CA1083609A - Hydroalkylation of benzene and analogs - Google Patents

Abstract

HYDROALKYLATION OF BENZENE AND ANALOGS

ABSTRACT OF THE DISCLOSURE
Mononuclear aromatic hydrocarbons, e.g. benzene and analogs, are converted by hydroalkylation to the corres-ponding cycloaklyl aromatics by contacting the mononuclear aromatic hydrocarbons in the presence of hydrogen with a catalyst comprising a rare earth-exchanged Y-type zeolite support carrying a promoter comprising at least one of ruthenium, iridium, rhodium and palladium, the catalyst being calcined in an oxygen-containing atmosphere at a temperature of 250 to 600°C prior to the hydroalkylation reaction.

Description

~ . ~

BACKGROUND OF THE INVENTION
The present invention relates to an improved process for the hydroalkylation of mononuclear aromatic hydrocarbons, namely benzene and analogs thereof, to form cycloaklylaromatics. Many patents have recently issued in the field of hydroalkylation of mononuclear aromatics. See, for example, U.S. 3,7605019, U.S. 3,784,617, U.s. 3,784,618, u.S. 3,829,514, U.S. 3,829,515, U.S. 3,829,516 and U.S.
3,829,517. In the processes disclosed in these patents, benzene or analog is contacted with a catalyst which is normally composed of a Group VIII transition metal supported .. : .
on a suitable carrier, the catalyst optionally containing tungsten. ~lany different supports are disclosed as useful including silica-alumina, zeolite and alumina. S~eci~ic C.~oup VIII transition metals disclosed to be useful are cobalt, nickel, ruthenium, rhodium, palladium, iridium~and platinum. -- '' , . . . . .
.: . ,.
~ : :
:: : '' - : , :

, . : " : :. - , ,. . ~ .. , : . ,: ' , . : . . , ~83609 ( 4~79) Although processes disclosed in the foregoing patents are caoable of effecting hydroalkylation of benzene and analogs to the corresponding cycloalkylaromatic com-pounds, they are disadvantageous in that they are unable to provide the desired cycloalkylaromatic product comoounds . , with high yields and high selectivities. ~loreover, in many processes it is necessary to sub~ect the catalyst to be used to an activation pre-treatment by reducing the catalyst with H2 prior to beginning the hydroalkylation reaction. In still other processes, it is necessary to carry out the hydroalkylation reaction in stages, the total amount of hydrogen necessary to effect hydroalkylation being added to the reaction system in stepped additions.
Accordingly, it is an ob,;ect of the present invention to provide an improved process for the catalytic hydroalkylation of benzene and analogs to the corresoonding cycloalkylaromatic compounds which produces the desired product compounds in higher yield and with higher selec-tivities than processes known prior to the present invention.
It is a further object of the present invention to provide a hydroalkylation process of the type described above which can be carried out either in batch mode or continuously in a single stage operation, i.e. a process which does not require stepped addition of reactants.
It is still another object of the present inven-tion to provide a hydroalkylation process in which the catalyst to be used can be employed directly after calcina-tion, H2 reduction of the catalyst prior to use being unnecessary.

3609 ( ~979 ) SUMMARY 0~ THE IN~ TI0~
These and other ob~ects are accomplished by the present invention in accordance with which mononuclear aromatic hydrocarbons are converted into cycloaklyl aro-matics by contacting the mononuclear aromatic hydrocarbons in the presence of hydrogen with a catalyst comprising a rare earth-exchanged Y-type zeolite support carrying a promoter comprising at least one of ruthenium, iridium, rhodium and palladium.
~ ore specifically, the present invention provides a process for the hydroalkylation of mononuclear aromatic hydrocarbons in which the mononuclear aromatic hydrocarbon together with hydrogen is contacted with a catalyst com-prising a rare earth-exchanged Y-type zeolite support carrying a ruthenium, iridium, rhodium and/or palladium promoter, the catalyst being calcined in an oxygen-contain-ing atmosphere at a temperature of 250 to 600C prior to the hydroalkylation reaction.
In a specific embodiment, the present invention provides a process for the hydroalkylation of mononuclear aromatic hydrocarbons which comprises contacting for a period of 10 minutes to 6 hours at a temperature of from room temperature to 400C hydrogen and a mononuclear aro-matic hydrocarbon selected from the group consisting of benzene and substituted benzene substituted with 1 to 4 alkyl groups each independently having 1 to 4 carbon atoms with a catalyst obtained by calcining in a molecular oxygen-containing atmosphere at a temperature of about 250 to 600C a composite comprising a rare earth-exchanged Y-type eolite support impregnated with at least one compound decomposable to yield a promoter comprising at least one of \

