FORM 2
THE PATENTS ACT 1970
[39 OF 1970]
&
THE PATENTS RULES, 2003
COMPLETE SPECIFICATION
[see section 10 and rule13]
“INTEGRAGED ALKYLATION AND TRANS ALKYLATION PROCESS”
Name and address of the applicant:
RELIANCE INDUSTRIES LIMITED
3rd Floor, Maker Chamber-IV, 222, Nariman Point, Mumbai – 400 021, Maharashtra, India
Nationality: Indian
The following specification particularly describes the invention and the manner in which it is to be performed.

TECHNICAL FIELD
The present disclosure relates to organic chemistry in general. Particularly, the present disclosure relates to integrated alkylation and transalkyation process for manufacturing/preparing light alkyl aromatic compound in the presence of an ionic liquid compound catalyst. In an embodiment, the ionic liquid compound catalyst for the said integrated alkylation and transalkylation process is prepared by reacting metal hydroxides and metal halides. The present disclosure further relates to a system for carrying out the said integrated alkylation and transalkylation process in the presence of the ionic liquid compound.
BACKGROUND AND PRIOR ARTS OF THE DISCLOSURE
Alkylation of benzene produces linear alkyl benzenes that may find various commercial uses. The linear alkyl benzenes are very important raw material for the manufacture of detergents. Surfactants which are used in the production of detergents are produced by sulfonation of linear alkyl benzenes. In the alkylation process benzene is reacted with an olefin to produce linear alkyl benzene. The alkylation conditions comprise the presence of homogeneous or heterogeneous alkylation catalyst such as aluminium chloride, boron trifluoride, sulfuric acid, hydrofluoric acid, phosphoric acid and zeolitic catalysts at elevated temperature.
However, majority of the commercial plants for such alkylation reactions use hydrogen fluoride (HF) as an acid catalyst. However, HF based process does provide operational concerns in terms of safety, toxicity, volatility, corrosiveness, waste disposal and troublesome acid recovery and troublesome purification. Solid acid catalysts such as UOP Detal have been developed recently to replace HF. But these known solid acid catalyst and liquid catalyst known in the prior art cannot be retrofitted in the HF based technology manufacturing plants.
Further, during the alkylation process various side reactions take place leading to the formation of dialkylaromatics, oligomers of olefins considered as heavier aromatic compound, which have low commercial value than the lighter alkyl aromatics. However, use of excess reactant will help in minimizing the heavier compounds, but cannot be eliminated Therefore, the catalyst known in the prior art are not selective, thereby leading to the formation of heavier compounds which have least commercial value. Also, the

catalyst reported so far have certain disadvantages such as higher operating conditions, catalyst instability with feed stock and higher regeneration cost, thereby making the process uneconomical.
Therefore, there is a need to overcome the limitations and the description provided herein aims at overcoming such limitation.
SUMMARY OF THE DISCLOSURE
Accordingly, the present disclosure relates to an integrated alkylation and transalkylation process to obtain light aromatic compound, said process comprising steps of:
a) contacting aromatic hydrocarbon or paraffin with olefin in presence of
ionic liquid compound of formula I- [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o
(solvent)]
wherein,
M1, M2 & M3 are independently metals selected from a group comprising
Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any
combination thereof,
X & Y are halides,
'p' represents 0 to 5
'q' represents 0 to 5
'r' represents 0 to 5
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,
OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene,
toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and
ethylene dichloride, or any combination thereof,
to obtain the light alkyl aromatic compound and heavy aromatic
compound;

b) contacting the heavy aromatic compound of step a) with alkyl aromatic compound in presence of ionic liquid compound of formula I-[(M1)p(M2)q(M3)r (OH)m(X)n(Y)o (solvent)]
wherein,
M1, M2 & M3 are metals independently selected from a group
comprising Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and
Hg, or any combination thereof,
X & Y are halides,
p represents 0 to 5
q represents 0 to 5
r represents 0 to 5
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,
OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene,
toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and
ethylene dichloride, or any combination thereof,
to obtain the light alkyl aromatic compound.
In another embodiment, the present disclosure relates to a system for an integrated alkylation and transalkylation process as mentioned above to obtain light alkyl aromatic compound, said system comprising:
a) at least one mixer adapted to independently receive substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, paraffin, olefin and ionic liquid compound of formula I and wherein the mixer is adapted to convert the substituted aromatic hydrocarbon or unsubstituted aromatic hydrocarbon or paraffin or heavy aromatic compound to the light alkyl aromatic compound in presence of ionic liquid compound of formula I, olefin and alkyl aromatic compound;

