ALKYLATION OF BENZENE TO FORM LINEAR ALKYLBENZENES USING FLUORINE-CONTAINING MORDENITE

Abstract: This invention is directed to a fluorine-containing mordenite catalyst and use thereof in the manufacture of linear alkylbenzene (LAB) by alkylation of benzene with an olefin. The olefin may have from about 10 to 14 carbons. The fluorine-containing mordenite is prepared typically by treatment with an aqueous hydrogen fluoride solution. The benzene alkylation may be conducted using reactive distillation.

Description: ALKYLATION QF BENZENE TO FORM LINEAR ALKYLBENZENES USING FLUORINE-CONTAINING MORDENITE Technical Field This invention generally relates to the alkylation of benzene with olefins using mordenite catalysts. Background Art Linear alkyl benzenes (LAB's) having long chains (typically 10-14 carbons) are commonly used, commercial products LAB's are commonly sulfonated to thereby produce surfactants. Typically, LAB's are manufactured commercially using classic Fπedal-Crafts chemistry, employmg catalysts such as aluminum chloride, or usmg strong acid catalysts such as hydrogen fluoride, for example, to alkylate benzene with olefins. While such methods produce high conversions, the selectivity to the 2-phenyl isomer is low, generally being about 30% or less. LAB's with a high percentage ofthe 2-phenyl isomer are highly desired because such compounds when sulfonated have long "tails" which provide enhanced solubility and detergent properties. Summary oflnventipp It has now been recognized that a need exists for a method of LAB production having high substrate olefin conversion, high selectivity to 2-phenyl isomer LAB, and employmg a catalyst having long hfetimes and easy handling. This invention provides a solution to one or more of the problems and disadvantages descπbed above This invention, in one broad respect, is a process useful for tlie production of monoalkylated benzene, comprising contacting benzene with an olefin containing from about 8 to about 30 carbons in the presence of fluonne-containing mordenite under conditions such that linear monoalkylated benzene is formed. In a second broad respect, this invention is a process useiiil for the production of monoalkylated benzene, compnsmg introducing a feed composing olefin having about 8 to about 30 carbons and benzene mto a fluonne-containing mordenite catalyst bed under conditions such that monoalkylated benzene is produced, allowing benzene, olefin, and monoalkylated benzene to descend (fall) into a reboiler from the catalyst bed, removing monoalkylated benzene from the reboiler, and heating the contents ofthe reboiler such that benzene refluxes to further contact the fluonne-containing mordenite. In another broad aspect, this mvention relates to mordenite useful for alkylating benzene with olefin havmg a silica to alumma molar ratio of about 10T to about 100:1; wherein the mordenite has been treated with an aqueous hydrogen fluoride solution such that the mordemte contams from about 0.1 to about 4 percent fluorine by weight. In another broad respect, mis invention is a method useful for the preparation of fluonne-containing mordemte, compnsmg contacting a mordemte having a silica to alumina molar ratio in a range from about 10 1 to about 100:1 with an aqueous hydrogen fluonde solution havmg a concentration of hydrogen fluonde in the range of from about 0.1 to about 10 percent by weight such that the mordemte containing fluonne is produced, collecting the fluonne-containing mordemte by filtration, and drying. The fluonne treated mordemte catalyst advantageously produces high selectivities to the 2-phenyl isomer in the preparation of LAB, generally producmg selectivities of about 70 percent or more Also, the fluonne treated mordenite enjoys a long lifetime, preferably expeπencing only a 25 percent lr less decrease in activity after 400 hours on stream. A process operated in accordance with the apparatus depicted in FIGS. 1 and 2 has the advantage that nsmg benzene from the reboiler continuously cleans the catalyst to thereby mcrease lifetime of the catalyst. In addition, this invention advantageously produces only low amounts of dialkylated benzene, which is not particularly as useful for detergent manufacture, as well as only low amounts of tetralin denvatives. Certain terms and phrases have the following meanings as used herein "Meq/g" means milliequivalents of titratable acid per gram of catalyst, which is a unit used to descnbe acidity of the catalysts. Acidity is generally determmed by titration