, and chemical element composition analysis mass fraction is: Na
2O 0.32%, BaO 35.0%, SiO
240.0%, Al
2O
321.0%, K
2O0.32%.The absorption property evaluation result of adsorbent B sees Table 1.
Example 3
Get 90 kilograms of 13X molecular screen primary powders, 61.27 kilograms of Ba (NO
3)
2, 15.0 kilograms of KNO
3, as binding agent, fully mix Ba (NO with 8 kilograms kaolin and 9 kilograms of silica gel
3)
2With KNO
3Mol ratio be 1.5: 1.0, exchange is than being 1.0.Mixed material is worn into particle less than 300 microns on centrifugal mill, spray 20 kilograms deionized water on rolling limit, rolling granulator top, prepare particle diameter and be 0.3～0.8 millimeter bead.4 hours, 520 ℃ roastings of 180 ℃ of dryings 4 hours are cooled to 90 ℃ naturally, do not have sodium ion with the washing of synthermal deionized water to flowing out liquid, and 120 ℃ of dryings 8 hours make adsorbent C, and its water content is 5%.
Used 13X molecular screen primary powder relative crystallinity 101%, framework si-al ratio in the above-mentioned preparation: 2.36, crystallite dimension is about 1 micron, and the mass fraction of its chemical element composition analysis is:
Na
2O?15.0％，SiO
2?52.0％，Al
2O
3?30.0％，K
2O?0.59％
The bright basic bulk density of adsorbent C is 0.80 grams per milliliter, and chemical element composition analysis mass fraction is: Na
2O 0.46%, BaO 34.0%, SiO
239.0%, Al
2O
323.0%, K
2O 0.5%.Method by example 1 is carried out the absorption property evaluation to adsorbent C, the results are shown in Table 1.
Comparative Examples 1
Adopt the solion exchange process to prepare adsorbent.
90 kilograms of former powder of 13X and 9.8 kilograms of kaolin and 6.9 kilograms of Ludox are mixed, press the method rolling moulding of example 1, make particle diameter and be 0.3～0.8 millimeter bead, 120 ℃ of dryings 4 hours, 540 ℃ of roastings 4 hours.The former powder relative crystallinity 101% of 13X, framework si-al ratio: 2.36, about 1 micron of crystallite dimension, the mass fraction of chemical element composition analysis is:
Na
2O?15％，SiO
2?52％，Al
2O
3?30％，K
2O?0.59％
Solids after the roasting is carried out ion-exchange with conventional ionic liquid phase post.Exchange column is to be made by the stainless steel tube of φ 39 * 7 * 600mm, and exchange column is placed in to have in the temperature controlled vertical electric furnace and heats.End entrance links to each other with nitrogen system with the feed pump of exchange liquid on the exchange column, and the lower end outlet connects pressure-control valve and is connected with the effluent gatherer.When carrying out ion-exchange, exchange liquid enters from the last end entrance of exchange column, and exchange is carried out under 0.2～0.3MPa condition at 120～130 ℃, and exchange liquid is that concentration is the Ba (NO of 0.18 mol
3)
2The aqueous solution, the little hourly space velocity of liquid that exchange liquid flows into exchange column is 12 hours
-1, exchange is than being 2.0.After the barium exchange, feeding deionization from the exchange column upper end does not have sodium ion towards Xian to flowing out the liquid, and the 120 ℃ of dryings of molecular sieve after the exchange were got adsorbent Z in 8 hours.
The bright basic bulk density of adsorbent Z is 0.81 grams per milliliter, water content 5%, and the mass fraction of chemical element composition analysis is:
Na
2O?0.33％，BaO?34％，SiO
2?39％，Al
2O
3?21％，K
2O?0.04％
Method by example 1 is carried out performance evaluation to adsorbent Z, the results are shown in Table 1.
Comparative Examples 2
90 kilograms of former powder of 13X and 16.7 kilograms of kaolin are mixed, press the method rolling moulding of example 1, make particle diameter and be 0.3～0.8 millimeter bead, 120 ℃ of dryings 4 hours, 540 ℃ of roastings 4 hours.The former powder relative crystallinity 105% of 13X, framework si-al ratio: 2.24, about 1 micron of crystallite dimension.The mass fraction of its chemical element composition analysis is:
Na
2O?16％、SiO
2?51％、Al
2O
3?32％、K
2O?0.54％
The solid of gained after the roasting is carried out the ionic liquid phase exchange by the method for Comparative Examples 1, and exchange liquid is Ba (NO
3)
2And KNO
3Mixed liquor, Ba (NO
3)
2Concentration is 0.18 mol, KNO
3Concentration is 0.32 mol, and the little hourly space velocity of quality of exchange liquid is 12 hours
-1, exchange is than being 2.0.After the exchange, feeding deionization from the exchange column upper end does not have sodium ion towards Xian to flowing out the liquid, and the 120 ℃ of dryings of molecular sieve after the exchange were got adsorbent S in 8 hours.