b) at least one settler unit fluidly connected to at least one mixer, wherein the settler unit is adapted to receive at least one of the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon the paraffin, the olefin and the ionic liquid compound of formula I, the light alkyl aromatic compound, the alkyl aromatic compound and the heavy aromatic compound from the mixer, and wherein the settler unit is adapted to cause settling of at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the olefin, the alkyl aromatic compound and the paraffin;
c) at least one purifier fluidly connected to at least one of the settler unit, the purifier is adapted to receive at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the olefin, the substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, the paraffin, the olefin, the heavy aromatic compound, the alkyl aromatic compound and alkali solution and wherein the purifier is adapted to purify the light alkyl aromatic compound;
d) at least one fractionating column adapted to receive at least one of the light alkyl aromatic compound, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin, the olefin and the ionic liquid compound of formula I from at least one settler unit and wherein the fractionating column is adapted to separate at least one of the light alkyl aromatic compound, the heavy aromatic compound, the unsubstituted aromatic hydrocarbon, the alkyl aromatic compound, the ionic liquid compound of formula I and the paraffin; and
e) at least one catalyst recovery unit adapted to receive at least one of the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin the alkyl aromatic compound and the light alkyl aromatic compound, independently from at least one of the settler unit and at least one of the fractionating column and wherein the catalyst recovery unit is adapt to regenerate the ionic liquid compound of formula I.

BRIEF DESCRIPTION OF THE ACCOMPANYING FIGURE
In order that the disclosure may be readily understood and put into practical effect, reference will now be made to the exemplary embodiment as illustrated with reference to the accompanying figure. The figure incorporated herein forms part of the specification, and serves to further illustrate the embodiments and explain various principles and advantages, in accordance with the present disclosure:
Figure 1 represents a system of the present disclosure employed for carrying out integrated alkylation and trans-alkylation process of the present disclosure.
DETAILED DESCRIPTION
The present disclosure relates to an integrated alkylation and transalkylation process to obtain light aromatic compound, said process comprising steps of:
a) contacting aromatic hydrocarbon or paraffin with olefin in presence of
ionic liquid compound of formula I- [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o
(solvent)]
wherein,
M1, M2 & M3 are metals independently selected from a group comprising
Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg or any
combination thereof,
X & Y are halides,
p represents 0 to 5,
q represents 0 to 5,
r represents 0 to 5,
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,
OH is hydroxyl group,

the solvent is at least one selected from a group comprising benzene, toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and ethylene dichloride, or any combination thereof, to obtain the light alkyl aromatic compound and heavy aromatic compound;
b) contacting the heavy aromatic compound of step a) with alkyl aromatic compound in presence of ionic liquid compound of formula I-[(M1)p(M2)q(M3)r (OH)m(X)n(Y)o (solvent)]
wherein,
M1, M2 & M3 are metals independently selected from a group comprising
Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any
combination thereof,
X & Y are halides,
p represents 0 to 5,
q represents 0 to 5,
r represents 0 to 5,
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,
OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene,
toluene, xylene, chlorobenzene, bromobenzene, hexa methyl benzene and
ethylene dichloride, or any combination thereof, to obtain the light alkyl
aromatic compound.
In an embodiment, the ionic liquid compound of formula-I is prepared by mixing metal hydroxides and metal halides in the presence of an aromatic solvent.
In another embodiment, the metal hydroxide is selected from a group comprising hydroxides of S-block metals, hydroxides of P-block metals and hydroxides of transition metals, or any combination thereof.

In an exemplary embodiment, the metal of the metal hydroxide is selected from a group comprising Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any combination thereof.
In another embodiment, the metal halide is selected from a group comprising transition metal halides and P-block metal halides or any combination thereof.
In an exemplary embodiment, the metal of the metal halide is selected from a group comprising Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any combination thereof.
In another exemplary embodiment, the halogen of the halide is at least one selected from a group comprising chlorine, bromine, fluorine, and iodine, or any combination thereof.
In another embodiment, the solvent is selected from a group comprising benzene, toluene, xylene, chlorobenzene, bromobenzene, hexa methyl benzene and ethylene dichloride, or any combination thereof.
In an embodiment, the weight percentage of solvent in the ionic liquid compound of formula I ranges from about 10% to 60%.
In a preferred embodiment, the weight percentage of solvent in the ionic liquid compound of formula I ranges from about 20% to 60% by wt.
In a further embodiment, in the integrated alkylation and transalkylation process, the step a) is alkylation and the step b) is transalkylation.
In another embodiment, the aromatic hydrocarbon is selected from a group comprising substituted and unsubstituted aromatic hydrocarbon, or a combination thereof; wherein the unsubstituted aromatic hydrocarbon is benzene and the substituted hydrocarbon is selected from a group comprising toluene, ethylbenzene, xylenes, cumene, wherein, the paraffin having carbon atoms about 2 to 50 is selected from a group comprising straight chain or isomers of butane, pentane, hexane, heptane, octane, nonane, decane, undecane, dodecane, tridecane, tetradecane or combinations thereof; wherein the olefin having carbon atoms about 2 to 50 is selected from a group comprising straight chain or isomers

of butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, tridecene, tetradecene or combinations thereof; wherein the heavy aromatic compound is selected from a group comprising isomers of dimethyl benzene, trimethyl benzene, diethyl benzene, triethyl benzene, dibutyl benzene, dipentyl benzene, diheptyl benzene, dioctyl benzene, didecyl benzene, didodecyl benzene, diundecyl benzene, ditridecyl benzene, ditetradecyl benzene or combinations thereof; the alkyl aromatic compound is selected from a group comprising decyl benzene, undecyl benzene, dodecyl benzene, tridecyl benzene, tetradecyl benzene or combinations thereof and the light aromatic compound is selected from a group comprising isomers of methyl benzene, ethyl benzene, propyl benzene, butyl benzene, pentyl enzene, hexyl benzene, heptyl benzene or combinations thereof.
In a further embodiment, molar ratio of the aromatic hydrocarbon or paraffin to olefin ranges from about 2:1 to 20:1.
In a still further embodiment, the molar ratio of the alkyl substituted aromatic hydrocarbon to heavy alkyl aromatic compound ranges from about 1:1 to 20:1, preferably about 2:1 to 8:1.
In another embodiment, volume ratio of the ionic liquid compound of formula I to the aromatic hydrocarbon or the paraffin and the olefin ranges from about 0.001 to 1.5 and wherein volume ratio of the ionic liquid compound of formula I to the alkyl substituted aromatic hydrocarbon and heavy alkyl aromatic compound ranges from about 0.01 to 1.5.
In a non-limiting embodiment, the ionic liquid compound of formula I is Al4(OH)3Cl9C6H6.
In a non-limiting embodiment, the Al4(OH)3Cl9C6H6 is a mixture of Al(OH)3 (metal hydroxide) and AlCl3 (metal halide) in presence of benzene (solvent). The mole ratio of metal hydroxide to metal halide is about 1:3 with about 40% to 50% of benzene by weight.
In an embodiment, the contacting of the step a) of the integrated alkylation and transalkylation process is at a temperature ranging from about 5oC to 150oC, preferably

ranging from about 10oC to 100oC, and at a pressure of about 50 atmosphere, preferably at a pressure of about 10 atmosphere.
In an embodiment, the contacting of the step b) of the integrated alkylation and transalkylation process is at a temperature ranging from about 5oC to 170oC, preferably ranging from about 50oC to 150oC, and at a pressure ranging from about 1 atmosphere to 50 atmosphere, preferably 1 atmosphere to 10 atmosphere.
In another embodiment, in the integrated alkylation and transalkylation process, the step
a) and the step b) independently further comprises deacidification of the light alkyl
aromatic compound by method selected from a group comprising washing with alkali
solution, centrifugation, alumina treatment and acid stripping, or any combination
thereof.
In a further embodiment, the deacidification of the light alkyl aromatic compound is carried out by washing the light alkyl aromatic compound with the alkali solution having about 2% to 50% concentration of alkali in the solution, wherein the alkali is selected from a group comprising sodium hydroxide, potassium hydroxide and calcium hydroxide, or any combination thereof, and wherein the volume ratio of the alkali solution to the light alkyl aromatic compound ranges from about 0.2 to 1.
In another embodiment, in the integrated alkylation and transalkylation process, conversion of the olefin in the step a) ranges from about 99% to 99.7%
In another embodiment, in the integrated alkylation and transalkylation process, conversion of the heavy alkyl aromatic compound to the light aromatic compound in step
b) ranges from about 40% to 80%.
In a further embodiment in the integrated alkylation and transalkylation process of the present disclosure, during transalkylation, there is higher selectivity of heavy aromatic compound, thereby leading to higher conversion of heavy aromatic compound to lighter aromatic compound, having conversion rate of about 40% to 80% when compared to known methods in the art.

In an independent embodiment, the present disclosure also relates to a system for an integrated alkylation and transalkylation process as described above to obtain light alkyl aromatic compound, said system comprising:
a) at least one mixer adapted to independently receive substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, paraffin, olefin and ionic liquid compound of formula I and wherein the mixer is adapted to convert the substituted aromatic hydrocarbon or unsubstituted aromatic hydrocarbon or paraffin or heavy aromatic compound to the light alkyl aromatic compound in presence of ionic liquid compound of formula I, olefin and alkyl aromatic compound;
b) at least one settler unit fluidly connected to at least one mixer, wherein the settler unit is adapted to receive at least one of the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon the paraffin, the olefin and the ionic liquid compound of formula I, the light alkyl aromatic compound, the alkyl aromatic compound and the heavy aromatic compound from the mixer, and wherein the settler unit is adapted to cause settling of at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the olefin, the alkyl aromatic compound and the paraffin;
c) at least one purifier fluidly connected to at least one of the settler unit, the purifier is adapted to receive at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the olefin, the substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, the paraffin, the olefin, the heavy aromatic compound, the alkyl aromatic compound and alkali solution and wherein the purifier is adapted to purify the light alkyl aromatic compound;
d) at least one fractionating column adapted to receive at least one of the light alkyl aromatic compound, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin, the olefin and the ionic liquid compound of formula I from at least one settler unit and wherein the fractionating column is adapted to separate at least one of the light alkyl aromatic compound, the heavy aromatic compound, the unsubstituted aromatic hydrocarbon, the alkyl