wim a base, as by adding excessive base, such as sodium hydroxide, to the catalyst and then back titrating the catalyst "Conv." and "Conversion" mean the mole percentage of a given reactant converted to product Generally, olefin conversion is about 95 percent or more in the practice of this invention. "Sel " and "Selectivity" mean the mole percentage of a particular component in the product Generally, selectivity to the 2-phenyl isomer is about 70 or more in the practice of this invention. The mordenite catalyst of the present invention is useful as a catalyst in the production of LAB's m accordance wim the process of manufacturing LAB's of this invention. LAB is useful as starting mateπal to produce sulfonated LAB, which itself is useful as a surfactant. Brief Description of the Drawings FIG 1 shows a representation of a first contmuous reactive distillation column employed in the practice of this mvention. FIG. 2 shows a representation of a second continuous reactive distillation column employed in the practice of this invention. Detailed Description of he Invention Catalyst Preparation and Properties The catalyst of this mvention is a fluonne-containing mordemte. Mordenite is a type of zeolite. The catalyst of this invention is prepared from hydrogen mordenite (typically havmg 0.1 percent or less of sodium) having a silica-alumina molar ratio of from about 10:1 to about 100:1. More typically, the starting mordenite has a silica/alumina molar ratio of from about 10.1 to about 50:1. The starting hydrogen mordemte, which is commonly available commercially, is treated with an aqueous solution of hydrogen fluonde ("HF") to produce the active, long-life and highly selective catalyst ofthe invention. In the course of such HF treatment, as well as duπng subsequent calcination of said HF-treated mordenite, the silica/alumina molar ratio typically mcreases. The finished catalysts of this invention show a fluonne content of from about 0.1 to about 4 percent by weight, more typically about 1 percent. While not wishing to be bound by theory, it is believed that the HF reacts with sites where -Si-O-Al- linkages occur such that the linkage is broken with fluonne becoming bonded to the Al such that -Si-OH and F-Al- groups form This is believed to decrease the total Bronsted acid sites and mcrease the strength of the remaining acid sites in the mordenite and is believed to stabilize the acidity of the mordenite such that the mechanisms which degrade performance dunng LAB production, such as coke build-up, are retarded The aqueous solution used to treat the mordenite may contain a range of HF concentrations Generally, the HF concentration is a minimum of about 0.1 percent by weight. Below such minimum concentration, the effect ofthe fluonne treatment significantly decreases, resultmg in the undesirable need for repeated treatments Generally, the HF concentration on the upper end is about 10 percent by weight or less Above a concentration of about 10 percent by weight, the HF is so concentrated that it is difficult to prevent HF from destroying the crystallmity ofthe mordenite, thereby detrimentally affecting its efficacy as a catalyst for LAB production The aqueous HF solution may be prepared by diluting commercially available 48% HF solutions to the desired concentration Alternatively, HF can be sparged into water to provide an aqueous HF solution Typically, the treatment is earned out by adding mordemte powder or pellets to a stirred aqueous HF solution at a temperature of from about 0°C to about 50 °C The stirπng and contactmg is continued for a time sufficient to achieve the desired level of fluonne in the mordenite This time may vary depending on factors such as HF concentration, amount of HF solution relative to the amount of mordenite being treated, speed of agitation is employed, and temperature After treatment, the mordemte can be recovered by filtration, and then dned It is also possible to impregnate the mordenite to incipient wetness with a given HF solution, as well as to treat the mordemte with gaseous hydrogen fluonde Preferably said fluonde-treated mordenite would be calcined m air pπor to use in alkylation service The preferred calcination temperature would be in me range from about 400 °C to about 600 °C Alternative mordenite fluorinating agents to hydrofluoπc acid and hydrogen fluonde mclude ammonium fluonde, fluoπded silicon compounds and fluonded hydrocarbons The HF-treated mordemte of this mvention generally has about 0 1 percent by weight or more