• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    An absorptive separation process is disclosed for separating para-aromatic isomers from a hydrocarbon feed containing a mixture of aromatic isomers, using a crystalline aluminosilicate adsorbent which has been treated with an alkyl amine preferably an alkyl amine hydrochloride. The alkyl amine treatement substantially increases the selectivity of the adsorbent for the paraxylene isomer, relative to the heavy desorbent p-DEB thereby improved the efficiency of the separation process.
    公开号:SU1097191A3
    申请号:SU813308437
    申请日:1981-06-15
    公开日:1984-06-07
    发明作者:Герберт Росбэк Дональд
    申请人:Юоп,Инк. (Фирма)；
    IPC主号:
    专利说明:

    I1097 The invention relates to methods for isolating p-xylene from a cf containing a mixture of Cg aromatic isomers, including the acylpars-isomer, by selective adsorption. There are known methods for the isolation of fi-xylene from mixtures of C-aromatic hydrocarbons, according to which crystalline aluminosilicate containing cations of metals of groups I and II is used as an adsorbent, which increase its selectivity 1 and .2, the adsorbed Lav-isomer is removed from the adsorbent with a desorbent. The desorbent should have the ability to desorb the adsorbed isomer without creating large volumes of material flow, and should also be easily displaced from the adsorbent during the subsequent adsorption cycle. In addition, such a desorbent must be able to easily separate from the adsorbed starting components, which allows for high purity separation of the depleted products and reuse of the desorbent. Since this separation is usually carried out by distillation distillation, a large difference in the boiling points of the starting material and desorbent is necessary in order to make it possible to economically separate the starting components from the desorbent by simple rectification. During the separation of aromatic isomers with 8 carbon atoms, both tolu ol 1 3 and diethylbenzene 2 can be used as desorbents. Toluene plants are designed for raw materials practically free of naphthenes with 8 carbon atoms. Such raw materials are obtained as a fraction of reformed products after solvent extraction and extraction distillation. These plants work well, but with the rapid increase in the cost of energy in recent years, their practical application is becoming less and less economical due to the fact that large quantities of desorbent are subjected to evaporation and condensation during distillation distillation. Currently, installations for the separation of aromatic compounds provide for the use of heavy desorbents. However, when replacing light desorbent in heavy lime plants, adsorbents that allow to achieve good results using light desorbent do not always work well in combination with heavy desorbent. For example, the extraction of fi-xylene according to the method proceeds insufficiently selectively. In the case of using toluene as a desorbent, it is also impossible to increase the production of h-xylene Yu by adding the Cd fraction of aromatic hydrocarbons to an isomerization unit of undesirable Cg aromatic isomers. Usually, under isomerization conditions, small amounts of 5 naphthenes with 8 carbon atoms are obtained, which accumulate in the toluene desorbent and contaminate it. Thus, for a number of reasons, it is desirable to change the operation of the existing 20 units for the separation of aromatic compounds with 8 carbon atones by replacing the light desorbent with a ton of carbon. However, this usually requires replacing the known adsorbents 25 with others, which is a costly undertaking. Therefore, it is necessary to modify the known adsorbents used, which are characterized by a low content of barium and high content of potassium components. A known method for isolating p-xylene from mixtures of Cg-aromatic hydrocarbons by adsorption, according to which, as an adsorbent, a zeolite of the type NaX or NaY is used, containing barium and potassium cations, modified by treating with valuable aliphatic alcohol to a content of the last 40 zeolite 1.0-8.0 wt.% f3J. The addition of alcohol to the adsorbent allows the use of benzene desorbent, which solves the problem of contaminating the desorbent with naphthenes of 8 carbon 45 atoms. But in general, the process proceeds insufficiently sadly. The closest to the invention in terms of the achieved result is a method of separating li-xylene from a mixture of Cg-aromatic hydrocarbons by adsorption on a zeolite of the type NaX or NaY containing barium or potassium cations, or their mixture, modified by treatment with water until its content j calculated on the anhydrous basis. zeolite 1-8%. wt% According to this method, a mixture of isomers of diethylbenzene, (ortho, para, meta) AJ can be used as a desorbent. 310 However, the known method proceeds insufficiently selectively. The purpose of the invention is to increase the selectivity of the process. This goal is achieved in that according to the method of separating pxilol from mixtures of Cg-aromatic hydrocarbons by adsorption on a zeolite of the NaX or NaY type containing barium or potassium cations or their mixture, a zeolite additionally containing methyl ammonium or dimethylammonium introduced into the initial zeolite is used. its treatment with a solution of methylamine hydrochloride or diethylamine hydrochloride with the following cation content, May.