1~36~9 (1~979) ruthenium, iridium, rhodium and palladium, the amount of the decomposable co~.pound on the support being such that the amount of promoter on the support after calcination is between about 0.2 and l0 weight percent with the weight of the rare earth-exchanged Y-type zeolite plus the weight of the promoter being taken as 100%.
In accordance with the present invention it has been found that cycloalkylaromatics can be produced with higher yields and higher selectivities than previously known processes ~or hydroalkylation of benzene and analogs. ~or example, it has been found that cyclohexylbenzene can be obtained with per pass conversions approaching 50~ at selectivities close to 80%, which is significantly better than obtainable with the prior art processes disclosed in the above-noted patents. rnoreover, the inventive process can be accomplished in a single stage operation, i.e., without the stepped addition of reactants and hence is easier to carry out than conventional processes carried out in multiple stages. .~lso, the catalyst employed in the inventive process can be used directly after calcination without H2 reduction, and hence practice of the inventive process is easier than conventional processes requiring H2 reduction as part of the catalyst preparation.

DETAILED DESCRIPTION
Process Conditions The inventive hydroalkylation reaction is accom-plished by contacting the mononuclear aromatic hydrocarbon to be reacted with a reaction catalyst in the presence of hydrogen. The reaction can be accomplished both in batch mode and continuously with both fixed and fluid catalyst beds.
The reaction is normally carried out in single stage ~836~ ( 4979) operation, i.e., all of the reactants and the catalyst necessary for the reaction are brought together at the same time and not in stepped additions. However, the reaction can be carried out in stages if desired.
The reaction temperature is normally maintained between room temperature and 400C, preferably 100 to 300C, more preferably 150 to 250C and optionally 200C. The reaction pressure is normally maintained at 100 to 800 psig, preferably 200 to 500 psig and most preferably 300 to 400 psig. When the reaction is carried out in the batch mode, the reactants and catalysts are contacted with one another for a period of 10 minutes to 6 hours, preferably more than 1/2 to 3 hours, and optionally about 1,5 hours. A reaction time of less than 10 minutes or more than 6 hours can be used if desired although better results will be obtained if the reaction time is maintained within this range. When the process is carried out on a continuous basis, the reactant/
catalyst contact time is normally 10 seconds to 10 minutes, preferably 100 seconds to 5 minutes.
The amount of hydrogen in the reaction system is not critical, and the reaction will proceed so long as any amount of hydrogen is present. Preferably the amount of hydrogen correspond to the amount of hydrogen present when a 600 cc reactor containing 5 grams of catalyst and 2.0 moles of benzene is filled with hydrogen to the pressures indicated above. If desired, a carrier gas which is inert to the reactants, product and catalyst can be included in the reaction system.

~ 3 ~ ~ (4979) , The present invention finds wide applicability in the hydroal~ylation of all types of mononuclear aromatic hydrocarbons. Benzene (unsubstituted) and substituted benzene substituted with 1 to 4 alkyl groups each indepen-dently having 1 to 4 carbon atoms can be readily converted to the corresponding cycloalkylaromatics in accordance with the present invention. Specific examples of compounds which can be processed by the present invention include benzene, ethylbenzene, cumene (isopropyl benzene), toluene, xylene, and durene (tetramethylbenzene).
In order to recover the product compound from the reaction mixture when the reaction is completed, the liquid reaction product is separated from any unreacted hydrogen and carrier gas that may be present in the system. The liquid reaction product is then filtered to remove catalysts therefrom and the filtrate is sub~ected to distillation or other suitable separation technique to recover the product compound from unreacted starting material.

