SA08290007B1 - Y-85 and Modified LZ-210 Zeolites - Google Patents

Abstract

Y-85 and Modified LZ-210 Zeolites Abstract The invention relates to the detection of catalysts for the conversion of polyalkylaromatics to aromatics monoalkylated compounds, in particular cumene and ethyl benzene comprising Y-85 zeolites or zeolites LZ-210 modified. For the production of cumene and ethyl benzene, an unfolded catalyst, made of 80 wt% alumina binder on a volatile-free basis, has one or more of the following physical properties: (1) Absolute intensity of zeolites Y- 85 or zeolites LZ- 210 modified as measured by X-ray diffraction (XRD) preferably at least 50% and (ii) framework aluminum for zeolites Y-85 or zeolites LZ-210 modified preferably at least 60% aluminum for zeolites Y-85 or zeolites LZ- 210 average.

Description

a x ! Y-85 and Modified 17-210 Zeolites. Full Description BACKGROUND 'Disclosed herein are 85-No and 210-LZ-modified zeolites with methods for their manufacture that can be used as catalysts for the transalkylation of polyalkylaromatics ¢ For example PIPBs « JUidl rui to cumene i . © ethyl enzenes The following description will refer to a specific reference for the use of the catalysts disclosed herein in the 'transalkylation' of polyisopropylbenzenes (PIPBs) with benzene to give: cumene ¢ but it must be known that this is done individually for the purpose of clarity and simplicity of explanation. 1 A recurring reference in this patent will be indicated to the internal field of this application for emphasis. :

0 cumene is a major trade product; Provided that one of its main uses is Ble from the source of phenol and its neutrality through air oxidation and acid-catalyzed decomposition of intermediate hydroperoxide. Because of the importance of both acetone and phenol as commodity chemicals; Great emphasis is placed on the preparation of cumene and documentation is peppered with the processes for its manufacture. The most common and perhaps the most direct way to prepare cumene is the alkylation of benzene with propylene, in particular using an acid catalyst.

-+- Another common way to prepare cumene is the transalkylation of benzene with “PIPB” and in particular: di-isopropylbenzene (DIPB) and tri-isopropylbenzene (TIPB) ¢ and in particular using a catalyst acid catalyst A commercially suitable process must meet the demands for the conversion of polyalkylated aromatic Sle Clad 0 and high selectivity to processed products; by a monoalkylated alkyl. The dominant direction of the reaction of benzene with PIPB leading to cumene corresponds to the Markownikoff addition of a propyl group. In any case; A small but very significant amount of the reaction occurs by adding an anti-Markownikoff to give n-propylbenzene (NPB). 0 The importance of the formation of NPB is that it interferes with the oxidation of cumene to phenol acetone s + as a result, the cumene used for oxidation is Lela pure in relation to the NPB content because it is difficult to separate the NPB cumene by conventional means (for example; aay “distillation”). That dan cumene be produced by transalkylation of benzene with PIPB with the lowest amount of 8 production. An important factor to consider is that the use of an acid catalyst for cross-alkylation leads to to the formation of PIPB plus with increasing temperature.Therefore, to reduce the formation of PIPB cross alkylation should be carried out at a lower temperature of silver:silver as much as possible. i YAo¢

! . where 8 and 1105 are not only the co-feeds for the transalkylation of benzene with PIPBs but also the common by-products of the alkylation of benzene with propylene when forming a cumene. Transalkylation is commonly practiced in Blend with alkylation to reduce the production of lower value by-products and to produce additional cumene. In this Jie synthesis process; 0 is typically extracted from the cumene produced by SS from alkylation and cross-alkylation in a single product stream. Since DIPB is also formed and the amount of alkylation increases and the amount of DIPB formation in alkylation increases with the increase in the degree of hall, the production of 8 must be changed in both alkylation and cross-alkylation with respect to each other so that the cumene product stream is empty Relatively DIPB. 0 What is needed is a transalkylation catalyst, Ja for example; to produce cumene or ethyl benzene; Actively enough to affect reciprocal alkylation at acceptable reaction rates at low temperatures for silver sufficiently to avoid the formation of an unacceptable DIPB. Because 177 zeolites exhibit significantly greater activity than many zeolites; It may be received in close examination as a catalyst in aromatic transalkylation. In any case; There is a problem in 1 that 57 zeolites undergo cross-alkylation at unacceptably low rates of silver at low silver temperatures desired to reduce NPB formation therefore; and for a commercial process 1 based on Y zeolites to become a reality; It is necessary to increase the activity of the catalyst ie; The rate of production of cumene or ethyl benzene increases at a lower known temperature. z

} This is the general description of the invention in fulfillment of the need referred to before; Catalysts containing Y-modified zeolites containing less than 70.7 by weight of the metal hydrogenation component are detected. One of the Y zeolites modified by Jolie sodium Y zeolite is prepared ionic ion- ; exchanging 0 with first ammonium to produce low-sodium Y zeolites i contains sodium cations ¢ has a sodium content less than 17 by weight, 1180 by weight of the zeolites Y low-sodium ¢ on a celal-free basis having cell size first unit 0 after dll) Ak thermoforms vaporize low-sodium Y zeolites low- Denhu at a temperature ranging from 2004 (710°F) to 8560°C (101Y thf) to produce 0 evaporated zeolites containing sodium cations; It has a first apparent Si/AL molecular ratio; and has a cell size of a second unit less than ana of a cell cell size of the first unit 0 at the end; The evaporated Y zeolites are contacted with a sufficient amount of an aqueous solution of ammonium ions having a pH of 11M less than 4; preferably from 7 to 4; sufficient time to exchange some lesser sodium Je cations in the evaporated zeolites Y ammonium ions J and to produce modified Y zeolites having 1 dws a second apparent SVAL molecular greater than the Si/AL ratio Adal) (virtual cd) and preferably in the range from 6.9 to .717. The unit cell size of the 77 modified zeolites is in the range from 14.74 to 4.5 7 angstroms. Another 57 modified zeolites are prepared by processing a starting material; Such as zeolites 74 -7 or 37-54 with a solution (Sb fluorosilicate) that leads to LZ- 210 zeolites and has a cell size of unit cell size 'YAo¢

{-1- first. after that; Samples treated with J) fluorosilicate are subjected to evaporation at Sha grades ranging from (<a)YY)ao Or to oY)a Ao 0 1F) to produce evaporated LZ-210 zeolites containing sodium cations; It has a molecular ratio of 5/12 to an apparent first; It has a cell size of a second unit less than the cell size of a cell of the first unit. in the end; The evaporated LZ- 210 zeolites e is contacted with a sufficient amount of an aqueous solution of ammonium ions having a Ji pH of 4 long enough to exchange at least some sodium cations in the LZ 210 zeolites - the evaporator for ammonium ions and to produce 210 LZ-modified zeolites has a second SAL molar ratio greater than the first Si/AL molar ratio; And in the range from 1.5 to .01, the unit cell size of the Y-modified zeolites is in the range from ; 5.7? to 2.5 angstroms. Then ] 0 an acid extraction can be performed to remove excess frame ammonium. Prior to the 'Y' zeolites being treated with a fluorosilicate salt or a dimension or both the catalyst may be subjected to ammonium ion exchange(s) to reduce the sodium content to 7 wt NayO by 71 wt or less with Preserving the first apparent SIAL molecular ratio. in another form; Y zeolites treated with fluorosilicate (or (LZ- 210) zeolites alternated with ammonium) without going 0 to the evaporation step to reduce the Lilia content) can be NayO to produce a material suitable for this disclosure. The disclosed manufacturing techniques depend on the number and nature of ammonium excess frame (Lewis sites of acid) as indicated by a variable 5/12 ratio and variable unit cell size which improves the incorporation properties, and increases the activity of the “jimall”. and reduce the formation of NPB YAo¢

vo z One of the disclosed catalysts comprises zeolites and a binder and has at least one property selected from the set of: (1) Absolute intensity of Y-modified zeolites as measured by X-ray diffraction Xray diffraction (XRD) of at least 00 and (1) aluminum framework for preferably modified Y zeolites at least 7680 m In one GAB the final catalyst for the production of cumene Produced absolute intensity of modified zeolites Y as measured by XRD and 7 aluminum frame for aluminum in modified zeolites Y which is greater than 47000. In another example 0 is the final catalyst for cumene production Absolute yield strength of Y-modified zeolites of 0 as measured by XRD and 7 aluminum frame for aluminum in Y-modified zeolites is greater than 49080. Other embodiments of the process disclosed herein are explained The patent is in the detailed description Brief explanation of the drawings Figure “1 graphically shows the conversion of DIPB (cy-7 axis) against temperature (- (+x ve) for catalysts prepared according to examples -7; Nor does this disclosure against the comparative examples 1 and ©; and i oF graphically shows the ratio of NPB (cy-axis wt-ppm) in the product versus conversion of 3 (7-“x-axis) for the catalysts of Example-7; and for this disclosure versus the comparative examples 1 and ©; and Fig. ? graphically illustrates the conversion of DIPB (-axis Reply %) versus temperature (x-axis M YAot ْ

; 0 z for the catalyst of Example #9 before regeneration (Example #V) and after regeneration (Example #4) and against comparative Example 1; and Fig. -ppm) in product vs. DIPB conversion (axis-ex 7) for example catalyst ? before regeneration (Example # ) and after regeneration 0 (Example #4) and vs. Comparative Example 1; and 1 Figure ©aly shows the conversion of DEB (-5% axis) versus temperature (x-axis) for example 1 catalyst for this disclosure, thus establishing that the disclosed catalysts perform well with alkyl groups Non-propyl vs. comparative example 1; f aly Figure 1 shows the conversion of DIPB (y-axis %) vs. temperature (i-axis (a x 0) for the catalysts prepared according to the examples ¢ = 06 for this statement vs comparative example SOY 1 Figure 7 Joly shows the ratio of NPB to cumene (oy-axis wt-ppm) in product versus DIPB conversion (x-axis 7) for 11-1 AB catalysts of this disclosure vs. comparative example A 11 9¢ <A JSS graphically illustrates the DIPB conversion (axis-(” 7) vs. temperature (axis-1) ox aad 1 Example No. 114 before and after renewal (Example No. 1) and against Comparative Example 11; Figure 4 shows; dail ratio of NPB to cumene (cy-axis wt-ppm) in product versus DIPB conversion (ex-axis 4) of example VE catalyst before and after regeneration (example No. 14) and against the comparative example 11. Detailed description 1: YAo¢