%: Barium - 7.3-85.3 Potassium7.3-16.3 Methylammonium or dimethylammonium 4.0-5.8 Sodium up to 100 Barium93.6- 95.3 Methylammonium or di Methyl ammonium 1.9-3.6 Sodium. Up to 100 Potassium 70,2-74,5 Methylammonium or dimethylammonium 23.0-27.0 Sodium to 100 Raw materials always contain one or several extract components and one or several raffinate components. With regard to the separation of p-xylene and other xylenes in ethylbenzene, ft xylene is usually the extract component, at least with respect to these adsorbents, while the other xylene components and ethyl benzene are raffinate components. Adsorbents modified by the implementation of the proposed method can be used either in a single layer or in a layer, working according to the principle of pseudo-countercurrent. The conditions for the implementation of the proposed method are conventional and include the following parameters. Selectivity is roughly equivalent to extreme volatility in distillation. This parameter determines the efficiency of the adsorbent in the separation of various types of products. For a successful industrial section, 4, the selectivity should be at least about 2.0. Reduced selectivity in the separation process requires the creation of large inventories of the adsorbent. High selectivity reduces the need for inventories of the adrbent. The retention volume is a quantitative measure of the selectivity between the adsorbed products and the desorbent. In the case of para-xylene, i.e. when p-xylene is an extract or adsorbed phase, the para-xylene retention volume is an indication of how much desorbent is required to desorb p-xylene from the adsorbent. Typically, for the test conditions described below, the p-xylene retention volume should be in the range of 25 to 30 cm. A volume of less than 22 cm means that the selectivity for p-xylene for desorbent is less than one, which is undesirable. A value in excess of 35 cm indicates that too much desorbent is required to desorb p-xylene. The p-Xylene retention volume is closely related to selectivity, which is not directly proportional to the selectivity of p-xylene compared to desorbent. The selectivity of p-xylene versus desorbent from about 1.1 to 1.5 is considered ideal. This means that the desorbent and p-xylene equally well replace each other. It is necessary to avoid the relationship between p-xylene and; desorbent selectivity, which is much higher than 1, because it means that too much desorbent is required to displace the P-xylene from the adsorbent. On the other hand, the ratio between p-xylene and desorbent selectivity, which is less than 1, turns out to be disadvantageous, because although this means that to remove p-xylene from ad-. Only a small amount of desorbent is required for the sorbent, the subsequent displacement of the desorbent from the adsorbent by p-xylene when the adsorbent is brought into contact with the starting material is difficult. } 109 If we talk about selectivity, then preferably the adsorbent should be more selective for all extract components relative to the raffinate component than for the desorbent material with respect to the raffinate component. Desorbent materials should be compatible with the adsorbent and the initial mixture, i.e. they should not reduce or degrade the decisive selectivity of the adsorbent for the extract components with respect to the raffinate components. The process is carried out in isothermal and isobaric liquid phases. The process can also be carried out under conditions of pressure gradients, temperatures, desorbent concentrations, etc. In the case when the desorbent is used in a diluent medium, for example
    measures p-diethylbenzene in heavy paraffinic diluent, it is desirable to use two concentrations of diluent material to save P-diethylbenzene desorbent. With the four-zone technology of the process, a relatively weak desorbent generated in zone IV is envisaged, with the stronger desorbent being added as a regular stream of desorbent with a uniform composition. The process can also be carried out using three zones or four zones with forced bed movement, when a diluted desorbent is used in one part of a forcibly moving layer, while a more concentrated desorbent is used in the other part. Alternatively, it is possible to vary the temperature of the forcibly moving layer or the flow of materials passing through it. For some desorbents, it is common for the characteristics to change with temperature, so it may be advisable to add the first portion of the desorbent at a relatively low temperature followed by the introduction of a second portion of the desorbent at a relatively high temperature, for example, similar to SJ However, in most cases the cost and complexity of the process at different concentrations x and / or temperatures of the desorbent is economically unjustified, therefore the process of separation of aromatic compounds with 8 carbon atoms preferably carried out in isothermal conditions