aromatic compound, the ionic liquid compound of formula I and the paraffin; and e) at least one catalyst recovery unit adapted to receive at least one of the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin the alkyl aromatic compound and the light alkyl aromatic compound, independently from at least one of the settler unit and at least one of the fractionating column and wherein the catalyst recovery unit is adapt to regenerate the ionic liquid compound of formula I.
In a further embodiment, the mixer is selected from a group comprising stirred vessel, plug flow reactor, static mixer, jet mixer and pump mixer, or any combination thereof.
In a still further, the settler unit is selected from a group comprising gravity settling vessel and decanter, and wherein the settler unit is arranged horizontally or vertically comprising series of settlers arranged inside the settler unit either horizontally or vertically, or a combination thereof.
In another embodiment, the purifier is selected from a group comprising stirred vessel, centrifuge separator, column packed with alumina, evaporation and stripper, or any combination thereof.
In yet another embodiment, the mixer is at a temperature ranging from about 5oC to about 170oC and at a pressure ranging from about 1 atmosphere to 50 atmospheres.
In a further embodiment, the conversion of heavy alkyl aromatic compound ranges from about 40% to 80%.
The present disclosure relates to an integrated alkylation and trans-alkylation process for the production of light alkyl aromatic compound, using salt such as liquid salt including but not limiting to ionic liquid compound. .
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, there is alkylation of aromatic hydrocarbon or paraffin having carbon atom of

about 2 to 50 with olefin to yield light alkyl aromatic compound alongside heavy aromatic compound.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the aromatic compound during alkylation includes but is not limited to unsubstituted aromatic hydrocarbons and substituted aromatic compound, wherein the unsubstituted aromatic hydrocarbon isobenzene, and the substituted aromatic compound is selected from a group comprising toluene, ethylbenzene, xylene, cumene.
In an embodiment, in the integrated alkylation and trans-alkylation process the light aromatic compound is linear alkyl aromatic compound selected from a group comprising methyl benzene, ethyl benzene, propyl benzene, butyl benzene, pentyl enzene, hexyl benzene, heptyl benzene, octyl benzene, decyl benzene, undecyl benzene, dodecyl benzene, tridecyl benzene, tetradecyl benzene or combinations thereof.
In a further embodiment, the linear alkyl aromatic compound is linear alkyl benzene selected from a group comprising decyl benzene, undecyl benzene, dodecyl benzene, tridecyl benzene, tetradecyl benzene or combinations thereof.
In another embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the alkylation relates to producing light alkyl aromatic compound along with heavy alkyl aromatic compound with olefin having carbon atoms of about 2 to50, optionally along with paraffin in an alkylation reactor in the presence of liquid salt including but not limiting to ionic liquid compound.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, alkylation comprises acts of contacting aromatic hydrocarbon or paraffin with olefin in the presence of catalyst such as ionic liquid compound to obtain light alkyl aromatic compound alongside heavy aromatic compound.
In an embodiment, the ionic liquid compound is a recyclable catalyst in the alkylation reaction of the integrated alkylation and transalkylation process of the present disclosure, thereby the ionic liquid compound employed during alkylation is either fresh ionic liquid

compound or recycled ionic liquid compound or partly recycled ionic liquid compound or combination thereof.
In yet another embodiment, the catalyst such as ionic liquid compound used in the alkylation reaction of the integrated alkylation and transalkylation process is a strong lewis acid based ionic liquid compound.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, during alkylation, the catalyst such as ionic liquid is provided as a stream.
In an embodiment of the present disclosure, the ionic liquid compound used in the alkylation reaction of the integrated alkylation and transalkylation process of the present
disclosure is an ionic liquid compound of Formula I- [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o
(solvent)] wherein,
M1, M2 & M3 are metals independently selected from a group comprising Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any combination thereof,
X & Y are halides, p represents 0 to 5, q represents 0 to 5, r represents 0 to 5, ‘m’ represents 0 to 20, ‘n’ represents 0 to 20, ‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other, respectively, X=Y or X≠Y, OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene, toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and ethylene dichloride, or any combination thereof.
In a specific embodiment the ionic liquid compound is Al4(OH)3Cl9C6H6.

In a related embodiment, the ionic liquid compound Al4(OH)3Cl9C6H6 is a mixture of Al(OH)3 and AlCl3 in presence of benzene.
In a further embodiment, the mole ratio of metal hydroxide to metal halide is about 1:3 with about 40% to 50% benzene by weight.
In an alternate embodiment, the ionic liquid compound, Al4(OH)3Cl9C6H6 is employed for the alkylation of iso paraffins having carbon atom about 2 to 50 with olefins having carbon atom about 2 to 50.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the alkylation is carried out at a temperature ranging from about 5oC to 150oC. In an alternate embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the alkylation is carried out at a temperature ranging from about 10oC to 100oC
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the alkylation is carried out at pressure ranging from about 5 atmospheres to 50 atmospheres. In an alternate embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the alkylation is carried out at pressure of about 10 atmospheres.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, alkylation involves steps including but not limiting to alkylation reaction, catalyst separation, recycling of catalyst, light alkyl aromatic compound phase separation from catalyst, light alkyl aromatic compound purification optionally along with at least one of neutralization, centrifugation, water wash, deacidification using alumina treater, recycling of unconverted aromatics by methods including but not limiting to specific mixing, phase separation, decantation, centrifugation, washing, purification, distillation during the reaction at regular intervals, distillation of light aromatic compound and distillation of catalyst.