! 3 Improved catalysts that include a crystalline zeolitic molecular sieve are detected. Molecular sieves shall be for use in the catalyst disclosed by Ble for zeolites; Jia compounds Y-85 zeolites and 127-210. Y- 85 zeolites ' 0 with reference first to the Y zeolites of this disclosure; US Patent No. 7,170,009 explains; which are incorporated in their entirety into this patent by reference; Type 7 zeolites. Modified Y zeolites suitable for use in the preparation of the catalyst disclosed herein are generally derived from Y zeolites by a treatment that substantially modifies the structure and composition of zeolites frame 377 zeolites This is usually an increase in the apparent SAL to a value typically higher than 0 of 1.8 and/or a decrease in the unit cell size. will be understood; In any case; that in the conversion of starting material zeolites Y into zeolites Y a modifier is useful in the process disclosed in this: patent; The resulting modified Y zeolites may not have exactly the same powder X-ray diffraction pattern as the Y zeolites as described in US Patent No. 9705005. Modified Y A zeolites may have a powder X-ray diffraction pattern similar to that of US Patent 000097 but with spacings not slightly offset because; As those skilled in the field will realize; cation exchange processes; roasting operations, etc.; Which are generally necessary to convert zeolites Y into a catalytically active and stable formdh. 4 am

Z E L Z The modified Y zeolites disclosed herein have a cell size of j unit apparent SIAL modifier molecular ratio of Y zeolites in angstroms. YE.OA to 4 compounds have 1.9 to JY in preparation of Y zeolites component modified for exposed catalysts starting sale may be 0 la 2801168 in the form of alkali metal (eg » (sodium as described in US Patent No. VAT is 1 ion-exchanged for zeolites Y to form alkali metal with ammonium ions » or quarternary Ji ammonium raw materials J ammonium ions or organic cations containing nitrogen to reduce the alkali metal content to less than 74 by weight, preferably less than ZY by weight and more preferably 01 less than 77.5 By weight; expressed as alkali metal oxide Aedalkali metal by way of zeolites on a dry basis. As used in this patent; means the weight of (N20 JU) on a water-free or dry basis is the weight of the zeolites After maintaining the weight of the zeolites at degree a qu. (110) for approximately 2 hours. z Optionally, the zeolites may also contain the starting or at some stage of the adjustment procedure i to such an extent that they form content earth cations ion exchanged to contain vo-earth alkali cations such as REZ03 from 70.1 wt. to 717.5 wt. of zeolites (anhydrous basis); It is preferred from 74.5 wt. to 711 wt. It will be understood by those skilled in the art that Jalil Ionic 080860©»©-100 has less ability to introduce alkali earth cations during the exposed curing process cycle. Accordingly; 13) the cation of the earth's alkali was exchanged; For example: as the final step of the preparatory process; It may not be possible to enter even the quantity (JU 0

Yaot

+ -110- for the framework for the preferred SVAL starting material from the alkali earth cations. The ratio could be . 608 within the range is less than ? to 7; but usefully greater than zeolites Y critical factor z ammonium 1 of the ion-exchanged ion 1 is not the way to perform this exchange and can be performed by means known in the art. For example; Exchanges higher than 4 are performed. PH at these ammonium pH values for a conventional ionic Jie 0 by weight in parts such that 7111 aqueous ammonium nitrate is advantageous to use a three-stage procedure with Solution time is 1. It is zeolites to ammonium The ratio of the initial weight A in each salt phase is one hour for each phase exchange medium and exchange medium zeolites flocculation between

Y) between stages by 7.5 liters zeolites q). The VA9 is washed at a temperature of 85 °C. The zeolites are exchanged in 85 lbs. Thus, 1 kg (01.45 gallons) of water is dried per 0 at 1000 °C to 770 by weight. If (LOT) to Loss on Ignition (YY) m 001 ° | It is preferable to contact the mutual image with ¢ earth cations by using terrestrial alkali cations from an aqueous solution (Sle) with a solution of zeolites by the ammonium by the known method. From aqueous shurry A chloride salt of alkali earths mixed with an aqueous slurry may be added 1 h dap in (zeolites and 820 per gram ammonium pha “7031). zeolites to 40 m to produce an a Ao product ranging from

RE,03 Jie by weight terrestrial alkali 211 to Ao of i YAo¢

-11- after ion-exchanged 1 with ammonium is completed; The evaporation of zeolites exchanged with ammonium « and optionally exchanged with terrestrial alkali is carried out by contacting a vapor environment containing steam at an absolute pressure of 4 kpha / m²; preferably steam 1000 at 0 8°C to 0 7 0°F a AO to 5167 (<a) or from 0 7°C vo to 0 7°F (<a WAY for a period of time sufficient to reduce the unit cell size below YE angstroms, preferably to the range from YEE to YEA Angstroms.Vapor concentration of 7000 and temperature from 00C to 1117(AVY F to BLF) for 1 hour.It should be noted that a steaming step is not required to start zeolites with SIAL ratios of Tio or higher as represented by materials. 0 treatment with Cua 006 conferring higher Y/Z ratios sufficient stability to sustain acid extraction treatment 611, catalyst preparation, and hydrocarbon conversion. exchange with low pH ammonium is a sensitive characteristic of the preparation of the zeolites Y component modified for the catalyst used in the process disclosed in this ell - this exchange can be carried out in the same way as in the case of the initial ammonium exchange Except that the pH of the exchange medium is lowered to less than ϕ and of preferred i to less than ; at least during a certain part of the ion-exchanged procedure 1 . The pH is easily lowered by adding a mineral or organic acid to the ammonium ion solution. Nitric acid is particularly suitable for this purpose. preferably Acids that are insoluble aluminum salts are avoided! Yao¢

“\Y—- insoluble aluminum salts in the exchange procedure | An ion-exchanged ion with low pH ammonium + both the pH of the exchange medium and the amount of exchange medium for zeolites and the contact time of the zeolites with a medium Exchange is an important factor. It has been discovered that as long as the exchange medium has a Jil pH of ef 0, sodium cations are exchanged for hydrogen cations -hydrogen 98 in zeolites. In addition; At least some aluminum ¢ is extruded, predominantly unframe and some rim. US 30 process optimization; In any case; By acidifying the ion exchange medium with more acid than is needed to lower the pH 11C below Z4 directly. As it will be clear from the data shown below; the more acidic the exchange medium is 0; The greater the tendency to extract frame and also non-frame aluminum from zeolites. The extraction procedure is carried out to a degree sufficient to yield a zeolites product having an apparent Si/Al ratio of 1.0 to 8.70 other models' apparent SAL of 1.0 to YY and more preferably of 8 to .01 zeolites Y is typical of zeolites Y modifier-17 total silica-to-alumina used in the 10 catalyst process disclosed herein on a zeolites named 85 Y=US patents explain 14 .d 0 VARY; incorporated herein by reference; Y-85 zeolites, and its preparation; So it is not necessary in this patent to explain these in detail. As shown in Figures 1-0 and the following examples; The revealed catalysts provide increased catalyst activity” and in Ala cumene production; Reduce formation of NPB i YAot

Z Nie in the case of producing ethyl benzene from axie ethyl benzene compounds (figure ©), while the internal isomerization of the Anita groups is “_ with little interest, although ethyl de sane is smaller than the propyl group The incorporation properties of the disclosed catalysts appear to be important. 0 It is suggested that the disclosed catalyst may contain a metal hydrogenation catalytic component; this Jie component is not required. Weight of catalyst: i such hydrogenation catalytic metal component may be present at a level of less than 70.7 by weight or less than 7000 by weight calculated as the corresponding oxide of the metal component; or the catalyst may be free of any Hydrogenation catalyst metal component If present, the catalytic metal component 0 for hydrogenation dab may be the composition of the final catalyst in the form of halide s sulfide 5 oxide Jie and the like; or in the elemental metallic state. As used herein Patent » The term 'metal catalytic hydrogenation component' includes these different forms of metal compounds. The catalytically active metal Jab can be contained within the internal adsorption zone; any; pore system. of the zeolites component » or on the outer surface of the zeolite crystals or its conductor z 0 to or carried by a binder or a diluent or a yal component if Jie is used this. The mineral may be incorporated into the overall composition in any manner which will result in the acquisition of a highly dispersed state. Among the suitable methods are impregnation, adsorption, and cation exchange; and concentrated mixing. The metal can be t copper ; or silver ¢ or gold ¢ or titanium ¢ or chromium ¢ 0 tungsten 0 « molybdenum 0 0 ¢ or rhenium » or manganese ¢ or zinc ¢ or vanadium ¢ or YAot

, Ne ¢ palladium s ¢ platinum and in particular 01-8 groups TUPAC Any of the elements in i alloys of metals may be used. nickel 5 ¢ cobalt 5 « rhodium 5 Final catalyst formulations may contain the usual binders in quantities which are in the order of +75 by weight. The binder is 11 to 7785 by weight; It is preferred from the range 01 of inorganic or mixtures thereof. Amorphous oxide can be used normally 0 and alumina — silicay alumina silica and crystalline materials. Examples of suitable binders include an alumina binder. boria - silica zirconia silica s zirconia clays favourite. binder wt. binder 0 77 and zeolites wt ZA +; have the final catalyst; made from cumene to produce | Characteristics SS on a non-volatile basis; in one preferred form; and more preferably alumina 0 E X-ray as measured by X-ray diffraction Jad) zeolites Y absolute intensity of the following (1): | aluminum (Y) + at least 0 at least; and more favorable by 50 by modified diffraction (XRD) preferably by at least 770; more favorable by 778 over Y-frame zeolites (examples; The final catalyst for the production of modified asl. In under-frame aluminum zeolites Y aluminum 7s XRD modified as measured by Y zeolites yields an absolute intensity of Vo; The modified ethyl benzene, which is greater than 4709. To produce 7 zeolites in aluminum an absolute intensity z (1) of the final catalyst is preferably one; and more preferably both of the following properties: 10 on (XRD) modulated as measured by X-ray diffraction zeolites Y for | modified as zeolites Y frame for aluminum (1) at least » and less Yo . and more preferable zeolites Y aluminum at least; more preferable at least 790 than 7250 0 Favourite: YAo¢