CATALYST
The catalyst employed in the inventlve process comprises a rare earth-exchanged Y-type zeolite impregnated with a small but suitable amount of a iroup VIII transition metal promoter selected from the group consisting of ruthen-ium, iridium, rhodium and palladium. Y-type zeolite is a well-known material in the art and described in detail in Chapters 18-20 of ~eier and Uytterhoeven, MOLECULAR SEIVES, American Chemical Society, ~1ashington, D.C., copyright 1973.
See also U.S. 39130,007. As well-known in the art, Y-type zeolite can be treated to accept various types of ions by impregnating the Y-type zeolite with a solution of the ions to be accepted. Such a procedure causes an exchange 83~

reaction to occur, cations in the aqueous solution being exchanged for cations originally in the zeolite. See column - 18 of U.S. 3,130,007. The catalyst support useful in the inventive process is a rare earth-exchanged Y-t~pe zeolite which is produced by exchanging rare earth ions from an aqueous solution thereof with the ions originally in Y-type zeolite. This material is well-known as pointed out in columns 7 and 8 of U.S. 3,78~,617. In the preferred embodi-ment of the invention, the rare earth-exchanged Y-type zeolite employed in Linde's SK-500 ~, which is a well-known commercially available catalyst support. Linde's SK-500 is composed of 65.0 weight percent SiO2, 22.7 weight percent A12O3, 1.6 weight percent Na2O and 10.7 weight percent various rare earth metals. Rare earth-exchanged Y-type zeolites other than Linde's SK-500 can be employed in the present invention, the specific rare earth impregnating the Y-type zeolite being unimportant. In this connection, since it is expensive to separate one rare earth from another, commercially available rare earth-exchanged Y-type zeolites are made with mixtures of different rare earths rather than a single rare earth.
In accordance with the present invention, the rare earth-exchanged Y-type zeolite employed as the catalyst additionally contains a promoter metal selected from the group consisting of ruthenium, iridium, rhodium and palladium.
The preferred promoter is ruthenium. The amount of promoter metal in the catalyst can vary between relatively broad proportions. If the amount of promoter metal is about 0.1 weight percent, no significant promoting effect will be obtained. Moreover, although amounts of promoter metal about 10% will provide effective catalysts, the cost of ;' "
,~

~83f~

using such large amounts of promoter metal is prohibitively expensive. Threfore, the amount of promoter metal in the catalyst is greater than 0.1 weight percent and usually between 0.2 and 10 weight percent based on the weight of promoter metal in the catalyst with the weight of the rare earth-exchanged Y-type zeolite plus the weight of the pro-moter metal being taken as 100 percent. Preferably the catalyst contains 0.5 to 2 weight percent promoter metal, while the most preferred amount is about one percent by weight.
In order to deposit the promoter metal on the rare earth-exchange Y-type zeolite support of the present inven-tion, any convenient technique can be employed. For example, the promoter metal in the form of a decomposable salt or other compound can be dissolved in a solvent therefore and the solution so obtained used to impregnate the rare earth-exchanged Y-type zeolite material. Chloride salts (i.e.