of fluonne based on the total weight of the mordemte Typically, the fluorine-containing mordemte contams about 4 percent by weight or less fluonne The fluonne-containing mordemte most typically contams about 1 percent by weight of fluonne The mordemte can be used in the practice of this invention as a powder, in pellet form, as granules, or as extrudates. The mordemte can be formed into pellets or extrudates usmg binders well known to those of skill the art, such as alumina, silica or mixtures thereof Reactants for LAB Production In me practice of tins mvention, benzene is alkylated with olefin to form LAB These reactants can be handled and punfied as is generally performed by those of skill m the art. In this regard, it is preferred that the reactants are water and alcohol free The olefins employed in the practice of this invention have from about 8 to about 30 carbons, preferably from about 10 to about 14 carbons, such as is available commercially or produced as dehydrogenated paraffin feed stocks. It is preferred that the olefin be monounsaturated It is most preferred that the olefin be an alpha-olefin contammg a terminal ethylenic unit Commonly, said olefins would be available in a paraffinic media of the same carbon range. Olefins in the 10 to 14 carbon number range would typically be available from C ,„ to C. H paraffin dehydrogenation in a C , 0 to C. M paraffin mixture havmg an olefin content of 5 to 20% Often, the olefin content of said olefin- paraffin mixmre would be 8 to 10 weight %. The 2-phenyl isomer ofthe LAB produced in accordance with this invention is of formula: wherem n is from about 5 to about 17 and preferably from about 7 to about 11. Process Conditions, Procedures, and Apparatus The process of this invention can be earned out using the contmuous reactive distillation column depicted in FIG. 1. In FIG. 1, a feed mixture of benzene and olefin, generally at a benzene-to-olefin molar ratio range of about 1:1 to 100:1 flows from feed pump 10 to feed inlet 14 via lme 12. The feed mixture falls to packed mordemte catalyst bed 32 where alkylation m the presence of the fluonne-containing mordemte occurs. Alternatively, while not depicted m FIG. 1, the benzene and olefin can be introduced separately mto the bed with mixing occurrmg m the bed, or the reactants can be mixed via an m-line mixer pπor to introducing the reactants into the catalyst bed, or the reactants can be injected separately above the bed with mixing affected by use of standard packing above the bed, or the reactants can be sparged mto the chamber above the bed. The catalyst bed 32 depicted in FIG. 1 for laboratory scale may be made of two lengths of 1.1 inch internal diameter tubing, the lengths bemg 9.5 inches and 22 inches. In the catalyst bed 32, the falling feed mixture also contacts nsing vapors of unreacted benzene which has been heated to reflux in reboiler 42 by heater 40. Such πsmg vapors pass over thermocouple 38 which monitors temperature to provide feedback to heater 40. The πsmg vapors of benzene and/or olefin also pass through standard packing 36 (e.g., 7.5 inches of goodloe packing) The nsmg vapors heat thermocouple 30 which connects to bottoms temperature controller 28 which activates heater 40 when temperature drops below a set level Pπor to startup, the system may be flushed with nitrogen which enters via line 54 and which flows through lme 58. After startup, a nitrogen blanket is maintained over the system. Also pnor to startup and dunng nitrogen flush, it may be desirable to heat catalyst bed 32 so as to dπve off water from the fluorine- containing mordemte Residual water from the feed mixture or which otherwise enters the system is collected in water trap 24 upon bemg liquified at condenser 21 (along with benzene vapor). If the feed is very dry (free of water) the water trap 24 may not be needed. Removing water leads to longer catalyst lifetime. Hence, the water trap 24 is optional. The same applies to FIG. 2. Condenser 21 is cooled via coolant such as water enteπng condenser 21 via port 22 and exiting via port 20. As needed, water in water trap 24 may be drained by opening drain valve 26. As needed, when LAB content in reboiler 42 πses to a desired level, the bottoms LAB product may be removed from the system via line 47, usmg either gravity or bottoms pump 48 to withdraw the product When product is so withdrawn, valve 44 is opened. In FIG. 1, dip tube 46, which is optional, is employed to slightly increase the pressure in reboiler 42 to thereby raise the