> rate. in one GRY) the final catalyst for producing cumene has a yield strength of 7 modified Y zeolites as measured by XRD and 7 aluminum frame for aluminum in modified Y zeolites being greater than 45000 . in one of the models; The process disclosed herein uses a catalyst which is considerably dry 0 0 does not necessarily follow 1 ion-exchange with low pH ammonium by a calcination step which is Pretty much all the water around. It has been found that the performance of the catalyst in the process described herein is improved by the removal of water. In order to maintain high activity and low NPB formation, it was discovered that the content of SLA zeolites should be relatively low before being used in the transalkylation process. 0 Excess water may reduce the number of active sites and restrict incorporation to them so it does not efficiently catalyze exchange alkylation. to identify and solve this problem; Dehydration of the catalyst particles to contain the desired amount of coll prior to ead) may be effected by a drying agent which may be introduced to the cross-alkylation reaction zone; The temperature in the reaction zone may be slowly increased before the aromatic substrate or the cross-alkylatable organic matter is introduced. During this initial heating period; The water 1 content of the zeolites is determined by the equilibrium between the zeolites; catalyst and drying agent; the amount of water in the reaction zone, if any; temperatures in the reaction zone. The zeolites portion of the catalyst is very hydrophilic and the level of dehydration is controlled by adjusting the rate at which the drying agent passes over the catalyst and the temperature during the dehydration step. The drying agent may be any agent which removes water and does not have a detrimental effect on the catalyst; as molecular nitrogen; or air; or benzene 0 . The temperature is maintained during the dehydration step between YO and 00 C SY (mm)

+ve ayy m). The water content of the catalyst is calculated by measuring the weight loss on ignition (LOT) which is normally determined by the weight loss after heating for 2 hours at 100°C (oY) 1F and then subtracting the quantity from 38 by weight due to the decomposition of ammonium ion to ammonia . where the catalyst contains more water than desired; Any greater than the amount of depletion water the catalyst will contain at any time during the start of the process; Loss of water once equilibrium has been built during coal is not necessary; However, it may be desirable for the dehydration step to be implemented to give the catalyst an amount of water that is equal to or less than the equilibrium amount. Some desirable properties of the catalyst such as crush strength are achieved. strength and concentration of 0 ammonium; By controlling the time and temperature conditions at which the extruded catalyst or particles are calcined in some cases; Roasting at higher temperatures will leave the required amount of water i in the catalyst and thus make it unnecessary to perform a preferred Cilia step. so; “dehydrating drying” and “dehydration drying” as used herein means not only

1 is a separate step in which the catalyst is dehydrated after calcination but Load includes a calcination step carried out under conditions such that the desired amount of water remains on the catalyst particles. From the actual process of making the catalyst disclosed in the manufacturing plant will be understood; On 0 i.e. Js that procedures other than previously described can be used to dehydrate the catalyst either in YAo¢

1m manufacturing unit at the time the catalyst is manufactured or at a specific time (HAT) in the manufacturing unit or other location. For example, extruded catalyst particles can be dried in situ in a reactor! transalkylation by passing a water-deficient gas; such as nitrogen ; sale Jia ¢ dry reactant Jeli sala or air; or dry molecular nitrogen (> 0) over an aromatic substrate (eg) benzene or an alkylatex over catalyst (34) (TIPB or DIPB (eg dry transalkylatable aromatic exchangers at relatively high temperatures until the catalyst contains the desired amount of material the catalyst in an in situ dehydration step gas containing water deficient or sale reactant typically less than 0" part in million by weight water and the contact is made at a temperature between 0 °C (VY)!, dry flowing in nitrogen to 00 °C (477 °F).In one example, the catalyst is contacted with a 0 gas phase H at degree £AY a YOu F) The catalyst is contacted with dry benzene 0 mm Nr; (GY) ae (ae) F) to 160 F Yi) º can clad (GT) M81 (QTY) a N00 (TAY) M7001 to (Ten)] at the manufacturing unit or other location so that 1 The catalyst particles are stored in contact with an ambient gas until the desired amount of material is collected. Typically the 101th of the catalyst that is packaged in Je lia transalkylation is º ;/wt. after filling into the reactor; Preferably before using NY in the range of the catalyst reactor to enhance the transalkylation reactions ¢ the catalyst may be subjected to , 1

Yao¢

º' -1-i nitrogen A dehydration step to reduce the water content of the catalyst. The content of the disclosed catalyst is also preferably reduced for the cross-alkylation of cross-alkylatable aromatic compounds. The cross-alkylation process disclosed herein is preferably accepted as a feed a transalkylatable hydrocarbon for transalkylatable hydrocarbons. Aromatic substrate is characterized by the formation of a molecule on the basis of An aromatic base substance, Allg, of aromatic compounds, hydrocarbons, and one or more hydrogen atoms, with one or more alkylating compounds that take the place of a hydrogen atom. aromatic substrate ring structure About the ring structure of the aromatic substrate 01 de gana may be selected from Ally alkylating agent compounds Alkylation agent compounds include: various substances: as well as – acetylenic hydrocarbons and – polyolefins « diolefins 3 » monoolefins º: © alkylsulfates for last 1 and includes ¢ ethers esters and “alcohols y” alkylhalides .various esters of carboxylic acids and various esters of carboxylic acids d alkylphosphates and includes Alls Preferred olefinic hydrocarbons are olefin compounds that act as monoolefins containing only one double bond per molecule. In the disclosed process, monoolefins are either naturally gaseous or liquid. S olefins can be used as compounds that operate naturally and include:

YAot liquid olefins and liquid olefins « ethylene, propylene, I-butene, 2- butene, isobutylene

naturally high molecular weight compounds such as pentenes, hexenes, and various z-octenes; and still liquid olefins lle molecular weight; The latter include various olefin oligomers having 9 to VA carbon atoms per molecule including propylene trimer rho propylene “propylene pentamers tetramer 0 etc. Cy normal olefins may be used to © Jie, cyclopentene compounds such as cyclopentene Jia, methylcyclopentene, etc.; may be used; Although it is not necessary ¢ methyleyclohexene s cyclohexene

with equivalent results. It is preferable that a monoolefin contain ¥ and no more than VE' at least one carbon atom. More specifically, monoolefin 00 would preferably be propylene . Alkylating agent compounds are

Preferred is aliphatic hydrocarbons Cp-Cig and more preferable '. propylene

The useful aromatic substrate 63S may be selected from feeding to transalkylation from a group of aromatic compounds comprising monocyclically and in mixture with i monocyclic alkyl substituted benzene and benzene substituted by a monocyclic alkyl benzene 0

It has the structure: Gr Rn YAo¢ :

3z where R is a hydrocarbon with 1 to 14 carbon atoms; len is an integer from 1 to 0 in other words; The aromatic substrate fraction of the feed charge may be benzene ¢ and benzene containing from 1 to © an alkyl group substituent group and mixtures thereof. Unlimited examples of such feed charge compounds include benzene “, orthotropic ethyl benzene ¢ xylenes 0 ” and mesitylene (1,3,5-trimethylbenzene) + covalent with “propylbenzene” and dodecylbenzene 5 “butylbenzene and ctetradecylbenzene and mixtures thereof. It is specifically preferred that the aromatic substrate be benzene. The transalkylation process revealed may have a number of purposes. in one of them; 0 The catalyst is used for the cross-alkylation reaction zone to remove the alkylating agent compounds in excess from one of the cyclic structures of the aromatic compounds treated by a poly-alkyl 0td and to transfer the alkylating agent compound to an aromatic substrate molecule which has not been After being processed by JS and thereby increasing the amount of desired aromatic compounds produced by the process. for a related purpose; The reaction taking place in the AY cross-reaction region includes 0 removing all the components of the alkylating agent from the aromatic compound with it substituting and by doing this i converting the aromatic substrate into benzene. The feed mixture has a water concentration and compounds containing oxygen in the combined feed preferably of less than 7 ppm by weight based on the weight of the aromatic substrate and the alkylable aromatic substance passing into the reaction zone. The method by which such z vy. Low concentrations of silver in the feed mixture are acquired is not decisive for the process disclosed in this YAo¢.

-1? Innocence. usually; One stream containing aromatic ALE is supplied for cross-alkylation; With each stream, it has a concentration of water and raw materials for compounds containing oxygen so that the feed mixture formed by merging the streams separately has the preferred concentration. The water and oxygen-containing compounds can either be removed from the streams separately or Lads 0 feeding by conventional methods; jie drying; or adsorption or separation. Compounds containing z-oxygen may be any alcohol, epoxide sf, aldehyde, phenol s ketone, or ether which has a molecular weight or boiling point within the range of molecular weights or boiling points of hydrocarbons 5090816 | 0 ¢ A continuous or uninterrupted introduction of a feed mixture containing an aromatic substrate and polyalkyl-treated aromatic compounds in molecular ratios ranging from 1:1 to Vion and preferably from 1:1 to 1:01 in a cross-alkylation reaction zone containing the disclosed catalyst under cross-alkylation conditions including a temperature of 10 to 0°C (774°F); Especially from 01 to 0100 pm (058 to 7 F). 1 The pressures which are suitable for use in this patent shall be preferably higher than 1 0101 atm (kPa (absolute)) but shall not exceed 111 atm (1,717,695 z kPa (absolute) ). A particularly desirable pressure range is 0.01 to 0.010 atm to 057 kPa (absolute). A space weight velocity per hour (WHSV) of 1-1 to 00 hours' is desirable; particularly from vio to *h'; Based on a rate of 0 - polyalkylaromatics feed and total weight of the catalyst on a dry basis. while may + YAo¢ |

1 y rr ; The vapor phase process disclosed herein must be performed in the vapor phase Note that the combination of temperature and pressure used in the transalkylation reaction zone is preferably such that transalkylation reactions occur Reciprocal alkylation is necessary. in a liquid phase reciprocal alkylation process to produce monoalkylation aromatic compounds; The catalyst is continuously washed with the reactants; This prevents the accumulation of monoalkylated 0 from forming silver on the catalyst. This leads to reduced amounts of silver coke feedstock for the catalyst, and catalyst quenching is a major problem. Coke carbon on said catalyst whose formation is extended further; The selectivity is to produce a monoalkyl aromatic; In particular, the production of - in this patent as the liquid phase is higher in the catalytic cross-alkylation reaction of the cumene gas phase is comparable with the catalytic cross-alkylation reaction of the 1 0 gas phase of the process disclosed in this patent at proportions Transalkylation conditions include transalkylation that may be .1:75 to 1:1 in general from partial JST of aromatic cyclic groups per group () or less. at 1:0.706 and it is believed that the molecular ratio may be 1:1; Less than ((cumene) in the production of “propyl group 1” catalyst particles typically contain water ¢ transalkylation under cross-alkylation conditions

Lad in quantity preferably less than 74 wt. and more preferably less than 73 wt.; and more preferably an amount of nitrogen s “Karl Fisher less than 77 wt.; As measured by titration - hydrogen - (carbon (CHN) less than 720.05 wt. as measured by microanalysis. (nitrogen Y.