The bright basic bulk density of adsorbent S is 0.80 grams per milliliter, water content 5%, and the mass fraction of chemical element composition analysis is:
Na
2O?0.35％，BaO?32.0％，SiO
2?52.0％，Al
2O
3?33.0％，K
2O?0.52％
Method by example 1 is carried out performance evaluation to adsorbent S, the results are shown in Table 1.
Table 1 data show that the performance of the absorbent that makes with the ionic liquid phase exchange process in the adsorbent of the inventive method preparation and the Comparative Examples is suitable.But the exchange of the inventive method ratio is 1.0, and it is few to illustrate that this method is used for the amount of metal salts of ion-exchange, and does not have the exchange mother liquor; And the ionic liquid phase exchange process need with the exchange ratio be 2.0, it is more obviously to be used to the amount of metal salts that exchanges, and remaining barium, potassium ion are arranged in the mother liquor, needs cycling and reutilization, and carries out post processing and could discharge.
Table 1
The following component of subscript letter representative in the table 1: XY-dimethylbenzene, P-paraxylene, M-meta-xylene, O-ortho-xylene, E-ethylbenzene
Claims (10)
1, a kind of preparation of adsorbent method of selecting the adsorbing separation arene isomer comprises the steps:
(1) with X or Y zeolite, IA and/or IIA slaine and small amount of binder mixing back mill
Become particle diameter less than 300 microns particulate, again through rolling moulding, 500～580 ℃ of roastings, its
Middle IA and/or IIA slaine are 0.6～0.8: 1 with the mixing quality ratio of molecular sieve, binding agent
With the mixing quality ratio of molecular sieve be 0.08～0.20: 1,
(2) material that obtains after the roasting is spent deionised water to the mass fraction of sodium ion less than
0.5％。
2, in accordance with the method for claim 1, it is characterized in that described IA slaine is potassium nitrate or potassium chloride.
3, in accordance with the method for claim 1, it is characterized in that described IIA slaine is barium nitrate or barium chloride.
4, in accordance with the method for claim 1, it is characterized in that described binding agent is kaolin, Ludox, aluminium oxide or they mixture of the two arbitrarily.
5, in accordance with the method for claim 1, it is characterized in that described X type or Y zeolite are NaX or NaY type molecular sieve.
6, in accordance with the method for claim 1, it is characterized in that (1) described rolling moulding of step is that described raw material is made particle diameter is 0.3～0.8 millimeter bead.
7, in accordance with the method for claim 1, it is characterized in that described sintering temperature of (1) step is 540～580 ℃, the time is 2～6 hours.
8, in accordance with the method for claim 1, it is characterized in that described deionized water temperature of (2) step is 80～90 ℃.
9, in accordance with the method for claim 1, when it is characterized in that using simultaneously IA and IIA slaine, the mol ratio of IIA and IA slaine is 0.9～1.1: 1.
10, in accordance with the method for claim 1, it is characterized in that described arene isomer is ortho-xylene, meta-xylene, paraxylene and ethylbenzene.
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| CN106552583B (en) * | 2015-09-29 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of ethylbenzene adsorbent and preparation method thereof |
| CN105124806A (en) * | 2015-10-22 | 2015-12-09 | 浙江海洋学院 | P-xylene protective facial mask and preparation method thereof |
| CN105258998A (en) * | 2015-11-03 | 2016-01-20 | 浙江海洋学院 | Preparation detection method of adsorbent based on leaked PX in soil |
| CN110511118A (en) * | 2018-05-22 | 2019-11-29 | 中国石油化工股份有限公司 | A kind of method of liquid phase adsorption separation paracresol |
| CN110511118B (en) * | 2018-05-22 | 2022-02-08 | 中国石油化工股份有限公司 | Method for separating paracresol by liquid phase adsorption |
| CN109589912A (en) * | 2019-01-29 | 2019-04-09 | 山东奥福环保科技股份有限公司 | A kind of concentration runner adsorbent material and preparation method thereof |
| CN109589912B (en) * | 2019-01-29 | 2021-09-17 | 山东奥福环保科技股份有限公司 | Concentrated rotating wheel adsorption material and preparation method thereof |
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