In a related embodiment, post the alkylation reaction in the integrated alkylation and transalkylation process of the present disclosure, deacidification of the light alkyl aromatic compound is carried out to separate the alkylated product.
In a further embodiment, post the alkylation reaction in the integrated alkylation and transalkylation process of the present disclosure, deacidification is carried out using techniques including but not limited to treatment with aqueous solution such as alkali solution selected from a group comprising sodium hydroxide, calcium hydroxide and potassium hydroxide, or any combination thereof.
In a still further embodiment, during deacidification, the volume ratio of aqueous or alkali solution to reaction product of the alkylation reaction comprising the light alkyl aromatic compound along with other reaction products such as heavy alkyl aromatic compound and residue catalyst ranges from about 0.2 to 1.
In an embodiment, concentration of alkali used for deacidification may range from about 2 to about 50% in alkali solution.
In another embodiment, the heavy alkyl aromatic compound produced alongside the light alkyl aromatic compound in the alkylation process is subjected to transalkylation reaction in the integrated alkylation and transalkylation process.
In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, transalkylation comprises acts of contacting heavy alkyl aromatic compound from the alkylation process with unsubstituted aromatic hydrocarbon or alkyl substituted aromatic hydrocarbon in the presence of catalyst such as ionic liquid compound to obtain light alkyl aromatic compound.
In a non-limiting embodiment, the heavy aromatic compound to be transalkylated includes but not limited to alkyl benzene having carbon atoms ranging from about 3 to about 50.
In a preferred embodiment, in the integrated alkylation and transalkylation process of the present disclosure, in transalkylation, the heavy alkyl aromatic compound to be

transalkylated is selected from but not limited to alkyl benzene having alkyl carbon atoms ranging from about 3 to about 50 with benzene or toluene.
In an embodiment, the alkyl substituted aromatic compound is selected from a group comprising decyl benzene, undecyl benzene, dodecyl benzene, tridecyl benzene, tetradecyl benzene or combinations thereof.
In yet another embodiment, the catalyst used in the transalkylation reaction of the integrated alkylation-transalkylation process is a strong lewis acid based ionic liquid compound.
In another non-limiting embodiment, the heavy alkyl aromatic compound is provided as an operation process stream and the aromatic compound is provided as another process stream.
In an embodiment of the present disclosure, the ionic liquid compound used as catalyst for the transalkylation reaction of the integrated alkylation-transalkylation process of the
present disclosure is the ionic liquid of Formula I - [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o
(solvent)]
wherein,
M1, M2 & M3 are metals independently selected from a group comprising Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg or any combination thereof, X & Y are halides, p represents 0 to 5, q represents 0 to 5, r represents 0 to 5, ‘m’ represents 0 to 20, ‘n’ represents 0 to 20, ‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other, respectively,
OH is hydroxyl group,

the solvent is at least one selected from a group comprising benzene, toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and ethylene dichloride, or any combination thereof.
In a specific embodiment the ionic liquid compound of formula I in the transalkylation process in the integrated alkylation and transalkylation is Al4(OH)3Cl9C6H6.
In another embodiment, the ionic liquid compound Al4(OH)3Cl9C6H6 is a mixture of Al(OH)3 and AlCl3 in presence of benzene.
In a further embodiment, the mole ratio of metal hydroxide to metal halide is about 1:3 with about 40 % to 50% benzene by weight.
In an embodiment, the ionic liquid compound is a recyclable catalyst in the transalkylation reaction of the integrated alkylation and transalkylation process of the present disclosure, thereby the ionic liquid compound employed during transalkylation is either fresh ionic liquid compound or recycled ionic liquid compound or partly recycled ionic liquid compound or combination thereof. In an embodiment, in the integrated alkylation and transalkylation process of the present disclosure, during transalkylation, the catalyst such as ionic liquid compound is provided as a stream.
In a further embodiment, in the integrated alkylation and transalkylation, the reaction product of the transalkylation reaction comprising the light alkyl aromatic compound of interest is deacidified and distilled to isolate the light alkyl aromatic product and the catalyst is optionally recycled.
In a further embodiment, post the transalkylation reaction of the integrated alkylation and transalkylation process of the present disclosure, deacidification is carried out using techniques including but not limited to treatment with aqueous solution such as alkali solution selected from a group comprising sodium hydroxide, calcium hydroxide and potassium hydroxide, or any combination thereof.
In a still further embodiment, during deacidification, the volume ratio of aqueous or alkali solution to reaction product of the transalkylation reaction comprising the light