YAO¢

All references in this patent shall be to groups of elements of the periodic table to TUPAC 'new y notation' on the periodic table of elements in the inner front cover of the book entitled: z the book entitled CRC Handbook of Chemistry and Physics, ISBN 0-8493- 0480-6, CRC

Press, Boca Raton, Florida, U.S.A., 80™ Edition, 1999-2000. 0 as used herein; The molecular ratio of aromatic cyclic groups per z alkyl group is set as follows. The numbering of this ratio is the number of moles of aromatic cyclic groups passing through the reaction region during a specified period of time. The number of moles of aromatic cyclic groups is the sum of all the aromatic cyclic groups; regardless of the compound in which the cycloaromatic group occurs. for example » in the production of cumene; Each contributes one mole of z| with 1 mole of TIPB and 1 mole of <DIPB; And one mole of cumene and one mole of “benzene 0 ethyl” from one aromatic cyclic group to the total aromatic cyclic groups. in the production of one mole of EB from daly; And a mole of benzene from one mole of JS (EB) benzene contributes with one mole of the aromatic cyclic group to the group of z-di-ethylbenzene (DEB) groups that have the same number of aromatic alkyl atoms. The denominator of this ratio is the number of moles of | groups The carbon such as that of the alkyl group on the desired No mono-alkyl-treated aromatic material passes through the reaction zone during the same specified time period. Z 0 - 0 is the number of moles of alkyl groups is the sum of all alkyl and alkenyl groups with the same number of carbon atoms as that of the alkyl group on the desired aromatic substance treated with a monoalkylated ¢ regardless of which compound an alkyl or z | group occurs in so; The number of moles of groups is . paraffins except that alkenyl 0 y YAo¢ is not included

! 1 e | groups » iso-propyl ¢ n-propyl group; or iso-propyl JS is the sum of propyl : ic gana or ¢ n-propyl or ¢ iso-propyl ; Regardless of the compounds in which propenyl n-butane 5 “propane occurs like paraffins, except that it does not include” 71a JA, for example. propyl and metastaminate is higher than calculating the number of moles of “isobutane y i” groups in one mole of an NPB group; one mol cumene and one mol ¢ propylene mol aly contribute 0; While one propyl mole contributes to the total propyl groups to the total propyl i groups moles of EDS tri-proplybenzene and one propyl mole contributes to the ¥ DIPB groups of one JS contributes . n-propyl s iso-propyl _ to distribute the three groups between propyl groups { Lain; ethyl to collect ethyl groups one mole of EB groups and one mole of ethylene mole ° three ri-ethylbenzene contributes 1 mol ethyl mol of ¥ DEB groups contributes 1 mol 0 . ethyl any moles of ethane groups does not contribute. moles of ethyl groups  space weight velocity per hour; which is designated WHSV as used herein means “as the weight-per-hour flow rate divided by the catalyst weight; Where the weight flow rate: and the weight of the catalyst are in the same weight units. In DIPB there is little difference between moles of DIPB as used in this patent; Transformation 1 is set

JV ev in the feed multiplied by DIPB in the product; Divided by moles of DIPB feeding and moles All references in this patent are calculated to surface area using 1/00 pressure data points, using the Model 1 method. to 1.07 ranges from nitrogen partial pressure i m : 0 1 as described in: nitrogen using adsorption technology (Brunauer-Emmett-Teller) BET

Yaot

: Y=

Standard Test Method for Determining Micropore Volume and ¢ASTM D4365-95Zeolite Area of a Catalyst. In the example by: .S. Brunauer et al, J.Am. Chem. Soc, 60(2), 309-319 (1938) by absolute intensity diffraction as indicated herein; Absolute intensity measured 0 ! X-ray powder (XRD) X-ray powder of zeolites Y by calculating the normal sum of the intensities for a few selected XRD peaks of the zeolites Y and dividing this sum by the natural sum of the intensities of a few XRD peaks for standard 335 (NBS 674a alpha-alumina) which is the main standard confirmed by the National Institute of Standards and Technology (NIST) management agency 'is the product of dividing zeolites Y by the absolute intensity of US trade. 0 sum multiplied by j Yeo os 001 X (zeolites Y) intensities obedient to peaks of a material absolute intensity - 0 (intensities obedient to peaks of 0:0: # 80016 Ye [|_ (intensities obedient to standard peaks of i ( alpha-alumina In table (1), the survey parameters for the zeolites material and the alpha-alumina standard are shown. Table (1): Y zeolites for the alpha-alumina standard

SFEY 0 11-1 51-4 | 2T Mada aff Kim Mada .7p 1

Yao t rv , zeolites

ONY) oY o£) Aa (VEY) (OF) ¢(£€+) ¢(0)).YYY) Peaks (17 £) 17 AY Y) + (coo da ) 7 which zeolites Y for absolute intensity for the purposes of this disclosure; The absolute intensity can be calculated as a part by weight of the binder (Z = 001) and a part by weight Z to give a mixture of zeolites mixed with a non-admixture binder using absolute intensity on a dry basis of the intensity The absolute zeolites is not: and © is the intensity zeolites Y is the absolute intensity of A Cua “A=C(100/Z) has been made PeralSB alumina with zeolites Y For example, where 0 part by weight link You zeolites part by weight Av is mixed to give a mixture of HNO; semi-colloidal by the measured absolute intensity of the mixture on the basis of dry; the absolute intensity is ALO;

Yo f(A /001) x (10) to be Y zeolites calculating the unit absolute intensity; which is sometimes cell size as used herein; means cell size referred to as coefficient Crystal structure » unit cell size calculated using the method which 0 ((AE0) 5 (000) 5 ¢(AYY) 5 (147) for peaks XRD used a fit form to find the positions of the peaks to make the correction. (111) silicon The faujasite peak and (144) site are apparent zeolites of Si/AL as used herein; the molecular ratio as specified is based on the total amount (ALO; to Si0;) alumina to silica molecular ratio of 1; and in some zeolites (framework and non-framework) contained in silicon aluminum or the totality of the totality of 1 in this patent the molecular ratio (8:0 to alumina to silica is sometimes referred to as alumina

Yaot¢

; “YA by conventional chemical analysis which includes SAL molecular ratio (ALO; naturally occurring silicon s aluminum on all images which are zeolites of aluminum eda as is obtained) Used in this patent, the framework of the article is calculated by: Kerr-Dempsey's aluminum framework of the mass-equation formula of aluminum and the article Z “G. T. Kerr, A. W. Chester, and 10.11. Olson, Acta. Phys. Chem., 1978, 24, 169 ° .G. T. Kerr, Zeolites, 1989, 9, 350 by As used herein; means a dry substrate on the basis of weight after drying in a flowing air at temperature i by 100 m (1107 F) for one hour. The following examples are provided for illustrative purposes only and are not intended to define the scope of this disclosure. Example number = comparator 1 i { aqueous solution in aqueous solution 7- 74 zeolites From a slurried sample a slurry was made

Y- 74 zeolites m). is 1 Y) m vo by weight and the temperature of the solution is set to 1/0 NH,NO; cell size of approximately 5.7 and cell volume of Si/Al equilibrium with sodium zeolites ratio 577 is i over Na,O by weight calculated as approximately 77.17 sodium and a us content of 1.07 units. Apparent size Si/AL with a sodium zeolites Y ratio of 1-74 zeolites on a dry basis. 1 is prepared by weight approximately 79.4 sodium approximately 14.77 units; and a cell size content of approximately 4 and a cell size of approximately 4 to remove approximately 5 ammonium calculated as 118:0 on a dry basis which is exchanged with F) by following steps 111") by steam at 100 °C alumina Then remove Na from the i

Yao¢

¢

(Y) 5 (1) Generally for the procedure described in column; line 7; to column 0 line Y of US patent FY £AYY. Y= 74 zeolites are produced and obtained from UOP LLC , Des Plaines, Illinois USA 1 hour after contact at 0 V0 m (11Y); The slurry was filtered and the filtercake was washed with an excessive amount of warm de-ionized water. These steps of ion exchange (NH4+) and filtration; washing with water were repeated two more times. The filter cake had an apparent ratio of 0:51/81 and a sodium content of 70017 by weight calculated as 108: 0 on a dry basis, unit cell size of YE.0VY angstroms and absolute intensity 976 as the specified X-ray diffraction z. The resulting filter cake was dried to an appropriate moisture level; 0 and mixed with Pural 58 alumina was made semi-colloidal by HNO; to give a mixture of Av 1 part by weight of zeolites and 0? part by weight of the ALO binder; on a dry basis and moisture control to give an appropriate dough texture and then extruded to A cylindrical extrusion with a diameter of 1.00 mm (111 in). The kernels were dried and roasted at 4°C (11K°F) for approximately 1 hour in flowing air. This catalyst was representative of existing art. yo this ama catalyst had a unit cell size of 4.494 ? angstrom and absolute XRD intensity Z of 1011 and 7597.7 aluminum as a percentage of aluminum in modified Y zeolites. Z Example No. Y A slurry was prepared from another sample of 74-7 zeolites used in Example No. 1 in an aqueous solution of 7101 NH,NO; aqueous solution by weight. The pH was lowered from ; to 1: m

:

By adding a sufficient amount of solution and 1180 7117 by weight. Then the temperature of the slurry was heated to Vo 0,197°C (°C) and maintained for 1 hour. After one hour of contact in degrees ! filtercake slurry was filtered m (not 1 m)» Vo slurry was filtered with an excessive amount of warm deionized water 61 . These steps were washed and filtered; and washing with water NH” with fon exchange from acid extraction in the presence of ion exchange 0 sodium and an apparent Si/AL content of V1.0 once; The resulting filter paste had a ratio of

less than 70.00 wt. specified as Nao on a dry basis; The cell size of a z unit is 14.47 angstroms. The resulting filter cake was dried to an appropriate moisture level; And mixing it with Pure SB alumina it was made semi-colloidal by HNO; to give a mixture of 0 86 parts by weight of zeolites and 10 parts by weight of binder and 8120 on a dry basis and adjusting the humidity Z to give a suitable dough texture and then extruding it into an extrusion product Cylindrical with a diameter of 1.08 mm (VV inches). The BA product was dried and roasted at 100°C 111"(F) for 1 hour in flowing BA air. The catalyst properties were unit cell size of 7.407 ang and absolute XRD intensities of 11.59 and 797.7 aluminum as a percentage of aluminum in zeolites Y!_The rate and surface area of BET by 018 m/g Example No.? A slurry was made from another sample of 7-74 zeolites used in Example No. 1 in aqueous solution) 711 NHLNO; aqueous solution by weight. A sufficient amount of 711 HNO; i was added

by weight over a period of “0 minutes to remove part of the aluminum. Excess tire. Then the YAo¢ was heated

-1100-m) and maintain it for 90 minutes. After 90 minutes of z (1V0) 2 VA slurry temperature until slurry was filtered m (175 m) » VA contact slurry was filtered at 1 °C followed by 777 ammonium nitrate The filter cake was washed by a solution. The z oY was not repeated unlike Example No. . De-ionized excessively warm deionized water: for the second time. The resulting filter cake had an ammonium nitrate gag ratio of acid extraction at 0 on Na,O by weight specified as 70.08 sodium and a content of 8.57 lade virtual Si/AL z alumina resulting; And mix it with filter cake was dried dry base. filter cake has been dried; dried and roasted; dried extruded and extruded (HNO; made semi-colloidal by Pural SB unit cell size ana the catalyst properties were LY in the manner described for Example 10 as ammonium 781.1 absolute 18.8 and XRD of 74.487 angstroms and intensity of 0 / gram jie TAA of modified BET and surface area of Y zeolites in ammonium from Example No. The same procedure as described in Example No. ? In Example No. except that in comparison with the example a slurry was made of the same 74-7 equilibrium used in 777. HNO an increase of oF No. 14114200 719 by weight was used an amount of aqueous solution was added In 1 Mi solution Example 1 excess frame.ammonium min to remove Ye by weight over a period of 711 HNO; sufficient from M solution) and maintained for 90 min. After 1VO the slurry temperature was then heated to 74°C and the slurry was filtered vq min of contact in 0°C excessive amount of warm deionized water Alaulgy filtercake was washed ion exchange Contrary to Example No.; These ion exchange steps are not repeated. de-ionized 00

YAo ry visible amount of SIAL and filtration; And washing with water. The resulting filter cake had a ratio of NH," with by weight specified as 148:0 on a dry basis. 7007 sodium was dried and a content of 0 0 was made semi-Pural SB alumina as a result; and mixed with filter cake The filter cake was dried by the described method calcined; extruded and calcined with HNO; colloidal by 47.7 ang unit cell size The characteristics of the catalyst were LY cell size for Example No. © in ammonium as a percentage of absolute ammonium of 07.1 and 976.5/ XRD and intensity of 777 m/g. Modified BET and surface area of Y zeolites Example 0 = comparative Followed The same procedure as described in Example No. 7 in Example No. except that in comparison with the example a slurry was made of the same 74-7 equilibrium used in 757 HNO . Amount of 711 NHUNO; enough solution for 0 minutes. After 00 ad C) and maintaining it 175 ( VA C), the mortar temperature was heated up to

Jue slurry was filtered m)” Vy °) a va min. of contact in de-degree was filtered by an excessive amount of warm deionized water filtercake was washed 1 with ion exchange These steps are repeated for WY ion exchange unlike Example No. . 1 10101 apparent Si/AL, filtration; And washing with water. The resulting filter cake had a ratio (NH, by weight determined as 106:0 on a dry basis. The resulting 70008 sodium paste and Pure Alumina content was dried to a masking moisture level; mixed with the filter cake was dried Part Yo zeolites part by weight of Av to give a mixture of HNO; made semi-colloidal by 53 0

Yao¢

+ by weight of the ALO binder on a dry basis and then extruded into a cylindrical extrusion with a diameter of 0.94 mm (1/11 inch). The extrusion was dried and calcined at 600°C 111"(F) for approximately 1 hour in flowing air. The catalyst properties were a unit cell size of 74.418 angstroms, an absolute XRD of 54.78, and 1759.7 ammonium as a percentage. Percentage of ammonium© in 7 average zeolites and a BET surface area of YOU meter"/g. Example 1 A slurry was made from the same 74 Y-zeolites used in Example 1 in an aqueous Abe solution 1111,210 7211 by weight. The total amount of HNO in this example is the same as that in Example 0 on any Ya dla of the single step acid extraction procedure as shown in Example 0 in Example ©; The acid extraction is performed in two steps with 74858 total acid HNO; the total acid used in the first step and the remaining 715 total acid used in the second step. The acid extraction procedure/condition in each of the two separate steps was similar to that described in Example 0 A solution of 7117 HNO;wt was added to the slurry made of Y=4 and a solution of (1113,10). Heat the slurry to V4 m (1V0 m) and maintain 1 for 100 minutes. After 080 minutes of contact at 1°C va (Ye) the slurry was filtered 39 filtercake was washed by an excessive amount of warm de-ionized water . The acid extraction steps were repeated (with the remaining 715 d HNO used); his candidacy; washing with water; The resulting filter cake had an apparent SIAL ratio of 11104 and a sodium content of 70.09 by weight defined as 118:0 on a dry © basis. The resulting filter cake was dried to an appropriate moisture level; YAO

-? 1 and mixing it with Pure SB alumina was made semi-colloidal by (HNO; to give a mixture of 80 parts by weight of zeolites and 10 parts by weight of the ALO binder; on the basis of Gla and then extruded into an extrusion product Cylindrical with a diameter of 0.54 mm (V/V inch). The extrusion was dried and roasted at approximately 1111 000°C (1111°F) for 1 hour in flowing air. The catalyst properties were 0 unit cell size of 74.411 angstroms, absolute XRD intensity ammonium /YY.0 5 87101 aia; as a percentage of ammonium in 7 modified zeolites and surface area of BET by VAY sie "/g. Example No. 1 A slurry of the same 74 Y-zeolites used in Example No. ? in a solution of ammonium sulfate 0 718 by weight was made into this solution A solution of 71117 sulfuric acid was added over 0 minutes. The batch was then heated to 79 °C (1VO C) and held for 0 min. The heat was removed and the batch was then quenched with process water reducing the temperature to TY m (a yg ¥) and filtered. Bale was then formed a slurry of zeolites Y in ammonium sulfate 4 by weight and fixed at V4 °C (1V0 m) for one hour. The material was then filtered and washed with water. The resulting filter cake had an apparent Si/AL ratio of 1.971 and a content of 0.01 sodium/wt determined as Nay0 on a dry basis. The resulting filter cake was dried and mixed with Pure 58 alumina, made semi-colloidal by 1170, extruded 0 and dried; It was calcined and roasted by the method described for Example No. LY. The characteristics of the catalyst were a unit cell size of YEAS angstroms and an absolute XRD intensity of 715.7 ammonium IYo.Xy 0 as a percentage of ammonium in Modified Y zeolites. Table 1 summarizes the properties of the catalysts prepared in Examples 1 to 7. YAo¢

D 1 Table 1 Ce fo Figures with 1-H Y=) 6 (Y=) 1-A 1-A None 11 Period data Molecular ratio 106 8.00 Y.VA 4 10.0 000 Si/Al, apparent for zeolites Cell Size | 4,454 | 1m44 1:7 | Flama Almanda 1.4" 68 units zeolites Y absolute intensity 1.1 11.0 10.A 07.1 6 91.1 18.7 absolute intensity XRD of the catalyst absolute intensity AY.

Ved 084 Tv AY.Y AY. vit absolute intensity XRD of Y zeolites aluminum | It has 47.7 AY. 74 on vo.v vY.o zeolites LY atomic frame of aluminum with a total surface area of 77 var voi BET for the catalyst meter '/g Example No. A The catalysts prepared in Examples 1 to © and were tested for transalkylation performance using benzene-containing feed and benzene compounds treated with a polyalkylated 0 . The feed was prepared by mixing dallas benzene compounds by polyalkylation

+ a3 polyalkylated obtained from a cross-alkylating unit with benzene The prepared feed mixture represents a typical cross-alkylation feed composition with a molecular ratio of aromatic cyclic group to propyl group of approximately 7.9. The catalysts prepared by the process disclosed herein have been shown to provide the same advantages when processing feeds with basically lower or higher molecular feed ratios. done in a schedule? Summary of feed composition as measured by chromium gas autograph. The test was carried out in a solid bed reactor in a single-pass method under conditions of 447? kPa (gauge reading) (000 psi (gauge reading)) bial reactor; molecular ratio of aromatic cyclic groups to about 0.9 propyl group; and 8.” h-1 space velocity per hour for DIPB over a range of reaction temperatures. 0 The reactor is allowed to achieve necessarily stable Ala conditions at every temperature; Samples of the product were made for analysis. No stimulus smoothing was necessary during testing. before feeding; Glad) Each catalyst was subjected to a drying procedure by contact with a nitrogen effluent containing less than 10 wt-ppm water at yor °C (87;F) for 6 hours. to

11 tables? ah ms sa | 7 m- DIPB z o- DIF z 11.77 p- DIPB

TPB-4 1 1

Tetra-isopropylbenzene These examples demonstrate the benefits of high activity and product purity in the transalkylation of a polyalkylated polyalkylated to cumene attributed to catalysts prepared by the process disclosed herein. Z Third Number 9- Renewal Z 0 Example New Number Z Z

+ z A sample of the catalyst prepared in Example 7 was tested in the manner described in Example cA as z

It is explained before. After the test, the catalyst was placed into a hall in a ceramic dish ¢ which was placed in an airtight furnace. When the flowing air passes through the hermetic furnace; The temperature of the oven was raised from 0ºC 058ºF to #00ºC 0171"(ºF) at a rate of 1ºC .A) per minute; and stabilized at 86ºC 0177ºF (F). for 7 hours, then cooled to 1100 °C 7700 F. After regeneration, the catalyst was tested again in the manner described in Example A Figures 9f show the test results for catalysts before regeneration (numbered “Example 7”) and after Renewal (JES No. 4). The results show that the catalysts before and after the regeneration had similar activities and product purity states, of which the JS was better than the curve for the example number 0 catalyst; therefore, a good catalyst regeneration capability was shown. 0 Example No. 01z The samples of the catalysts prepared in Examples 1 and 7 were evaluated for polyethyl benzene crossalkylation. Each catalyst was tested using a feed consisting of a mixture of 7717.7 wt benzene and 7776.4 wt benzene (p-DEB) 28-41 µm. The catalyst was messed up in a reactor and then catalyst Z was dried by contact with a nitrogen effluent containing less than 0 wt-ppm vo water at £AY (a You) for 1 hour. The JS test was carried out at p- DEB WHSV by 1 h' and over a range of reaction temperatures from 0171°C (3748°F) to 0177°C (41°F). The reactor was allowed to achieve necessarily stable Ala conditions at each reaction temperature; Z Samples of the product were made for analysis. No stimulus smoothing was necessary during testing. Figure *z displays the results for both stimuli. The results show that the catalyst prepared in Example No. 7 has similar activity and stability or light: P97

+ is better than the curve for Example 10 catalyst and can be used for the transalkylation of poly-ethyl benzene.