boiling point of benzene a degree or two. Likewise, a pressure generator 56 may be optionally employed to raise the pressure of the system. Other standard pressure increasing devices can be employed. Pressure can thus be increased m the system such that the boiling pomt of benzene increases up to about 200 °C. In FIG. 1, control mechanisms for heat shutoff 50 and pump shutoff 52 are depicted which serve to shut off heat and pump if the liquids level m the system πses to such levels. These control mechanisms are optional and may be mcluded so that the catalyst bed does not come into contact with the bottoms of the reboiler. In the practice of this mvention in the alkylation of benzene, a wide vanety of process conditions can be employed. In this regard, the temperature in the catalyst bed may vary depending on reactants, rate of mtroduction into the catalyst bed, size of the bed, and so forth. Generally, the bed is mamtamed at the reflux temperature of benzene dependmg on pressure. Typically, the temperamre of the catalyst bed is above about 70 °C, and most likely about 78 °C or more m order to have reasonable reaction rates, and about 200 °C or less to avoid degradation of reactants and products and to avoid deactivation ofthe catalyst by coke build-up Preferably, the temperature is in the range from about 80 °C to about 140°C. The process may be operated at a vanety of pressures duπng the contactmg step, with pressures of about atmosphenc most typically bemg employed. When the process is operated usmg a system as depicted in FIGS. 1 and 2, the reboiler temperature is mamtamed such that benzene and olefin vaponze, the temperamre varying dependmg on olefin, and generally being from about 80 °C to about 250 °C for olefins havmg 10 to 14 carbons. The composition of the reboiler will vary over time, but is generally set initially to have a benzene olefin ratio of about 5:1, with this ratio being mamtamed duπng the practice of this invention. The rate of mtroduction of feed into the catalyst bed may vary, and is generally at a liquid hourly space velocity ("LHSV") of about 0.05 hr" 1 to about 10 hr "1 , more typically from about 0.05 hr "1 to about 1 hr '. The mole ratio of benzene to olefin introduced mto the catalyst bed is generally from about 1:1 to about 100:1. In commercial benzene alkylation operations, it is common to run at mole ratios of from about 2:1 to about 20:1, which can suitably be employed m the practice of this invention, and to charge said olefins as an olefin-parafϊin mixture compπsmg 5% to 20% olefin content. Said olefin-paraffin mixtures are normally generated commercially through dehydrogenation ofthe corresponding paraffin starting matenal over a noble metal catalyst Another contmuous reactive distillation apparatus is depicted in FIG. 2 In FIG. 2, the feed mixture enters the reactor via feed inlet 114. The feed mixture falls through the column into catalyst bed 132, wherem alkylation to form LAB occurs. A thermowell 133 monitors the temperature of said catalyst bed 132. The catalyst bed 132 may be optionally heated externally and is contamed withm 1-1/4 inch stainless steel tubing Goodloe packing is positioned at packing 136 and 137. LAB product, as well as unreacted benzene and olefin, fall through packing 136 into reboiler 142 In reboiler 142, electnc heater 140 heats the contents of reboiler 142 such that heated vapors of benzene and olefin πse from the reboiler 142 to at least reach catalyst bed 132. As needed, the bottoms LAB product may be removed from reboiler 142 by opening bottoms valve 144 after passmg through line 147 and filter 145. Residual water from the feed mixture, or which otherwise enters the system, may be condensed at condenser 121 which is cooled with coolant via inlet lme 122 and exit lme 120. The condensed water falls to water trap 124, which can be drained as needed by opening dram valve 126 Temperature in the system is monitored via thermocouples 138, 130, and 165 The system mcludes pressure release valve 166. A nitrogen blanket over the system is mamtamed by mtroduction of nitrogen gas via mlet line 154. Level control activator 150 activates bottoms level control valve 151 to open when the liquids level in the reboiler nses to the level control activator 150 While the systems depicted in FIG 1 and FIG 2 show smgle catalyst bed systems, it may be appreciated that multi-catalyst bed reactors are within the scope of this invention, as well as multiple ports for inlet feeds, water traps, product removal lmes, and