alkyl aromatic compound along with other reaction products such as heavy alkyl aromatic compound and residue catalyst ranges from about 0.2 to about 1.
In a relating embodiment, concentration of alkali used for deacidification may range from about 2 to about 50% in alkali solution.
In another non-limiting embodiment, in the integrated alkylation and transalkylation process of the present disclosure, in transalkylation, the ratio of unsubstituted aromatic hydrocarbon or alkyl substituted aromatic hydrocarbon to the heavy alkyl aromatic compound ranges from about 1:1 to 20:1.
In a preferred embodiment, in the integrated alkylation and transalkylation process of the present disclosure, in transalkylation, the ratio of unsubstituted aromatic hydrocarbon or alkyl substituted aromatic compound such as alkyl substituted aromatic hydrocarbon to the heavy alkyl aromatic compound is about 2:1 to 8:1.
In another embodiment, in the integrated alkylation and transalkylation process of the present disclosure, during transalkylation, the volume ratio of catalyst such as ionic liquid compound to the feed comprising the unsubstituted aromatic hydrocarbon or alkyl substituted aromatic hydrocarbon and heavy alkyl aromatic compound ranges from about 0.01 to about 1.5.
In another non-limiting embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the transalkylation is carried out at a temperature ranging from about 5oC to 170oC.
In a preferred embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the transalkylation is carried out at a temperature ranging from about 50 to 150 oC.
In a non-limiting embodiment, in the integrated alkylation and transalkylation process of the present disclosure, the transalkylation is carried out at a pressure ranging from about 1 atmospheres to 50 atmospheres,

In a preferred embodiment, the transalkylation is carried out at a pressure ranging from about 1 atmosphere to 10 atmospheres.
In an embodiment the alkylation and transalkylation process in the integrated alkylation and trans-alkylation process is carried out continuously or simultaneously or in combination
In a further embodiment, the mixed stream comprising the aromatic compound and the heavy alkyl aromatic compound is contacted with catalyst stream comprising the ionic liquid compound at a temperature ranging from about 5 oC to about 170 oC, preferably at a temperature ranging from about 50oC to 150 oC and a pressure ranging from about 1 atmospheres to 50 atmospheres, preferably 1 to 10 atmospheres.
In a still further embodiment, volume ratio of catalyst such as ionic liquid compound to the feed comprising mixture of heavy aromatic compound and alkyl substituted aromatic compound ranges from about 0.01 to 1.5.
In an embodiment of the present disclosure, the ionic liquid compound used as catalyst for the integrated alkylation-transalkylation process of the present disclosure is
represented by Formula I - [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o (solvent)]
wherein,
M1, M2 & M3 are metals independently selected from a group comprising
Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg or any
combination thereof,
X & Y are halides,
p represents 0 to 5,
q represents 0 to 5,
r represents 0 to 5,
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,

OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene, toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and ethylene dichloride, or any combination thereof.
In a specific embodiment the catalyst used for alkylation is having the general formula is Al4(OH)3Cl9C6H6.
In a related embodiment, the ionic catalyst Al4(OH)3Cl9C6H6is a mixture of Al(OH)3 and AlCl3 in presence of benzene.
In a further embodiment, the mole ratio of metal hydroxide to metal halide is about 1:3 with about 40% to 50% benzene by weight.
In yet another embodiment, the catalyst obtained after the alkylation and transalkylation reactions is either recycled as such or recycled after regeneration.
In a specific embodiment fresh catalyst can be used for alkylation and the spent catalyst obtained from alkylation section along with or without make-up of fresh catalyst can be used for trans-alkylation.
In another embodiment, fresh catalyst can be used for trans-alkylation and the spent catalyst obtained from trans-alkylation section along with or without make-up of fresh catalyst can be used for alkylation.
In an embodiment, deacidification of the reaction product comprising the light alkyl aromatic compound of both the alkylation and transalkylation reactions is carried out using techniques including but not limited to wash with aqueous solution or alkali such as but not limited to NaOH, Ca(OH)2, KOH or centrifugation or alumina treatment or HCl stripping .
In a relating embodiment, the volume ratio of aqueous or alkali solution to reaction products of the alkylation and transalkylation reactions comprising the light alkyl aromatic compound ranges from about 0.2 to about 1.

In a further embodiment, concentration of alkali ranges from about 2% to about 50% in alkali solution.
In a non-limiting embodiment, the system for the integrated alkylation and transalkylation process in the presence of the ionic liquid compound of formula I acting as catalyst comprises:
a) at least one mixer adapted to independently receive mixture comprising substituted or unsubstituted aromatic hydrocarbon or paraffin, olefins and ionic liquid of compound of formula I ; wherein the mixer is adapted to convert substituted or unsubstituted aromatic hydrocarbon or or paraffin and olefin into light alkyl aromatic compound during the alkylation reaction or mixture of substituted or unsubstituted aromatic hydrocarbon and heavy alkyl aromatic compounds obtained after alkylation into light alkyl aromatic compound during the transalkylation reaction;
b) at least one settler unit fluidly connected to at least one mixer, the settler unit is adapted to receive at least one of the substituted or unsubstituted aromatic hydrocarbon or paraffin, the olefin, the ionic liquid compound of formula I (spent/fresh), the light alkyl aromatic compound and the heavy alkyl aromatic compound obtained after the alkylation reaction, or the light alkyl aromatic compound and the ionic liquid compound of formula I (spent/fresh) obtained after the transalkylation reaction; wherein the settler unit is adapted to separate at least one of linear alkyl aromatic compound, ionic liquid compound of formula I (spent/fresh), substituted or unsubstituted aromatic hydrocarbon or paraffin, olefin;
c) at least one purifier fluidly connected to at least one of the settler unit, the purifier is adapted to receive at least one of the light alkyl aromatic compound, ionic liquid compound of formula I (spent/fresh), heavy alkyl aromatic compound, substituted or unsubstituted aromatic hydrocarbon or paraffin and alkali solution, post the alkylation reaction and light alkyl aromatic compound or ionic liquid compound of formula I (spent/fresh), post the transalkylation reaction; wherein the purifier is adapted to purify the light alkyl aromatic compound;