A summary of the data is provided by Figures -1#. In the form of ¢ the DIPB transformation of Examples 1-; is essentially no higher than that shown for Examples 1 and ©; Provided that Example 1 is represented by the line .0010© in the form of a number; The ratio cumene/NPB is lower for Examples 4-7 nor as compared with JUL (¢) which is represented by line .700 in Fig. oF The el DIPB transformation of the non-regenerating catalyst is for Example V and the regenerating catalyst of Example 9 in comparison with Example 1 which is represented by line 011 of Figure 1 in Figure 4; The cumene/NPB ratio is lower

For the non-regenerated and regenerated catalyst for Examples No. 1 and No. 9, respectively, as compared with Example No. 1

0, which is represented by line 700 of Figure 7. In Figure 0, Example 1 shows a conversion

8 is greater than example number oY which is represented by line 10 5. The lower activity and lower product purity of the catalyst prepared in comparative example number © is thought to be because the acid lly extraction conditions were too dangerous. cell Hazardous acid extraction conditions can reduce the crystallinity of Y zeolites crystallinity LZ-210 Vo. 7 zeolites may be used in the process disclosed herein and may be prepared

By dealuminating zeolites Y dealuminating has a lower total silica to alumina molecular ratio

of 0 and is disclosed in detail in US Patents 4807077 yo 4997407, 471017, and 07759770 which are fully incorporated herein by reference. reveal innocence to

4907077 for another procedure for dealuminating zeolites Y comprising contacting zeolites Y with an aqueous solution of fluorosilicate salt using measured proportions; temperatures; And pH cases that avoid the extraction of aluminum without replacing the silicon. Patent 907077 reveals that fluorosilicate salt is used as an extraction product of aluminum 0 and also as a source of foreign silicon, which is inserted into the structure of 1 zeolites in Place the extracted aluminum. Salt has the general formula: 6 and arr) z where m is a metallic or nonmetallic cation other than 11 z has a valency “b.” A Tiel) Cations by “A” are For alkylammonium + and z 0 #amlllau Mg"™ and Nay pots and eat Bay and 7 0©" "Cu™y" and 1 "Cas and Og" 5 Fe "Bam 5 Mn" 5 Pb" and 5 "Sry Ag" Ronel 5 Zn" A preferred member of this group of 7 zeolites is known as 17-0, which is an aluminosilicate molecular sieve described zeolites explained in patent 4007077 . Zeolites 17-210 and other zeolites 0 of this group are suitably prepared from starting material zeolites 7. In one embodiment; Zeolites 17-210 have a total molecular ratio of silica to alumina from ©* to 11. The unit cell size ranges from 1.78 to 74.50 angstroms; It is preferred from 74.460 to 7.464 Angstroms. Class 17-210 of the zeolites used in the process and the composition disclosed in this patent shall have a composition expressed in terms of the molecular ratios of the oxides as in the following formula: YAo¢

—\¢— (0.85-1.1)M,4,0 : AL,O3: xS10, where Sle "MY" is a valence cation of "0" and "172" has a value from © to .11 In general, 12-210 zeolites may be prepared by dealuminating Y-type zeolites using an aqueous solution Ale of fluorosilicate salt, preferably hexafluorosilicate solution. Ammonium removal can be carried out by placing zeolites 77 naturally but not necessarily 57 zeolites alternated with ammonium “in an aqueous reaction medium such as an aqueous solution of ammonium acetate” and slowly adding a solution aqueous ammonium fluorosilicate (aqueous solution). After the reaction is allowed to progress, zeolites are produced that have an excess total silica to alumina molecular ratio. The amount of increment of 1 depends at least in part on the amount of fluorosilicate solution in contact With zeolites and on the allowed reaction time Normally, a reaction time between 10 and 4 hours is sufficient for equilibrium to be achieved The resulting solid, which can be separated from the aqueous reaction medium by Auli filtration techniques, is Zeolites 127-210. In some cases this product may be steam roasted by methods known in the art. For example; The product may be in contact with 1 water vapor at a partial pressure of 0.4 kPa (absolute) (107 psi (absolute)) for a period between 1/4 to ? hours at a temperature between 87°C (00°F) pM You. ) q) in order to provide greater crystalline stability. In some cases the product of the steam roast may be subjected to exchange with ammonium by methods known in the art. For example; The product may be slurryed with water after which ammonium salt is added © the slurry. The resulting mixture is typically heated for a period of hours; his candidacy; And washed it with water. Yao¢ is done

Describe ways to evaporate zeolites 127-210 and exchange it with ammonium in US Patent Nos. in one of the models; Exchange with ammonium is followed by treatment with an aqueous solution (a fluorosilicate salt) to increase the Si/AL ratio, enhance the hydrothermal bit 0, and decrease the natural tendency to form ammonium overframe. It can be done Carry out 1 ion-exchange with ammonium for zeolites 12-210 final low pH which is preferred; in the same way as in the case of initial exchange with ammonium for zeolites Y (and/or zeolites LZ-210 as described before) except that the pH of the exchange medium is lowered to less than 0 and preferably less than 0 oF during eda at least from the ion exchange procedure 1 10-10.The pH reduction is easily accomplished by adding a mineral or organic acid aD acid to the ammonium solution.Nitric acid is Particularly suitable for this purpose. Preferably, acids that are non-ALE salts of insoluble aluminum salts are avoided. In 1 ion exchange procedure 01-100 with low pH 10 ammonium they The pH of the exchange medium, the amount of exchange medium for the zeolites, and the contact time of the zeolites with the exchange medium are important factors. It has been discovered that as long as the exchange medium has a pH of less than 4; sodiumdl ions at +10 sodium cations are exchanged for hydrogen cations at 65 and additionally; © At least some of the ammonium is extracted; And predominantly non-frame and some frame. YAo¢ is being improved

1- ion- ionic | exchange medium; process efficiency; In any case; By acidifying the exchange medium the pH is lowered with more acid than is needed to lower the pH » 0 from £ directly. As it will be clear from the data presented below; The more acidic the ammonium exchange medium is; The greater the tendency to extract a tire and also exchange medium 4d zeolites, the extraction procedure is performed to a sufficient degree to produce a product. Unframed zeolites from © 1.0 Virtual from SIAL The ratio gyal virtual from 6.5 to *©7. In SAL forms a ratio of .01 and more preferably from 1.5 to YY to Examples 17-210 are provided for illustrative purposes only and are not intended to define the scope of this disclosure. Comparative 11 - Example #7 /11 NH, NO; aqueous solution in a solution of Y- 74 zeolites, then a slurry was made from a sample of 0 zeolites consisting of 7- 74 zeolites by weight, and the temperature of the solution was set to mm m (not 1 m). It is 1.07 unit cell size and Lu 5.7 in a equilibrium ratio of RL8/g8 apparent by approximately sodium 7 by weight calculated as 118:0 on a dry basis. 77.7 sodium, an apparent 1/51 “Louis” content of approximately £.9 and a volume of sodium zeolites Y of Y-74 zeolites preparation by weight approximately calculated as 79.4 sodium approximately 7.77 units; and cell size vo content and then Na approximately from Vo aly ammonium on a dry basis which is exchanged with NayO and (7) as (1(q) by following steps (11117) steam at 00°C alumina strip * US Patent Y generic for the procedure described in column; line 7; to column © line

UOP LLC, Des Plaines, was obtained from 7- 74 zeolites produced. 77 6/7

Yao¢

m Illinois USA 1 hour after contact in degree V TY (a V0 m); The slurry was filtered and the filtercake was washed with an excessive amount of warm de-ionized water. These steps of ion exchange (NH4+) and filtration; water washing were repeated two more times; the filter cake had an apparent 5:/812 ratio of 0 by 0.7 and a content of 7000 sodium by weight calculated as 116:0 on Gils basis, unit cell size of 4.577 7 angstroms, absolute intensity 97 as specified X-ray diffraction The resulting filter cake was dried to an appropriate moisture level; Colloidal by and 1170 to give a mixture of sia Ae by weight of zeolites and 1 7 parts by weight of the ALOs binder on a dry basis and adjusting the humidity to give Ve an appropriate dough texture and then extruding it into a cylindrical extrusion product with a diameter of 0.94 mm (V/V) inch). The extrusion was dried and roasted at 6010°C (1117°F) for approximately one hour in flowing air. This catalyst was representative of existing art. This ana catalyst had a unit cell size of 14.494 angstroms, an absolute XRD of 11.1, and 7817.7 Apu aluminum of aluminum in modified Y zeolites. vo Example No. 07) The zeolites 54-7 synthesized were exchanged with ammonium and then treated with ammonium fluorosilicate according to the procedure described in US Patent 4,503,03. 7-54 is sodium zeolites 7 with an apparent ratio of 5:/812 of £9.ly, a unit cell size of 175.71, and a sodium content of 79.4 by weight calculated as 11820 on a dry basis. . 0 Y- 54 zeolites is produced and obtained from UOP LLC, Des Plaines, Illinois USA.