    This is due to a more complete ion exchange, in which the lighter compound is involved, metalamine hydrochloride, than ion exchange, in which using concentrated desorbent. The alkylamines used are relatively inactive ion exchangers, but participating in weak ion exchange. The use of the corresponding alkylamines in the form of hydrochlorides significantly accelerates the ion exchange process. When treating the starting zeolite with an aqueous solution of the corresponding alkylamine hydrochloride between the zeolite and the alkylamine hydrochloride, a real ion exchange of RNHgHY occurs. The use of this group with a relatively short chain, such as methyl, is the most desirable form of alkylamine, since a heavier compound is involved. for example dimethylamine hydrochloride. It is possible that for a given percentage exchange both compounds act in the same way. The effect of the corresponding alkylaminohydrochloride differs depending on the type and amount of other cations on the sieves, as well as on the nature of the molecular sieves. In all cases of the test, a Y-type potassium sieve, a X-type barium sieve, and a X-type barium-potassium sieve, the separation selectivity of the pair (yra-xylene / ethyl ethylbenzene is improved with the adsorbent of the proposed method. In a similar way, the selectivity of parv-xylene / p-diethylbenzene is also improved. Example 1. Preparation of the adsorbent. The tests are carried out using four basic adsorbents. The type X zeolite (fuzhasite) used in the examples has the composition shown in Table 1. The type Y zeolite used (fujazite) holds adsorbent D of the following composition,%: potassium oxide 15.8; silicon dioxide 63.4; aluminum oxide 20.3; sodium oxide 0.5. Adsorbent A contains a relatively small amount of barium, but a large amount of potassium, so this
    The adsorbent works very well in isolating p-xylene from mixed xylene isomers when using a toluene desorbent. All adsorbents: B with a relatively high content of barium and a low content of potassium - type X fujasite; C - high content of barium - type X and D - faujasite with a high content of potassium - type Y yogurt of type 10 are broken sieves that are selective with respect to n-xylene and which are very good | even when p-diethylbenzene desorbent is used. Initial stages of preparation | and such materials are carried out in accordance with conventional ion exchange technology. The method of preparing any of these adsorbents involves placing the starting material, for example, a type X zeolite in a sodium phase, in a column, for example a long glass tube. The first stage of the ion exchange process is to pre-moisten the adsorbent with water for pre-closure. This operation must be carried out slowly and with some caution, since this is accompanied by the absorption of large amounts of heat. Depending on the specific source of the zeolitic material, it may be desirable to carry out a washing operation under mild alkaline conditions in order to eliminate the acidity and remove excess silica. In this case, when such a stage is necessary, it can be accomplished by contacting the sieves with a sodium hydroxide solution at a concentration of 0.25 weight,%, the amount of which is equivalent to a ratio of 0.0335 kg sodium hydroxide / kg dry zeolite, followed by washing water and careful drying. It may be beneficial to calcify the zeolites, but this is not necessary. Conditions for the ion exchange solution after the adsorbent is immersed in water: temperature in the column, upward flow, liquid hourly space velocity 2, use of an aqueous solution of the desired cation, for example, one that contains 0.32 wt.% Barium ions. Most suitable for the preparation of such a solution
    adding barium chloride to water. In order to prevent the creation of concentration gradients in the adsorbent of the preferred embodiment, after adding the desired amount of barium, the zeolite should be polished by circulating materials from one end of the column to the other for several hours. If you wish to add a second cation, you can perform a second ion exchange operation. If necessary, the presence of potassium ions on the zeolite, you can prepare a solution containing 0.35 wt.% Potassium, using potassium chloride as a source of potassium, and then carry out an ion exchange operation, displaced barium with potassium. After completion of the ion exchange operation, the zeolite must be washed for several hours with water and then dried. Next, the adsorbent is prepared by bringing said adsorbents into contact with the respective alkylamine hydrochloride according to the following. A 0.22 M alkylamine hydrochloride aqueous solution is recycled in an appropriate volume of adsorbent at 60 ° C for 6 hours. The adsorbent is washed from free, chloride ions, and then dried. The analysis of the adsorbent is carried out by analyzing the liquid remaining after ion exchange with alkylamine hydrochloride. A quantity of adsorbent is also analyzed to determine the percentage of carbon and the percentage of nitrogen in accordance with conventional technology. The carbon-nitrogen analysis of ion-exchange sieves with calculated equivalents of alkylamines added to sieves due to ion exchange in comparison with the amounts of removed inorganic ions is given in Table. 2. The ion equivalents removed during the ion-exchange treatment of the sieves of the two alkaline hydrochlorides tested are listed in Table. 