Ru~13~3H20, IrC13~4H20, RhC13-3H20 and PdC12) dissolved in ethanol or isopropanol as the solvent have been found especially suitable for this purpose. Any other compound (e.g. nitrates, acetates, etc.) which yield catalytically active ruthenium, rhodium, iridium or palladium when heated in the presence of oxygen under the calcining conditions discussed below can be employed in place of chloride.
Processes for depositing transition metals including ruthe-nium, iridium, rhodium and paladium,on Y-type zeolite supports are well-known as taught in U.S. 3,7~1l,617. This patent further teaches that it is well-known to deposit other types of Group VIII metals on rare earth-exchanged Y-type zeolites. Therefore, those skilled in the art should have no difficulty in producing catalysts including ruthen-ium, iridium, rhodium and/or palladium on a rare earth-exchanged Y-type zeolite as used in the present invention.

~1~83609 Once the promoter metal in chloride or other decomposable compourld form is deposited on the rare earth-exchnaged Y-type zeolite, the composite so formed is acti-vated by calcination. In accordance with the present invention, calcination is accomplished in a molecular oxygen-containing atmosphere at a temrerature of about 250 to 600C, preferably 350 to 500C, most preferably 427C.
Temperatures below 250C can be employed but activation is so slow that such temperatures are impractical. At tempera-tures above 600C, the zeolite support will begin to de compose hence reducing the catalytic activity of the catalyst produced. Calcination has the effect of expelling water from the zeolite support, which in turn causes the calcined catalyst obtained to exhibit a superior catalytic activity.
Therefore, calcination should be carried out for a time sufficient to drive off water from the zeolite support and hence improve the catalytic activity of the catalyst ob-tained. Those skilled in the art can determine the optimum calcination time by simple routine experimentation. In this connection, it has been found that at the preferred calcina-tion temperature of 427C, the calcination time is approx-imately two hours, whereas at the maximum calcination temperature of 600C calcination should last no more than about eight hours while at the minimum calcination tempera-ture of 250C calcination should be accomplished for at least about 24 hours.
Once the promoter metal-containing zeolite com-posite of the present invention has been sub~ected to calcina-tion,i~ can be directly used as the catalyst to effect the hydroalkylation reaction, reduction with hydrogen gas being unnecessary.

_g_ ~1~836~9 ~ .s indicated above, the products of the inventive process, namely cycloalkylaromatic hydrocarbons, are pro-duced in accordance with the present invention with high per pass conversions and high selectivities. mhus the present invention marks a significant advance over prior art pro-cesses since it is possible to produce more end product with a given amount of feed. rloreover~ with superior select-ivities, recycle requirements are reduced, thereby decreasing energy costs. Also, because hydrogen reduction of the catalyst prior to use is unnecessary, and because the inventive process can be carried out in single stage opera-tion the inventive process is simpler to accomplish than many analogous prior art processes.
The end products of the inventive process, namely cycloalkylaromatic hydrocarbons, have many significant uses.
For example, these compounds can be converted to phenol and/or cyclohexanone in the case of benzene and analogous products in the case of benzene analogs, which compounds have known utilities.
Working Examples --In order to more thoroughly illustrate the present invention, the following working examples are presented. In these examples "% ppc" reans percent per pass conversion and is defined as % _ moles carbon in reactant converted to product x lOC
ppc moles carbon in reactant fed (4979) 1~3 6 Example 1 Q.13 gra~. IrC13 4~ as dissolved in 200 cc distilled water to form a green solution. 9. 9 grams I.inde's SK-500 (<50 mesh powder) was added, and the water was e~1ap~
orated from the composition so obtained to form a light brown paste which was dried overnight at 110C to form an essentially white material. This material was then calcined in air at 427C for 2 1~ hours to produce a grayish-white catalyst containing 1~ Ir and 99% SK-500.
5 grams of the catalyst so obtained were charged into a 600 cc PA~P autoclave. 156.22 grams ( 2.0 moles) benzene was also fed into the reactor. The autoclave was then pressurized with hydrogen to a pressure 400 psig. The reaction progressed for approximately 35 minutes over which time the pressure in the reactor decreased from 400 to 180 psig and the reaction temperature increased from an initial value of 22C to 185~. After the 35 minute reaction period, the reaction product was recovered from the reactor and subjected to analysis by gas chromotography. The follow-ing results were obtained:
~pp c cyclohexane 8.36 bicyclohexane0.10 cyclohexylbenzene 43.94 dicyclohexylbenzene 0. 52 unreacted benzene 47.09 selectivity 83.oo (4979) ~83~
Example 2The procedure of Example l was repeated except that catalyst employed was com osed of l" Rh and 99i SK-500.
This catalyst was prepared in the same way as the catalyst employed in Example l except that 0.256 grams RhCl3~3H2o was employed rather than 0.193 ~rams IrCl3~4H20. Also, in Example 2, the reaction time was l '-~ hours rather than '~
hour. The following results were obtained:
~ ~pc cyclohexane32.51 bicyclohexanel.~,0 cyclohexylbenzene 35.78 dicyclohexylbenzene 0.52 unreacted benzene ll.40 selectivity 40.4 Example 3 Example 2 was repeated except th~t the catalyst employed contained 1% Pd and 99% SK-500. The catalyst of Example 3 was prepared as the catalyst of Example l was prepared except that 0.167 grams PdCl2 was employed. lhe following results were obtained:
, ppc cyclohexanelO.74 bicyclohexaneO.lO
cyclohexylbenzene 50.44 dicyclohexylbenzene 4.43 unreacted benzene 33.46 selectivity75.80 ~`