0? evaporation of the resulting 77 zeolites; which had an apparent molecular ratio of 5/812 of To at 111°C (111°F) by steam 7001 for 1 hour; And then exchange it with ammonium. The cake was dried “51:6_the resulting filter cake to an appropriate moisture level; And mixing it with Pure 58 alumina was made semi-colloidal by HNO; to give a mixture of Av part by weight of © zeolites and 10 part by weight of the ALO binder; based on Gila and adjusting the moisture to give a suitable dough texture and then Extrude it into a cylindrical extrusion with a diameter of 0.54 mm (1/11 inch). The extrusion was dried and calcined at 00°C (GIF) for approximately 1 hour in flowing air. The resulting catalyst had a unit cell size of 75.477 angstroms, an absolute XRD intensity of AV.T, and 717.7 aluminum frame as a percentage of aluminum in the modified Y zeolites. 11 Example No. 0 fluorosilicate and then treated with ammonium synthesized with 7- 54 zeolites exchanged 57 zeolites £04 YoY was evaporated according to the procedure described in the US patent ammonium in LZ-210 ( 9) output; which has an apparent molecular ratio of 5/812 by 1 and is referred to as 1 hour. A slurry manufactured 7001 F) was first prepared by steaming 111" (600 °C 1111/10 evaporator) and 77 g 11:0 evaporator. A solution of 17- 210 (9) aba YYA of 0 was then added.

LZ-210 (9) by weight to slurry 0 70 of, 011(710) aba TTY and 11.0 aha 711 made from the evaporator. The temperature of the resulting mixture was then raised to 85°C (140) and then mixed for a period of time. by weight; and the mixture was preserved 7717 HNO; min. To this mixture » 5.7 grams of min. were added at the end of the acid extraction; Tr q) was done with continuous stirring for 0825 (result at 85 m 001 m and then dried at 0001 ml (HHO). The mixture was filtered and the paste was washed by v.

Yao¢

YY) F) All night long. in the second part; 001 aha of dry paste was added to a solution made of 1597 g of 0 (NHNO; 75 wt) and 0019 (HO aha) to which 01 0 abs of and 1170 777 by wt were added. The resulting slurry was mixed for 010 min. Thereafter, the mixture was filtered and washed by 0001 ml 11:0 and the filter cake was dried in the oven at 7100°C (717(a) overnight. The zeolites had The result is an apparent SAL ratio of 00187 NayO 70.077 by weight The zeolites powder was mixed with Pure SB alumina made semi-colloidal by W1110 to give a mixture of 80 parts by weight of zeolites and 10 parts by weight of The ALO binder was dried on a dry basis and the moisture was adjusted to give an appropriate dough texture and was then extruded into a cylindrical extrusion with a diameter of 0.54 mm (1/11 in.). The extrusion was dried and roasted at approximately 0002°C (1°F). for one hour in flowing air. The resulting catalyst had a unit cell size of 7.470 ang, an absolute XRD intensity of 18.4 aluminum ZVY.A frame, and a BET surface area of 161 Jie/g. Example No. VE Synthetic Y-54 zeolites were exchanged with ammonium and then treated with ammonium Yo fluorosilicate according to the procedure described in US Pat. 07 49.07. The resulting 5 zeolites having an apparent molecular ratio of 51/812 by 9 and denoted as (9) LZ-210 in ERE IL TONE degree F) was evaporated by steam 7001 for 1 hour. An amount of 157 LZ-210 (9) evaporated aba was added to 1158 grams of NHNO; 777 wt. to the zeolites slurry; aba YA of 7117 HNO; wt. was slowly added over a period of Te min. The slurry was then heated to 08°C (171°F) and held at 20°C (GV) for 00 min. At the end of:

lac acid extraction; The slurry was quenched by 46 aba 11 11:0, filtered, washed with 1110g NELNO;777 by weight, washed with 10001ml HHO and then dried at 100°C (7011thF) for the night. The resulting zeolites had a ratio of Si/Al, apparent Na;O 0.748 720.04 by weight. The zeolites powder was mixed with Pure SB alumina and made semi-colloidal © by W1170 to give a mixture of 80 parts by weight of zeolites and 10 parts by weight of binder ALOs on a dry basis and moisture control to give an appropriate dough texture and then with its confidence into a cylindrical extrusion with a diameter of 4 mm (1/11 inch). The extrusion was dried and roasted at approximately 100°C (1117°F) for 1 hour in flowing air. The resulting catalyst had a unit cell size of 70,797 angstroms, an absolute XRD intensity of 19.7 ZAV.A5 aluminum frame, and a BET surface area of 0 44 lm aba example #11 Synthetic Y-54 zeolites were exchanged with ammonium and then treated with ammonium fluorosilicate according to the procedure described in US Patent 4,503,03 (US The resulting Y zeolites were evaporated; which has a molecular ratio of 8/812 apparent of 11 and denoted as (12) 210 LZ- at 10°C (GY) by steam 7001 for 1 hour. A slurry made of aba 771 (12) 210- 17 evaporator and 1768 g 11:0. A solution of 111/110 made of 711 g 11.0 and 1697 g of 10(L1O0 0 75 by weight) was then added to the evaporated LZ-210 (12) slurry. The temperature was then raised The resulting mixture was reduced to 85 M (VA) and then mixed for 1V min. To this mixture 7.4 g of HNO 777 by weight was added and the resulting mixture was maintained at 185 (a A V) with Continuous stirring for 100 minutes. At the end of the acid extraction, the mixture was filtered and the dough was washed with 1000 ml (HHO) and then dried: 4 m.

_$ A = 1001 grams of dough overnight. In the second part, YAY (001 m) was added at 11.0 aba 1580 degrees and by weight 0 75 (NHONO; from dry pha TTY to a solution made of min. After that, it was 01 of and 1170 777 by weight. zeolites m (71 F) overnight. The 001 was in the oven at 0 degrees. Pural SB alumina was made with zeolites by weight. Zee (NayOg VV) powder was mixed. 4 parts by weight of binder 01 and zeolites 80 parts by weight to give a mixture of HNO; Semi-colloidal by on a dry basis adjusting the moisture to give a suitable dough texture and then extruding it into an ALO, 1000 m extruder with a diameter of 1.09 mm (1/16 inch). The extrusion product was dried and calcined at cell size ana for 1 hour in flowing air. The resulting catalyst had a sad (approximately 1117) 0 aluminum frame of 796.9 81.7 ang, an XRD of 7.791 ang, a haf intensity of 7/19 m BET, and a surface area of 01 eg No. (before evaporation) to the Vo solution of Example No. LZ 210 (12) grams of 150 of 0:11 was added. The slurry was heated pha and 1709 75 0 (NHNO; grams of 5000 made of 1111/210 ( Vo slurry was F) and held at temperature for 2 hours. The slurry was then filtered (0 ¥)a until 40 and washed with water. The paste was then exchanged with 1071,850 and washed with water Once again by following the same filtered m) for F) Nw oven at degree filter cake was dried procedure. The resulting ratio of zeolites overnight. The zeolites were to give HNO. It was made semi-colloidal by Pural SB alumina with zeolites powder mixing ¥. On dry basis and ALO control; Part by weight of the binder 71 and zeolites part by weight of 80 mixture (V/V) 0.54 mm moisture to give an appropriate dough texture and then extrude it into a cylindrical extrusion product with a diameter of mm

_$9_ inch). The extrusion was dried and calcined at 100°C 111"(F) for approximately 1 hour in flowing air. The resulting catalyst had a unit cell size of 74.471 angstroms and an absolute XRD intensity of VY .Y and 789.7 aluminum frame and a BET surface area of 1780 t/g m/g © Jas summarizes the properties of the catalysts prepared in Examples 11 to Table AT Fig. 1-3 None None 4-1 l Solution Cycle solution Molecular ratio AN 8.0 A 7 17.4" 7.7 7.7 Si/Al, apparent zeolites Y ana cell 16" "7 1 7 | 74 | :) a | YEEYS 68 units Y zeolites angstrom absolute intensity 1.1 1m 7/76 .7 mm L A absolute intensity XRD of the catalyst absolute intensity 7 Vere | ad AA 0" | 11 3.1 absolute intensity J XRD Y zeolites aluminum 8.7 177 mil km 11.4 km 97.1 zeolites A JY atomic frame of aluminum total surface area avy via 511 16 116 BET for catalyst meter "/g d

EXAMPLE 11 The catalysts prepared in VUE Examples 11 were tested for transalkylation performance using a feed containing benzene and benzene compounds treated with “. The feed was prepared by mixing benzene compounds treated with polyalkylated 0 obtained from a commercial exchange alkylation unit with benzene. The composition of the feed as measured by chromium gas autograph is summarized in the preceding table (1). The test was carried out in a fixed bed reactor in a single-pass method under 447 conditions. ?kPa (gauge reading) (0 +0 psi (gauge reading)) of reactor pressure; molecular ratio of cycloaromatic to propyl groups approximately 7.7; +A h-1 space velocity per hour l

DIPB 0 over a range of reaction temperatures. The reactor was allowed to achieve necessarily steady-state conditions at every temperature; Samples of the product were made for analysis. No stimulus smoothing was necessary during testing. before feeding; Each catalyst was glad to a drying procedure by contact with a nitrogen effluent containing less than 01 wt-ppm water at °Yo. mm £AY) for 7 hours.