so forth. Moreover, the process may be run m batch mode, or in other contmuous processes usmg plugflow designs, tnckle bed designs, and fluidized bed designs It is believed that as average molecular weight of olefins increases, particularly when the average number of carbons exceed 14, the selecnvity and conversion to LAB, especially LAB with the 2-ιsomer, may incrementally decrease If desired, the product of the alkylation using HF-treated mordenite may be sent to a second, fimshing catalyst bed to improve yield This procedure is optional and is believed to be dependent on the needs and desires of the end user. An example of such a second catalyst is HF-treated clay such as montmonllonite clay havmg about 0.5% fluonde. Such a catalyst may also ser to lower the bromine number below about 0 1 , depending on conditions The following examples are illustrative of the present invention and are not intended to be construed as limiting the scope ofthe invention or the claims Unless otherwise indicated, all percentages are by weight In the examples, all reactants were commercial grades and used as received The apparatus depicted in FIG 1 was employed for examples 2-4 The apparatus depicted rn FIG 1 was used for example 5 It may be noted that example 2 illustrates LAB production from paraffin dehydrogenate using the fluonde-treated mordenite catalyst of example B, where good catalyst life (250+ hrs) is achieved without catalyst regeneration, while mamtammg a 2-phenyl LAB selectivity of >70% and high LAB productivity without sigmficant loss of fluonde. Comparative example 1, on the other hand, using untreated mordemte, with no fluonde added, shows a rapid declme in LAB production. In addition, examples 3 and 4 illustrate LAB production usmg a 5:1 molar benzene/C, 0 -C 14 olefin feed mix and the fluonde-treated mordemte catalysts of Example B when operating at different LHSVs m the range of 0.2-0.4 hr '. Catalyst life may exceed 500 hours. Example 5 illustrates LAB production with the fluonde-treated mordenite catalyst where the alkylation is conducted at higher temperatures and under pressure. Examples 6-8 illustrate the performance of three HF-treated mordenite catalysts with different fluonde loadings. Example 9 shows how virtually no alkylation activity is observed with a highly-fluonnated mordemte. EXAMPLE A This example illustrates the preparation of a hydrogen fluoπde-modified mordemte. To 30 g of acidified mordenite (LZM-8, SιO,/Al 2 0 3 ratio 17; Na 2 0 wt% 0.02, surface area 517 m 2 /g, powder, from Union Carbide Corp.) was added 600 ml of 04% hydrofluoπc acid solution, at room temperature. After 5 hours the solid zeolite was removed by filtration, washed with distilled water, dned at 120°C overnight, and calcmed at 538°C. EXAMPLE B The example illustrates the preparation of a hydrogen fluoπde-modified mordenite To 500 g of acidified, dealuminized, mordemte (CBV-20A from PQ Corp.; Sι0 2 /Al 2 0 3 molar ratio 20; Na 2 0, 0.02 wt%; surface area 550 m 2 /g, 1/16" diameter extrudates, that had been calcined at 538°C, overnight) was added a solution of 33 ml of 48% HF solution in 1633 ml of distilled water, the mix was cooled in ice, stirred on a rotary evaporator overnight, then filtered to recover the extruded solids. The extrudates were further washed with distilled water, dned in vacuo at 100°C, and then calcined at 538°C, overnight. Analyses ofthe treated mordenite showed. F: 1.2% Acidity: 0.49 meq/g EXAMPLE 1 This example illustrates the preparation of linear alkyl benzenes usmg a hydrogen fluoπde-modified mordemte catalyst. To a 500 ml flask, fitted with condenser and Dean Stark Trap was added 100 ml of benzene (reagent grade) plus 10 g of hydrogen fluoπde-modified mordemte zeolite, prepared by the method of Example A. The mix was refluxed for 15-20 minutes to remove small amounts of moisture, then a combination of benzene (50 ml) plus 1-dodecene (10 g) was injected mto the flask and the solution allowed to reflux for 3 hours. Upon cooling, the modified mordemte catalyst was removed by filtration, the filtrate liquid flashed to remove unreacted benzene, and the bottoms liquid analyzed by gas chromatography. Typical analytical data are summaπzed m Table 1. TABLE 1 DODECENE LAB ISOMER DISTRIBUTION (%) HEAVIES LINEAR LAB (LLAB) CONV. (%) 2-Ph 3-Ph 4-Ph 5-Ph 6-Ph (%) (%) 99.7 79.9 16.6 0.8 1.3 1.3 0.2 95.9 EXAMPLE 2 This example illustrates the preparation of linear alkylbenzenes from paraffin dehydrogenate usmg a hydrogen fluonde-treated mordenite catalyst. In