. -12 (4979) 1~8360~
Exam~le 4 -U. S. Patent 3,7849617 to Suggitt discloses a process for the catal~tic hydroalkylation of mononuclear hydrocarbons in which the catalyst may be ruthenium sup-ported on NH4-exchanged Y-zeolite. ~his Example 4 as well as the following Comparative Exam~les A, B and C are presented to show the improved results realized in accord-ance with the present invention when the catalyst is com-posed of ruthenium supported on rare earth-exchanged Y-zeolite.
1.056 grams RuC13 3H20 was dissolved in 200 cc of isopropanol to form a red-brown solutlon. 39.6 grams Linde's SK-500 was added to this red-brown solution, and the solvent was then evaporated with constant stirring at low heat. The green paste formed thereby was dried overnight at 110C in an oven to produce a gray powder. A portion of this gray powder was calcined at 427C for 2 hours in the presence of air to provide the Example 4 catalyst having 1,~
Ru and 99% SK-500.
Hydroalkylation of benzene was carried out in the same way as in Example 1 except that the reaction pressure was maintained at about 300 psig and the reaction tempera-ture was maintained at about 200C. Also, a portion of the liquid reaction medium was withdrawn at '~ hour intervals and the composition of each withdrawn portion determined. The following results were obtained:

108360~

~ . :
.~ ~:.
.,, . . . "
~, o ." ~ ~9 ) I` I`
U~ . :
, U~
,~ ~ `' ~o ~ ~ ~
X . ~ N . . ~ O
' ~ ~ ~ ~ ~ O ~:
S-l (I) O;) ~ d' ~
~ m o P
4~
:~ .
04~J N ~~;r :
P:~ I` o C~. . . :~
.~O ~ 1~
.,:
S~ O .~, :-.~ ~ ~ I~ t~
~ ~ ~ " O ,.'. , o~o O ~ ~i .~ ~1 ~ ~r .~ . Z ~ ~r . , :, , U P~ ~ ~ '. -,~ ,.
o o o o o ~i o m O
.1 K zic5~Lr~
u~ ~C ~ o o\O , ~ o ~
a~ :, -.
~ :
o~O _~ ~1 .~ .
. I O
a) u~ ,~
~ s~ O ~ .
.. ,~ ~~ O ~ .
E~ ~ ~1 ~1 0 ,. :
~Q ~ ~ ~ ~::
~ ~1 f~ ~ ~ trl i ~
0 ~ rl .
i ~1 :: ~

:

1~8360~

Comparative Example A
Example 4 was repeated except that the catalyst employed was composed of 1~ Ru and 99% NH4-exchanged Y-zeolite which was calcined at 427C for 2 hours. The following results were obtained:

:
~836~)g .~ ".
~ In ~ ~ ~ `,'~:
U~ ~
,~ C) ,~ ~ ~ ~ ,.
~ 0~ 0~ 1~ ~D '.
o ,, $ ~
U~ , :~
o a~
C) ~ ~ ~ ~ I~
O c~ a)~r ~ I~ :
1~ (~ N . . . , t~ O ~ ~D 1~ ~ ~1 ~ m s~ ;,,:

u ,~ o ~r o ~1 ~1 n ~ ~r 1~ cO

,0 m ,~ m ~ ~ O o ~r o o ~;

~ .~ ~ u~ Ln ~ o ~ ~ ~
~1 ~ C) o O O o ~ ~ i:q ?

., o ~ ~; ~ ~ 00 C~ ~ $ r- o c X ~
, ~ ~, ~r m a) z ~ :, 0~O ~ ~
.
I o O h ~1 ~`I o ~
~1 ~ ~ ~ O f~ :
E~
IY; ,1 ~1 ~ S~
o'~O
.

..

~ .
O
Z

E~ -:
~i ~ ~ ~ ~
a) (4979) ~83~)9 Comparative Example B
A portion Or the gray powder produced during catalyst preparation in Example Ll was prepared for use in accordance with the technique disclosed in U. S. Patent 3,829,517. Namely, the gray powder was calclned at 800C
for 2 hours in the presence of air ancl then reduced with H~
at 480C at atmospheric pressure for 2 hours. Example 4 was then repeated using this catalyst. The following results were obtained:

, :

p .~ Ln ~ ~ ~ :
o ~ o l` ~
~ ~ ~ oo oo :~ :
u~
~ :
a) tl) Ul ~ ~9 ~1 -~
o a~ cO r- c~ ~9 U~IT~ N
~ h o ~:5~ O 0~ 00 1 O o ~m O X ~

~ s~ ~.
o m ~ ~ ~ ~ ~ I
~1 C~ ~ ~ N ~D
~) ~ . . .
o ~ o O ~ ~
,1 0~ t) ~r m ~ m ~ ~ , ~~ ~ 0\o ~
,~ C~ ~, ~ O O
4O ~ r-l ~1 ~ N
~~X
~q r~.,, o ~ ~ a) ~ a) ' !~~ x c~
I O C) O
~ K m O~ ~ Z ~D ~ O CO
C~~ ~ ~ n ~ ~ r~ , E~ ~
o o ~ ~
~ o ~ :`
u~

:
l o ra O ~ ~ .
r d O E~ ~ ~ N
~ ~ ~ S~
rl ~_ ~1 t~
.
: "~ .
O '' Z;

.~
s~ m m m m ~C
; ~ ~:

1~9831~

Comparative Example 5 Example 4 was repeated except that the catalyst employed was composed of 1% Ru and 99~ NHLI-exchanged Y-zeolite, the catalyst having been calc:ined at 800C for 2 hours in the presence of air and thereafter reduced at 480C
in the presence of H2 for 2 hours in accordance with the technique taught in U. S. Patent 3,829,517. The following results were obtained:

3609 ~
.

, P ".~

~ ~r ~ o ~
U
a) ~ 1- ~ ~
:.
~q :~
C~ :`::
o :
CO
.,. ~ ~ oo c) a~ ~9 ~ ~ ~
td N : :
~Q ~ ~ . ~ ~D
s~ ~ a) .,, ~ ~m V m ~ :
o ~
s~ m o m ,~ ~ C~ U~ ~ O O :
~1 . . . . --o a~
u~
Q ~:q ~ 1` ~ ~1 1:~1 ~ ~ ';~
~ ~ a~ 0~o ~ ~ ~ o~ In ~! ~ ~1 ~ ~ ,~
X Z [`I`
:~ ~ I ~ ~mq ~ N
H d'~ t) O O O O
~j Z; E~ m ~ .
,. ~ 0O~ ,.
o Ul Z; O
~ ~ ~1 ~C
m ,~ o C~ ~ Ln 1` C~ S
~ m ~ .
0~O ~
~ ~.
o .. 4~ ~d ~1 C~
~, O . I o O
O ~ 5~ o ~
o ~ . .
E~ ~ ~ U
~1 ~ 5 _ s~
.,, ~ ~:
td~
H
:' Z
:

~ ~1 :` ~
X
~: ' ' ,.~ .
~;

(4979) 36~9 Comparative Example D
U. S. Patent 3,829,517 to Zuech discloses a catalytic hydroalkylation process employing a ruthenium halide-active clay catalyst which has not been heated under calcination conditions prior to use. This Comparative Example D as well as the following Comparative Examples E
and F are presented to show the superiority of the inventive process as illustrated in Example 4 with respect to the process shown in U. S. 3,829,517.
o.7895 grams RuC13 3H20 was dissolved in 200 cc ethanol to produce a dark red-brown solution. 29.7 grams Filtrol Grade-71 powder was suspended in the solution and impregnated at low heat with constant stirring. The solvent was then removed and the wet powder obtained dried in an oven at 110C for 3 hours to produce a gray powder. A
portion of the gray powder was calcined at 427C in the presence of air for 2 hours in the manner of Example 4 to yield a catalyst containing 1% Ru and 99% Filtrol Grade-71, which was employed as the catalyst in Comparative Example D.
Example 4 was repeated using as the catalyst the catalyst obtained above. The following results were obtained:

~ !

1(~836(~

u7 ~ ~ a~
~D ~ ~ U) a) o~ 00 a) , ~, ~
U~
~r a) a ~ ~ o ~r U~ ~, ~ ~ ~ o (1~ N
:1 a~ ~ O 1 o ~ a~ ~ ,~
m ~ m ::~
s~ :
o m O
P:l s~ o .,~ ~,1 O O ~1 a ~ o ~ 0~ ~ ~ ~
a ~ ~ ~
co a~ ~ ~1 .,1 ~ ~ ~ :.
u ~q a~

m C~ ~ . .
~ a) ,~ ~ o o E~ ~ ~ ~ ,.

~ ~ æ ~ O ~ ~, o o ~ O ~ O ~
c~ s~ m C) .~
0~O ~ .
~ ~ .
a~ ~ .
~ ~ C) I o O ~ .
~ O n~ ~ ~
o~ ~ ~ ~ c) ~1 ~ ~ \ ~ :
'1.
..
u~ ~ ~1 '.

., t~ O
æ
~:
. ~ ~ ~ ~ ~P
~: ~ a a a a , X
:. :
:.

~3609( 4979) Comparative Example ~
Example 4 was repeated using as the catalyst a portion of the gray powder produced during catalyst prepara-tion in Comparative Example D. It will be noted that this catalyst was composed of 1~ Ru and 99% SK-500 and was not calcined prior to use. The following results were obtained:

.

:

83~9 .~
~1 ~ ~D CO
C~ ~ ~ ~`
I~
~n ..
~ ~ `,.
O (U ~X) Il ) N 00 (d N ~0 N
~ a p m a~

m ,~ N O
m rl ~) C) ~1 O O O :`
..

1 ~4 t`
O P~
P O O O ~--1 1~ N N
~ Il~ ~ ~I r-l ~
~ , ~ ~ .', 1~1 U~ o\O ~.
~ O~o x a) :,., ~ ~ X O O O

C~ ~ Z O ~ CO CO
X ~ ~) t~
o ~ r~
~q ~ .

U~ I ~O) a ~ O
rl N O t~
E~ ~ ~ N ~ :
.,1 ~1 ~1 ~ ~ ' _. ~ S ~
a) ~ .
,~
.
~ O , : Z :
O ' ':

a) r I N ~) 'r ., ~1 :: ~
Q~
' X
.