1 Figures (1) and (7) show the test results for the catalysts prepared in Examples 11 and 1-16. In Figure (7), the catalyst prepared in Examples 1-16 shows higher activities (i.e. conversion higher DIPB at a known temperature) as compared with curve 000 of Example No. 11 in o(V) form. The catalysts prepared in Examples 16-16 show better product purity values (i.e. cumene /NPB is less in a known DIPB conversion) than Curve 7010 for the catalyst prepared in Example No. 1. Referring to Figures 1-OHV

© JU Statements No. 11 that no evaporation and acid extraction steps are required in the preparation

4 m17

1e catalyst as good performance is achieved even when both are omitted. Referring to Figures (1) Ladd (V) the data for Example VE shows that superior activity and equivalent product purity can be achieved using a single-step evaporation acid extraction; Yay from the two-step acid extraction of Example 1 Although the conditions for acid extraction are more dangerous. Example No. YA then test a sample of the catalyst prepared in Example No. 5 in the manner described in Example No. VY as described before. After 1 to test ' then put The spent catalyst is placed in a ceramic dish' which is then placed in a sealed furnace. While the flowing air is passed through the sealed furnace' the temperature of All is raised from (GV0A) a Ve to #001 or (G6) YY) at a rate of 1 m 0.8 (f) per minute; and fixed at 0177 (Joo.F) for 1 hour; Then cooling to 100 m (YF) F). The regenerated catalyst had a unit cell size als of 1.14 angstrom, an absolute XRD intensity of $78, an aluminum frame of 78 m, and a surface area of 101 BET m/g. summarizing table; Characteristics of the regenerated catalyst. after renewal; The catalyst was tested again in the manner described in Example 117. The catalysts before and after regeneration had similar activities (sf (conversion of DIPB at a known temperature) and product purity values of NPB (sl) cumene 0 upon conversion DIPB is known) and therefore a good catalyst regeneration potential has been shown. Example No. 14 and then select a sample of the catalyst prepared in Example No. 1 in the manner described in JU No. and as described before. After the test, the spent catalyst was regenerated in the manner described in Example No. VA After regeneration, the ye catalyst was tested again in the manner described in Example No. AY YAo¢

7e Figures (A) 5 (3) show test result data for the catalysts before regeneration (numbered “Example No.” (“VE”) and after regeneration (numbered JU No. (“VS”) The results show that the catalysts before and after regeneration have similar activities (i.e., higher DIPB conversion at a known temperature) and better product purity values (ie, Jil cumene /NPB at a known 21713 conversion) and that they were better than Curves 601 700 for Figures (A) and (9) On the 0 order of the OY example catalyst therefore shows good Sine regeneration potential.The above examples show the benefits of high activity and product purity in the transalkylation of polyalkylating compounds such as DIPB and 1175 to DEB cumene to EB is attributable to catalysts prepared by the process disclosed herein. Although the disclosed catalyst may contain a metal hydrogenation catalytic component 0 such a component is not required. On the basis of catalyst weight it may be a This Jie metal hydrogenation catalytic component present at a level of less than 0.7 7 by weight or less than 7000 by weight calculated as the corresponding oxide of the metallic component; Or the catalyst may be free of any hydrogenation catalytic metal component. if any; The hydrogenation catalytic metal component within the final catalyst composition may be in the form of a compound such as Wy halides sulfides oxide 00 similar; Or in the elemental metal case. as used herein; The term "metal hydrogenation catalytic component" shall include these various forms of metal compounds. The catalytically active metal can be contained within the internal adsorption zone; any; pore system. for the zeolites component; Or on the outer surface of the zeolite crystals or connected to or 0 carried by a binder, diluent, or other component if Jie C 127 is used

oh this. The mineral may be incorporated into the overall composition in any manner which will result in the acquisition of a highly dispersed state. Among the suitable methods are impregnation ¢ and adsorption; cation exchange ¢ and concentrated mixing. The metal can be: copper©0008, silver for silver ¢, titanium 0 ¢ gold ¢, chromium ¢ 0 molybdenum ©, ALL, rhenium ¢ or manganese ¢ or zinc ¢ or vanadium “¢ or any of the elements in the TUPAC groups V+ ~A and in particular palladium y ¢ platinum ¢ nickel 5 ¢ cobalt s » rhodium . Mixtures of minerals may be used. Final catalyst compositions may contain the usual binders in amounts which are in the range 01 to 795 by weight; Preferably from 11 to 0 75 wt. The binder 0 is normally an inorganic oxide or mixtures thereof. Amorphous and crystalline can be used. Examples of suitable binders include alumina - silicay alumina silica and boria - silica zirconia silicay zirconia s clays. Aluminadl is a preferred binder. to produce cumene; have the final catalyst; made of ZA by weight zeolites and 1077 by weight alumina binder 10 on a non-volatile basis; in one preferred form; and more preferably IS than; The following characteristics: (1) absolute intensity of 37 modified zeolites as measured by X-ray diffraction (XRD) of 50 over JE and more preferably at least 10; 5 (Y). ) frame aluminum for zeolites 7 preferably modified by at least 718; and more preferably ZV at least than for zeolites modified aluminum Y. In one example the final catalyst for producing cumene has a yield strength of +0 absolute So 7 modified zeolites as measured by XRD and / aluminum frame for aluminum: M7

6e

In 57 zeolites the rate is greater than 4709 . To produce ethyl benzene ¢ is the catalyst

final with one preferred image; and more preferred both; The following characteristics: (1) Absolute intensity of

7 zeolites modified as measured by X-ray diffraction (XRD) by

at least 5; and more preferably Vo at least and (7) aluminum frame for Y zeolites preferentially modified by at least 7590; and more preferably at least 0 than aluminum zeolites

7 average. In one ABN the final catalyst for cumene production is highly productive of zeolites

zeolites Y in aluminum frame of aluminum 7 3 XRD modified as measured by Y

The rate which is greater than 49000 .

While only certain models are indicated, they will be obvious substitutions and modifications from the foregoing description for those skilled in the field. These and other alternatives are considered equivalents and within the spirit and scope of this Disclosure and Elements

Attached protection.

Yao¢

Claims (1)

protection elements 1-1 aromatic catalyst for aromatic transalkylation catalyst comprising zeolite "modified 12-210 at a ratio ranging from about 75 by weight to about 7908 by weight" on a volatile-free basis And a binder of alumina, alumina binder | £; The molar ratio of the modified zeolite 17-210 containing the SIAL © mass is in the range from about 8 to about ¢YY and there is a ratio ranging from 1 7707 to 7958 aluminum in the modified zeolite 17 -210 in the form of framework aluminum. 17- Modified zeolite catalyst according to claim (1); Where the molar ratio of a substance, Y = 1 YY, ranges from 1.9 to SIAL, which has a mass of 210 " LZ-modified zeolite catalyzed by claim (1); where the absolute strength of a substance is -* 1 . X-ray diffraction at least according to diffraction measurements or about 210 " LZ-modified zeolite catalyzed by claim (1); Where is the absolute strength of Article 4-1 . X-ray diffraction at least according to 01 diffraction measurements of approximately 210 Y LZ modified zeolite catalyst per claim (1); Where the absolute intensity of -* 1 + X-ray diffraction material at least according to Vo-ray diffraction measurements is about 210 " \ 1- The catalyst according to the claim (1) ', where the content of Na, O in the modified zeolite is LZ-210 ‎YAO Y is less than 77 by weight based on the weight of the water-free zeolite. 1 7” - the catalyst according to the element of protection (1); where the percentage of loss in the catalyst material upon burning 1 under 0010 °C ranges from about To by weight to about 4 by weight. 1 - the compound according to the protection alc ( \ ) where the size of one cell in the zeolite "modifier 127-210 ranges from about 7.74 to about YEOA angstroms. 1 1 - the catalyst according to the protection element (1 ), as it contains a ratio ranging from about 0 75 by weight to about 785 by weight zeolite rate 17-210 JA of volatile-free basis ¥ -10 1 catalyst The catalyst according to claim (1) 1, where the catalyst is free of “metal hydrogenation” components. metal hydrogenation 7 _ by less than 77 on the basis of the weight of the catalyst 11-1 aromatic catalyst for the AY aromatic transalkylation catalyst comprising zeolite "modified 12-210 in a ratio ranging from about 75 by weight to Approximately 7900 by weight on a “volatile-free basis” and an alumina binder ¢; the absolute intensity of the modified zeolite is 17-210 according to the diffraction axl measurements © Nie is at least 0; there is a ratio from 717 to 7958 Yao¢ Lat 7 of aluminum in modified zeolite LZ-210 in the form of framework aluminum VV. z (VY) the catalyst according to the protection element (VY) where the product of the absolute intensity of the material Y 201:6 is 17-210 according to X-ray diffraction measurements; with a percentage! 7 For framework aluminum in modified zeolite material 17-210 is a value of z f in total greater than AY -14 0 1 catalyst according to the protection element (VY) where it is The molar ratio of the modified zeolite ¥ 17-210 containing AS 2 to 5:/8 ranges from about 1.9 to about YY z "and the volume of one cell is in the range from about 14.74 to about YEOA angstroms. 11-1 “transalkylating aromatics” process “in which the “transalkylating aromatics” with the aromatic z ¥ substrate is passed to the reaction zone; The conversion alkylate aromatic compound is contacted with a Z substrate; The aromatic compound with the catalyst according to the element of protection (1) in the reaction zone under suitable conditions for dial alkylation, that is, under a temperature ranging from about 100 “C to 0079” C; and under a pressure of 1 ranging from 1 to 101 atmospheric; and with a water concentration of less than about 10 ppm on a 1" basis z the sum of the weight of the trans-alkylatable aromatic compound and the substrate passing into the reaction zone z reaction zone ~~ A -0 1 process according Claim (10) where the temperature during the transalkylation process ranges from about 00 C to 7178 Mea “C; and the pressure ranges from about YAo¢ —0 A Ye YF is about 560 atmospheres. -17-1 Process according to claim (10) where the transalkylating aromatics ~~ Y contains at least one of the “polyalkylaromatic |” selected from a group consisting of polyisopropylbenzenes And polyethylbenzenes ¢-108#1. transalkylating aromatics; In which the “transalkylating aromatics” and the aromatic YF substrate are passed into the reaction zone; the transalkylating aromatics and the aromatic substrate are contacted with the catalyst according to the protection element (VY) © in the reaction zone under conditions suitable for transformational alkylation, i.e. under 7 temperature ranging from about 100°C to °F and pressure ranging from 1 to 101 atmospheres; And at a water concentration of less than about Yo ppm based on the total weight of the transalkylating aromatics A and the substrate passing into the reaction zone 9 -19 1 the process according to the claim (VA In it, the temperature during the transalkylating process ranges from Mea 110 “C to about” C, and the pressure ranges from about 0 to about Ee atmospheric. -01-1 Operation according to claim (18); where the convertible aromatic compound is YAo¢ 9e Y containing at least one of the polyaikylaromatic polyalkyl aromatic compounds selected "| from a group consisting of polyisopropylbenzenes and polyethylbenzenes. : M