the example, benzene was alkylated with a sample of C, 0 -C| 4 paraffin dehydrogenate contammg about 8.5% C| 0 -C, 4 olefins. Alkylation was conducted m a process unit as shown in FIG. 1. Alkylation was conducted by first charging 500 ml of a benzene/paraffin dehydrogenate mix (10:1 molar ratio, benzene/C 10 -Cι 4 olefin) to the reboiler and 250 cc of the HF-treated mordemte of example B to the 1.1" (2.8 cm) i.d. reaction zone. The mordemte was held in place using Goodloe packmg. The reboiler liquid was then heated to reflux and a benzene plus C 10 -C, 4 paraffin dehydrogenate mix (10:1 molar ratio, benzene/C 10 -C, 4 olefin) continuously introduced into the unit above the catalyst column at the rate of 100 cc/hr. (LHSV=0.4 hr 1 ). Under steady state, reflux, conditions liquid product was continuously withdrawn from the reboiler and water contmuously taken off from the water trap. The crude liquid product was periodically analyzed by gas chromatography. The reboiler temperature was typically in the controlled range of 97-122 °C. The column head temperature vaπabi ty was 78-83 °C. A summary of the analytical results may be found in Table 2. After 253 hours on stream, the recovered HF-treated mordemte catalyst showed by analysis: F: 1.1% Acidity: 0.29 meq/g H 2 0: 0.3% Table 2 Comparative Example 1 This example illustrates the preparation of lmear alkyl benzene from paraffin dehydrogenate usmg an untreated mordenite catalyst. Following the procedures of Example 9, the alkylation unit was charged with 250 cc of untreated, calcined, mordenite, (die starting mordenite of Example B), and the liquid feed compnsed benzene plus C 10 - C l4 paraffin dehydrogenate mix in a 10:1 molar ratio of benzene/C,o-C, 4 olefin. Typical results are summanzed in Table 3. The recovered mordenite showed by analysis: Acidity: 0.29 meq/g H 2 0: 2.1% Table 3 Time on Stream Sample Alkylate 2-Phenyl C 6 H 6 Cone. (Hrs) Cone. (%) Sel. (%) (%) 0 0 11.2 2 1 6.50 9.9 4 2 7.16 73.2 17.1 6 3 7.09 73.1 26.4 22 4 8.61 73.9 26.6 31 5 10.49 67.4 15.8 46 6 7.39 75.0 27.7 70 7 6.39 75.1 28.5 93 8 6.08 73.6 23.0 144 9 5.21 73.6 15.8 157 10 4.40 73.9 26.2 180 11 3.06 69.6 27.1 204 12 1.32 19.5 228 13 1.32 33.3 EXAMPLE 3 This example also illustrates the preparation of linear alkyl benzene from paraffin dehydrogenate usmg a hydrogen fluonde-treated mordenite catalyst. Following the procedures of Example 2, the alkylation unit was charged with 250 cc of the HF- treated mordenite of Example B, and the liquid feed compnsed a benzene plus C 10 -C, 4 paraffin dehydrogenate mix in a 5:1 molar ratio of benzene/Cι 0 -C] 4 olefin, the reboiler temperamre was typically in the range of 122- 188°C, the column head temperature 78-83 °C. Typical analytical results are summanzed in Table 4. After 503 hours on stream, the recovered HF-treated mordenite catalyst showed on analysis: F 1.0% Acidity: 0.35 meq/g H,0: 0.1% Table 4 Time on Sample Alkylate 2-Phenyl Corrected" Stream (Hrs) Cone. (%) Sel. (%) Cone. (%) Alkylate Cone. (%) 0 0 1.0 8.9 1.1 2 1 3.5 61.8 0.3 3.5 4 2 7.1 72.1 0 7.1 6 3 6.8 76.7 7.2 7.3 34 4 8.4 79.7 14.3 9.8 71 5 7.2 81.8 14.6 8.5 96 6 6.5 80.8 15.5 7.7 119 7 6.3 80.6 15.1 7.4 643 8 6.0 81.0 14.3 7.0 168 9 5.9 80.7 14.4 6.9 239 10 5.0 78.2 8.8 5.5 263 11 5.3 79.2 13.5 6.2 288 12 5.0 79.6 16.5 6.0 311 13 5.4 79.4 4.1 5.6 335 14 5.5 79.2 8.2 6.0 408 15 4.9 79.4 13.1 5.6 432 16 4.7 78.8 14.4 5.5 456 17 4.4 78.5 14.1 5.1 479 18 a 4.7 78.6 2.7 b 4.8 488 19 b 4.9 78.5 2.4 C 5.0 503 20 b 5.1 78.9 0.6 C 5.1 * Corrected for benzene in effluent sample. b Applied pressure 8" (20.32 cm) H z O Applied pressure 12" (30.5 cm) H 2 0 Example 4 This example also illustrates the preparation of linear alkyl benzenes from paraffin dehydrogenate using a hydrogen fluonde-treated mordenite catalyst. Following the procedures of Example 2, alkylation was conducted in the glassware unit of FIG. 1 complete with catalyst column, reboiler, condenser and controls. To the reaction zone was charged 500 cc of HF-treated mordemte of Example B. The liquid feed compπsed a benzene plus C 10 -C 14 paraffin dehydrogenate mix in a 5:1 molar ratio of benzene/C l0 -C, 4 olefin. The feed rate was 100 cc/hr (LHSV:0.2 hr ')• Under typical steady state, reflux, conditions, with a reboiler temperature range of 131-205 °C and a head temperamre of 76-83 °C, typical results are summanzed in Table 5. Table 5 Pressure Reboiler Time on Sample Alkylate 2-PhenyI CA Corrected" (Inch Temp. Stream Cone. Sel. (%) Cone. (%) Alkylate H 2 0) (OC) (Hrs) (%) Cone. (%) 