_ 24 --.

~1~8361~9 Comparative ~xample ~
Comparative Example D was repeated except that the catalyst was not calcined prior to use. It will thus be appreciated that the catalyst employed in this co~parative example was composed of 1~ Ru and 997 Filtrol ~rade-71, the catalyst bein~ uncalcined as taught in U. S. 3,829,517. mhe followlng results were obtained:

'~,':,, 1~3~

rl .,. CO CO
~, o ~ ~
~ I~ 0~ 00 1 U~

a ,~
aJ ~ ~ 1~ ~r ~
s~ a) ~ , 00 ,0 p m 'u :
m O O O O
o ~
~` ~ ::
:~:
o ~r ' s~ m ~ O
m ~ o o O ~ ~ ~

H o\ q O O O O
~ ~ m ~ Z
C_) P:; X N t~l ~ ~
0~ m O O O O
..
..
:
~1 ~ .
,. ~ tn I O
,.
o ~
\ ~ O 0 rl .. ~ ~
;', ~ rl .; .
~: ~o;

~:
,1 ~I N ~) ~
: ~ ~
'

Claims (14)

WE CLAIM:

1. A process for the hydroalkylation of mono-nuclear aromatic hydrocarbons comprising contacting a mononuclear aromatic hydrocarbon and hydrogen with a catal-yst comprising a rare earth-exchanged Y-type zeolite support carrying a promoter comprising at least one of ruthenium, iridium, rhodium and palladium, said catalyst having been calcined in a molecular oxygen-containing atmosphere at a temperature of about 250° to 600°C prior to use.

2. The process of claim 1 wherein calcination is accomplished for a time sufficient to activate said zeolite support.

3. The process of claim 1 wherein said mono-nuclear aromatic hydrocarbon is selected from the group consisting of benzene and substituted benzene substituted with 1 to 4 alkyl groups each independently having 1 to 4 carbon atoms.

4. The process of claim 3 wherein said mono-nuclear aromatic compound is benzene.

5. The process of claim 3 wherein said catalyst contains greater than about 0.1 weight percent promoter with the weight of said rare earth-exchanged Y-type zeolite plus the weight of said promoter being taken as 100%.

6. The process of claim 5 wherein said catalyst contains 0.2 to 10 weight percent promoter.

7. The process of claim 5 wherein said mono-nuclear aromatic compound is contacted with said catalyst at a temperature between room temperature and about 400°C.

8. The process of claim 7 wherein said process is carried out in the batch mode, said mononuclear aromatic hydrocarbon and hydrogen contacting said catalyst for a period of about 10 minutes to about 6 hours.

9. The process of claim 8 wherein said mono-nuclear aromatic hydrocarbon and said hydrogen contact said catalyst for a period of more than ? to three hours.

10. The process of claim 8 wherein said promoter is ruthenium.

11. The process of claim 10 wherein said mono-nuclear aromatic compound is benzene.

12. A process for the hydroalkylation of mono-nuclear aromatic hydrocarbons comprising contacting for a period of 10 minutes to 6 hours at a temperature of from room temperature to 400°C hydrogen and a mononuclear aro-matic hydrocarbon selected from the group consisting of benzene and substituted benzene substituted with 1 to 4 alkyl group each independently having 1 to 4 carbon atoms with a catalyst obtained by calcining in a molecular oxygen-containing atmosphere at a temperature of about 250° to 600°C a composite comprising a rare earth-exchanged Y-type zeolite support and at least one compound containing a promoter comprising at least one of ruthenium, iridium, rhodium and palladium, the amount of said compound on said support being such that the amount of promoter on said support after calcination is between about 0.2 and 10 weight percent with the weight of said rare earth-exchanged Y-type zeolite plus the weight of said promoter being taken as 100%.

13. The process of claim 12 wherein said promoter metal is ruthenium.

14. The process of claim 13 wherein said mono-nuclear aromatic hydrocarbon is benzene.