d) at least one fractionating column adapted to receive at least one of the light alkyl aromatic compound, the heavy alkyl aromatic compound, substituted or unsubstituted aromatic hydrocarbon or paraffin, the olefin and ionic liquid compound of formula I (spent/fresh), post the alkylation reaction and the light alkyl aromatic compound and the ionic liquid compound of formula I (spent/fresh) post the transalkylation reaction from at least one settler unit and wherein the fractionating column is adapted to separate at least one of the light alkyl aromatic compound, the heavy alkyl aromatic compound, substituted or unsubstituted aromatic hydrocarbon or paraffin, the olefin and ionic liquid compound of formula I (spent/fresh); and
e) at least one catalyst recovery unit adapted to receive at least one of the ionic liquid compound of formula I (spent/fresh), the light alkyl aromatic compound, the heavy alkyl aromatic compound, the substituted or unsubstituted aromatic hydrocarbon or paraffin, and the olefin post the alkylation reaction and light alkyl aromatic compound and spent catalyst post the transalkylation reaction independently from at least one of the settler unit and at least one of the fractionating column; wherein the catalyst recovery unit is adapted to regenerate the ionic liquid compound of formula I acting as catalyst.
In another embodiment, the settling step can be can be a single step settling or a multi-step settling with a series of settlers, either horizontal or vertical.
In a further embodiment, the settlers can be gravity settling vessel, either horizontal or vertical or centrifugal separator.
In another embodiment, a purifier is employed to remove acid traces from the light alkyl aromatic compound.
In a further embodiment, the purifier is selected from a group comprising a stirred vessel, centrifuge separator, packed column packed with alumina and stripper or a combination thereof.

In an exemplary embodiment, figure 1 illustrates the system for integrated alkykation and transalkylation process for manufacturing of light alkyl aromatic compound using an ionic liquid compound formed by reacting metal halides and metal hydroxides in the presence of solvent.
In an embodiment, the system comprises one or more mixers M1, M2, M3…Mn (collectively referred as M) configured to carry out alkylation process between the aromatic hydrocarbon or paraffin and the olefin or transalkylation process between the heavy alkyl aromatic compound formed as a result of the alkylation process and the substituted or unsubstituted aromatic hydrocarbon or paraffin in the presence of the ionic liquid compound of formula I; one or more settler units S1, S2, S3..Sn (collectively referred as S) which are fluidly connected to one or more mixers (M). The settler units (S) are configured to receive at least one of the heavy alkyl aromatic compound, the substituted or unsubstituted aromatic hydrocarbon or paraffin, the olefin, the ionic liquid compound of formula I and the light alkyl aromatic compound from the one or more mixers (M), and are adapted to carry out layer separation of at least one of the heavy alkyl aromatic compound, the substituted or unsubstituted aromatic hydrocarbon or paraffin, the ionic liquid compound of formula I and the light alkyl aromatic compound. The system also includes a purifier (PR) fluidly connected to the one or more settlers (S), and is configured to receive separated layer comprising the light alkyl aromatic compound from the one or more settlers (S). The purifier (PR) is adapted to purify the light alkyl aromatic compound. Further, the purified light alkyl aromatic compound from the purifier (PR) is fed back to the one or more settler unit (S) for further layer separation. The system also comprises one or more fractionating columns D1, D2, D3…Dn (collectively referred as D) fluidly connected to the one or more settlers units (S) for receiving further the separated layer comprising light alkyl aromatic compound from the one or more settler (S). The one or more fractionating columns (D) are configured to further separate the light alkyl aromatic compounds and recycle at least one of the heavy alkyl aromatic compound, the substituted or unsubstituted aromatic hydrocarbon or paraffin, the olefin and the ionic liquid compound of formula I, use to the one or more mixers (M). Further, a catalytic recovery unit (CRU) is provided in the system, and is fluidly connected to one or more settler units (S) for recovering or regenerating ionic liquid compound of formula I after layer separation, and recycle the ionic liquid compound of formula I to the one or more mixers (M).