12 205 2 1 8.2 74.3 0.5 8.3 193 4 2 9.2 75.0 0.4 9.2 175 6 3 10.0 74.8 2.3 10.3 204 21 4 12.7 78.7 0.3 12.7 146 44 5 11.7 81.0 10.4 12.9 136 68 6 11.5 81.8 10.0 12.7 2-3 days C b 11.6 81.4 9.4 12.7 136 93 7 11.3 82.6 10.8 12.5 4-5 days C-l b 11.0 81.8 11.0 12.2 142 165 8 10.4 83.0 11.4 11.5 142 189 9 10.2 83.4 10.5 11.2 146 213 10 9.7 80.2 11.2 10.7 139 238 11 9.6 83.4 11.1 10.7 143 261 12 9.9 81.9 11.0 11.0 133 333 13 9.2 83.4 11.3 10.3 138 356 14 8.9 83.5 11.1 9.9 138 381 15 8.8 83.0 1 1.3 9.8 131 405 16 8.7 82.8 1 1.2 9.7 a Conected for benzene in effluent sample b Composite product EXAMPLE 5 This example illustrates me preparation of linear alkyl benzenes from paraffin dehydrogenate using a hydrogen fluoride-treated mordenite catalyst. Following the procedures of Example 2, alkylation of benzene with C 0 -C l4 paraffin dehydrogenate was conducted using the stainless-steel unit of FIG. 2, complete with catalyst column, reboiler, condenser, and controls. About 250 cc or HF-treated mordenite of Example B was charged to the column. The liquid feed compπsed benzene plus C| 0 -C (4 paraffin dehydrogenate mix in a 10:1 molar ratio of benzene/C I0 -C |4 olefin. The LHSV varied from 0.2 to 0.4 hr 1 . Alkylation was conducted over a range of column and reboiler temperatures and a range of exit pressures. Typical results are summaπzed in Table 6. Table 6 Column Pressure Pot Time Sample Alkylate 2- H 6 Temp Temp. (hr) (#) Cone. Phenyl Cone. (OC) DIFF EXIT (OC) (%) Sel. (%) (psi) (psi) (%) 149-129 0.1 0 188 4 1 3.8 6.3 152-126 0 0 200 20 2 1.8 32.7 195-108 0 0 199 25 3 5.7 8.7 218-111 0 0 201 28 4 0.8 67.5 212-118 0 0 201 44 5 8.8 71.7 4.5 209-114 0.2 0 198 52 6 2.4 47.3 228-116 0 0 197 68 7 6.9 72.6 12.4 187-107 0.5 0 197 76 8 2.9 74.6 44.1 76 Ψ 4.8 72.9 25.3 9C b 6.8 72.2 1.0 174-107 0 0 178 6 10 4.1 79.2 54.9 170-106 0 0 172 22 11 2.0 59.8 28 12 a 6.6 76.8 26.8 142-107 0 0 136 31 13 4.8 67.9 18.9 141-110 0 0 138 47 14 4.4 65.9 16.9 142-110 0 0 136 55 ' 15 5.0 63.9 16.6 168-1 11 0 0 131 71 16 4.1 64.8 16.7 170-108 0 0 150 79 17 5.0 72.0 8.8 175-113 0 0 143 95 18 5.9 68.1 15.2 145-106 0 5.2 188 14 19 3.2 60.2 9.0 149-108 0 4.2 186 20 20 4.8 66.3 12.0 160-118 0 11.7 213 29 21 4.2 6.7 160-119 0 9.3 210 44 22 5.2 6.6 ' Composite product ' Stripped composite product Examples 6-8 These examples illustrate the preparation of linear alkyl benzene usmg hydrogen fluoπde-modified mordenite catalysts wim different fluonde treatment levels. Followmg the procedures of Example 1, me alkylation unit was charged with benzene (100 ml), a 10 g sample of hydrogen fluoride-modified mordenite prepared by the procedure of Example B, plus a mix of benzene (50 ml) and 1 -decene (10 g). Three HF-treated mordemtes were tested, having the composition: Catalyst "C" 0.25% HF on mordemte (CBV-20A) Catalyst "D" 0.50% HF on mordemte (CBV-20A) Catalyst "E" 1.0% HF on mordenite (CB V-20A) In each experiment samples ofthe bottoms liquid fraction were withdrawn at regular peπods and subject to gas chromatography analyses. The results are summaπzed m Table 7. Table 7 CATALYST TIME %LLAB %ISOS %HVY %2Ph %3Ph %4Ph %5P %6&7Ph h D 10 11.75 0.14 0 73.36 21.87 2.89 0.94 1.02 20 12.43 0.21 0 72.97 21.96 3.14 1.13 0.81 30 12.88 0.21 0 72.67 22.13 3.03 1.16 1.01 40 12.27 0.22 0 73.02 21.92 2.85 1.06 1.14 50 12.15 0.98 0 72.46 21.67 3.21 1.17 1.49 50 12.24 1.01 0 72.53 21.63 3.23 1.12 1.44 60 12.28 0.21 0 72.96 22.07 2.93 1.14 0.91 60 11.98 0.21 0 72.97 22.21 2.93 1.17 0.83 C 10 12.2 0.18 0 72.54 22.46 3.21 0.98 0.82 20 12.7 0.39 0 71.51 22.61 2.91 1.02 2.13 30 12.52 0.21 0 71.96 22.68 2.96 1.04 1.36 40 12.75 0.21 0 71.84 22.67 3.22 1.02 1.25 50 12.98 0.21 0 71.57 22.81 3.16 1.08 1.39 60 12.54 0.21 0 71.45 22.81 3.19 1.12 1.44 60 12.33 0.21 0 71.61 22.87 2.92 1.05 1.31 E 10 10.56 0.05 0 75.19 19.41 2.18 3.22 20 12.95 0.15 0 74.36 19.23 3.01 3.4 30 13.44 0.18 0 74.11 19.42 3.2 3.27 40 13.16 0.15 0 074.16 19.38 3.12 3.34 50 13.1 0.15 0 74.43 19.16 3.21 3.28 60 12.83 0.15 0 74.28 19.49 2.88 3.35 60 12.87 0.16 0 73.82 19.97 2.8 3.2 Example 9 This example illustrates the inactivity of a heavily loaded hydrogen-fluonde modified mordemte catalyst. Following the procedures of Example 2, the alkylation unit was charged with 100 cc of a hydrogen fluonde-treated mordenite (CBV-20A) prepared by the method of Example B but having a much higher loading of HF (fluonde content 4.8%) The acidity of said HF-treated mordenite was 0.15 meq/g. No significant amount of alkylated product was detected by gas chromatography.