3, In the case when there is only a slight ion exchange when using dimethylmine hydrochloride, especially in the examples with type X ity, namely adsorbents, B and C, the analytical method is to re-read to the level of its reliability limits. This is due to the fact that the quantitative indicator of ion exchange is calculated according to the analysis of the consumed impregnating solution. The analysis of large volumes of a solution containing traces of ions is associated with technological difficulties. The analytical method is much better implemented with respect to the potassium adsorbent - Y, i.e. adsorbent D, since in this case more significant amounts of cations n methylaminohydrochloride are involved in the exchange. From tab. 2, it is clear that alkylamine hydrochlorides predominantly dissolve potassium. Barium is preferably removed, depending on the amount of barium initially present. The presence of methyl ammonium and dimethylammonium ions (MA.N. and DMN.N. in the adsorbent confirms- ;, with the molar ratios between carbon and nitrogen. As a result of the described ion exchange, sieves with a cation content (wt.%), Indicated in Table 4 The adsorbent contains approximately 0.05% of chloride, calculated on the dry matter. Example 2. Selectivity test The adsorbent A is subjected to the test according to the procedure 43 After the ion exchange operation (ion exchange treatment) lacillin hydrochloride ion exchange is shown in Table 5. Example 3. Selectivity test tests The adsorbent B is subjected to the same tests. Characteristics of the adsorbent B after the alkylaminohydrochloride ion exchange treatment are shown in Table 6. Example 4. Similarly, the adsorbent C is subjected to tests. adsorbent C after completion of the alkylaminohydrochloride ion-exchange treatment is given in Table. 7. Example 5. The adsorbent D is subjected to an analogous test. The characteristics of the adsorbent D after carrying out the alkylaminohydrochloride ion-exchange treatment are given in Table. 8. Studies of the effect of water on the characteristics of the adsorbent before and after the alkylamine treatment showed that the process should preferably be carried out using sieves with relatively low water content in untreated sieves, since with increasing sieve water content, there is a tendency to decrease the selectivity to n Xylene relative ethylbenzene, as well as reducing the overall selectivity of the sieves. Carrying out the process with a water content below the optimum leads to a decrease in the degree of purity and the degree of recovery of the product, as a result of which it is necessary to ensure some level of moisture content in industrial installations. Carrying out the process without water would be desirable, since at the same time one would have to take one less variable for consideration. As in the above examples, after the treatment, all the sieves showed an increased selectivity for p-xylene compared to ethylbenzene, except in one case with adsorbent D, which was characterized by a reduced selectivity when dimethylammonohydrochloride was used. All adsorbents showed an increased selectivity for the p-xylene / p-diethylbenzene ratio, with adsorbent D having the greatest improvement, from which the selectivity varied from 0.62 to 1.52. The test results using the adsorbent A, i.e. the adsorbent originally intended for the toluene process and adsorbent D were particularly significant. After treatment with methylamine hydrochloride, adsorbent A is treated with p-diethylenebenzene desorbent, similar to adsorbent B, which is intended for use in combination with p-distilbenzene desorbent. KpQMe addition, the adsorbent And after processing acquires a slightly higher selectivity to the ratio of P-xylene / ztilbenzene in comparison with the selectivity of the raw adsorbent B, used, for example, in the well-known method f4J. This means that in industries that use adsorbent A, by carrying out an alkylaminohydrochloride treatment, an adsorbent can be obtained that can work very well in combination with p-distilbenzene desorbent. In this case, it is possible to be completely confident in good performance, since in all cases the selectivity for L-xylene in comparison with other xylenes in ethylbenzene exceeds 2.0, whereas without the alkylaminohydrochloride treatment, the selectivity according to C 3 dl. P-xylene / ethylbenzene ratios using p-diethylbenzene desorbent are unsatisfactory, less than 1.47-1.49. Such a low selectivity obtained using an adsorbent prior to treatment with an alkylamine hydrochloride is not an indication of the shortcomings of the desorbent itself, since the desorbent has very perfect properties if during these tests instead of p-diethylbenzene, toluene is used as desorbent, as in method 13 The characteristics of the adsorbent D change noticeably after the new treatment alknps. The value of the ratio between p-xylene and p-diethylbenzene varies from less than one to more than one (and the value from 1.5 is desirable), which is caused by the Absorbent Components,%
    Oxide Oxide Dioxide Oxide Oxide barium potassium silicon Alkimine sodium
    A 22.1 6.1 40.5 30.1 1.2
    B 25.1 3.1 40.5 30.1 1.2.
    From 31.5 - 38.7 28.7 1.1 Indicators11t
    ... L ...- i -. L -.... J ... i ... L ..