Claims: What is Claimed is: 1. A process useful for the production of monoalkylated benzene, compnsmg: contacting benzene with an olefin of from about 8 to about 30 carbons in me presence of fluonne-containing mordemte under conditions such that monoalkylated benzene is formed 2. The process of claim 1, wherein the fluonne-containing mordenite has a silica to alumina molar ratio in a range from about 10:1 to about 50:1, wherein the mordenite has been treated by contacting mordemte with an aqueous hydrogen fluonde solution, wherein the hydrogen fluonde in the aqueous solution has a concentration the range from about 0.1 to about 5 percent by weight. 3. The process of claim 1 or 2, wherem the olefin has from about 10 to about 14 carbons. 4. The process of claim 1 , 2, or 3 wherein me monoalkylated benzene contains about 70 or more percent of 2-phenyl isomer. 5. The process of claim 1, 2, 3 or 4 wherein the mordenite contains in a range from about 0.1 to about 4 percent by weight of fluonne. 6. The process of claim 1, 2, 3, 4 or 5 further compπsmg: allowing benzene, olefin, and monoalkylated benzene to descend mto a reboiler from the catalyst bed, removing monoalkylated benzene from the reboiler; and heating me contents of me reboiler such that benzene refluxes to further contact the fluonne- containing mordenite. 1. The process of claim 6, wherein the benzene to olefin ratio in the feed is about 2:1 to about 20:1, wherein the catalyst bed is mamtamed at a temperature of about 75 °C to about 200 °C, and wherein the feed is mtroduced into the catalyst bed at a liquid hourly space velocity of about 0.1 hr "1 to about 1 hr' 1 . 8. The process of claim 1, 2, 3, 4 or 5 wherem me benzene to olefin ratio is about 2:1 to about 20:1, wherein the fluonne-containing mordenite is maintained at a temperature in a range from about 75 ° C to about 200° C, and wherein the benzene and olefin is mtroduced into the fluonne-contammg mordenite at a liquid hourly space velocity of about 0.1 hr ' to about 1 hr "1 . 9. The process of claim 6 or 7 further compnsmg collecting water overhead to the catalyst bed in a water trap. 10. Mordemte useful for alkylating benzene with olefin having a silica to alumina molar ratio in a range from about 10:1 to about 100:1; wherein me mordenite has been treated with an aqueous hydrogen fluonde solution such that the mordenite contains fluonne m a range from about 0 1 to about 5 percent by weight. 11. The mordenite of claim 10, wherein the silica to alumina molar ratio is about 10:1 to about 50:1. 12. A method useful for the preparation of fluonne-containing mordemte, compπsmg: contacting a mordenite havmg a silica to alumina molar ratio m a range from about 10:1 to about 100:1 with an aqueous hydrogen fluonde solution having a concentration of hydrogen fluonde in the range of from about 0.1 to about 10 such that the mordenite containing fluonne is produced; collecting the fluonne-containing mordemte by filtration; and drying the collected fluoπne-contaimng mordenite. 13. The method of claim 12, wherein the silica to alumma molar ratio is about 50:1 or less. 14. The method of claim 12 or 13, wherein the fluonne-containmg mordenite contains fluonne in the range from about 0.1 to about 4 percent by weight. 15. The method of claim 12, 13 or 14 wherein a temperature m the range from about 80°C to about 140°C is maintained dunng the contactmg step.

Inventors: ANANTANENI PRAKASA RAO, DAI P EUGENE, KNIFTON JOHN F, ANANTANENI, PRAKASA, RAO, DAI, P., EUGENE, KNIFTON, JOHN, F.
Applicants: HUNTSMAN SPEC CHEM CORP, HUNTSMAN PETROCHEMICAL CORPORATION
Application year: 1997
Main classification: C07C15
IPC codes: B01D3, B01J29, B01J37, C01B39, C07C2, C07C15