    Methylaminohydrochloride ion exchange (MANS exchange)
    Percentage Carbon Percentage Ammonia
    Table 2
    Adsorbent
    0,35 0,31 0,21 1,03 0,48 0,37 0,29 1,52 more good work of P-diethylbenzene as desorbent. There is no need to maintain a constant moisture content of the sieve. This indicates the possibility of adjusting the ratio of psilol / P-d ethylbenzene by adding alklaminogidrochloride in order to maximize the efficiency of the installation. , For all adsorbents tested, the retention volume of p-xylene is increased. The value of this change is that the efficiency of the sieve performance increases and the number of compounds absorbed by the adsorbent decreases. If you compare the selectivity of the distribution of p-xylene in the proposed method with known methods, for example, with method 3, which uses an adsorbent treated with alcohol or with method 2 , in which β-diethylbenzene is used as desorbent, then as can be seen from the table. 9 and 10, for the adsorbents of similar composition, the proposed method is far superior in selectivity to the known ones. Table 1
    13
    1097191
    14 Continued. 2
    15
    1097191 T a b c a 4
     Sodium Potassium exchange Methylammonium barium exchange Sodium Potassium Dimethylammonium
    20.7 17.8
    The ratio between xylene and other source components of the P-Xylene / ethylenebenzene 1,49 1,4 P-Xylene / meta-xylene 4,33 4,29 p-Xylene / orthoxylene 4,00 3,61
    The ratio of meldupsfo-xylene and desorbent PS | p ((- Xylene / p-diethylbenzene-0,68 77.4
    2.75 3.3 13.5 70.2 27.05 -5.8
    Table. five
    About 20.0
    19.7 21.6
    25.5
    0.95 5.193.6 3.2 2.8 7.3 4.4 3.6 2.48 2.04 2.281.88 4.294.28 4.04 4.51 3.17 3.76 4.00 3.71 Number water theo on the adsorbent,% Retained volume of p-xylene, see Selectivity The ratio between P-xylene and other p-Xylene / ethylbenzene2.03 P-Xylene / metaxylene 2,98 P-Xylene / orthoxylene 2, “66 The ratio between fi-xylene and Desorbe P-Xylene / p-diethylbenzene Retained volumes of P-xylene, ml
    Selectivity
    The ratio between p-xylene and other starting components
    P-xylene / ethylbenzene p-xylene / metaxylene p-xylene / orthoxylene
    The ratio between f-xylene and desorbent P-xylene /, p-diethylbenzene1 151.30
    19.9
    1.88 4.97 4.61
    33.6
    26.9
    23.7
    1.92
    1.91 4.63 5.06 4.55 4.61 19.720.930.08 22.0 with initial components 1,702,791,792.15 4.804.593.953.02 4.404.433.792.59 ntom 0.90-1.30
    nineteen
    Held volumes of p-xylene, - ml
    Selectivity
    The ratio between ncqxj-xylene and other source components. Comparison method and
    20
    1097191 T, face 8
    26.75
    37.03
    20.4 selectivity of the process according to the proposed method / 3 / and method / 2 / Table 9
    Adsorbent D
    Indicators
    Type Y
    Potassium exchange
    with .
    Table 10
    The adsorbent used in method t23
    Type Y
    Potassium exchangeable DMA-HC1 1.16
    2.03 1.74 1.83 2.64 3.29
    权利要求:
    Claims (1)
    [1]
    METHOD FOR ISOLATING P-XYLENE FROM MIXTURES OF Cg-AROMATIC HYDROCARBONS by adsorption on a NaX type zeolite (or NaY containing barium, or potassium cations, or a mixture thereof, characterized in that, in order to increase the selectivity of the process, a zeolite additionally containing methyl ammonium or dimethyl ammonium introduced into the initial zeolite by treating it with an aqueous solution of methylamine hydrochloride or dimethylamine hydrochloride with the following cation content, wt.%:
    Barium 76.3-85.3
    Potassium 7.3-16.3
    Methylammonium or Dimethylammonium Sodium or
    Barium
    Methylammonium or Dimethylammonium Sodium or
    Potassium
    Methylammonium or Dimethylammonium Sodium
    4.0-5.8
    Up to 100
    93.6-95.3
    1.9-3.6
    Up to 100
    70.2-74.5
    23.0-27.05
    Up to 100
    SU „„ 1097191
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/160,053|US4283587A|1980-06-16|1980-06-16|Adsorptive separation of aromatic isomers|
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