In a non-limiting embodiment of the present disclosure, the system comprises first mixer (M1), second mixer (M2) and third mixer (M3). In an embodiment, the mixers M1, M2 and M3 are selected from a group comprising stirred vessel, plug flow reactor, static mixer, jet mixer and pump mixer, or any combination thereof. The system also comprises a first settler unit (S1), a second settler unit (S2) and a third settler unit (S3). In an embodiment, the settler units S1, S2 and S3 is a settling vessel such as but not limited to gravity settling vessel, arranged either horizontally or vertically, comprising single step settling or multi-step settling with a series of settlers arranged inside the settler units, either horizontally or vertically.
In a non-limiting embodiment, the purifier (PR) of the system is selected from a group comprising vessel such as stirred vessel, a separator such as centrifuge separator a column packed with alumina, an evaporator, and an acid stripper. In an exemplary embodiment, the purifier of the system removes acid traces from the light alkyl aromatic compound.
In an exemplary embodiment the working of the system for integrated alkylation and transalkylation process employing the ionic liquid compound of formula I as catalyst comprises following steps: Initially, the reaction raw material is prepared by mixing an aromatic hydrocarbon such as but not limited to benzene or alkyl substituted benzene or paraffin; and olefin coming from lines 1 and 2, respectively to obtain pre-mixed feed. The pre-mixed feed is then fed to mixer M1 where fresh/recycled/regenerated catalyst is added via line 3. The temperature in M1 is maintained between about 30 to 80 oC with a pressure of about 1 to 5 atmospheres. The mole ratio of benzene to olefin is in the range of about 2:1 to 12:1. The volume ratio of catalyst to pre-mixed feed is in the range of about 0.1 to 1.5. The reaction takes place in M1. The outlet of M1 is directly fed into second mixer M2 where further reaction takes place. The temperature and pressure conditions in M2 can be same as M1 or can be different. The outlet from M2 is fed into settler S1 where hydrocarbon and catalyst layers are separated. The heavier catalyst layer from S1 via line 7 is recycled to mixer M1/M3 directly or through catalyst recovery unit CRU. The upper hydrocarbon layer from S1 which comprises the light alkyl aromatic compound and the heavy alkyl aromatic compound produced alongside is fed to mixer M3 via line 6 where fresh/recycled/regenerated catalyst is added via line 3 or line 7. The

outlet from M3 is fed into settler S2 where hydrocarbon layer comprising the light alkyl aromatic compound of interest and catalyst layer are separated. The heavier catalyst layer from S2 via line 10 is recycled to mixer M1/M3 through CRU. Alternatively the heavier catalyst layer via line 10 is transferred to a centrifugal separator to removal of acid soluble oil free catalyst layer from the top and bulk catalyst layer from the bottom which is sent to CRU via line 10A. The upper hydrocarbon layer from S2 comprising the light alkyl aromatic compound of interest is fed to hydrocarbon purifier PR1 via line 9, where the hydrocarbon layer is washed with either water or alkali solution via line 11 or directly centrifuged without any addition of water or alkali solution to remove trace acid content in the light alkyl aromatic compound of interest. The volume ratio of water or alkali solution to hydrocarbon layer comprising the light alkyl aromatic compound is in the range of about 0.2 to 1 & the concentration of alkali may range from about 2-50% in alkali solution. The said purifier PR1 can also be a packed column filled with alumina or evaporator or stripper to remove acidic traces in hydrocarbon layer comprising the light alkyl aromatic compound of interest. The outlet from PR is directly fed to settler S3 where layer separation occurs. In case of water or alkali wash the bottom layer will be aqueous layer with large quantity, which is sent for effluent treatment via line 13 while in case of centrifugation or crystallization the bottom layer will be catalyst layer with very small quantity which is fed to CRU via line 13A. The upper hydrocarbon layer from S3 comprising the light alkyl aromatic compound of interest is fed to fractionating column D1 where benzene is distilled off and recycled to line1 via line 15. The residue of D1 is fed to fractionating column D2 via line 16 to remove and recover paraffin via line 17. The residue of fractionating D2 is fed to fractionating column D3 to separate light alkyl aromatic product by line 19 and heavy alkylated product by line 20. The distillation columns D1, D2 & D3 can be operated under pressure or atmospheric pressure or under vacuum. The heavy alkylated product (HAB) obtained from D3 via line 20 is pre-mixed with benzene stream coming from line 1. The pre-mixed feed having the HAB is then fed to mixer M4 where fresh/regenerated catalyst is added via line 3. The catalyst may be either pure catalyst or pre-mixed catalyst where the said catalyst is mixed with solvent such as benzene or toluene. Alternatively the catalyst can be the spent catalyst obtained from alkylation section via line 21 from centrifugal separator (CF). The temperature in M4 is maintained between 30 to 150 oC with a pressure of 1 to 20 atmospheres. The mole ratio of benzene to HAB is in the range of 2:1 to 8:1. The volume ratio of catalyst to pre-mixed feed is in the range of 0.01 to 1.5.The transalkylation takes place in M4. The outlet

of M4 is directly fed into another mixer M5 where further transalkylation takes place. The temperature and pressure conditions in M5 can be same as M4 or can be different. The outlet from M5 is fed into settler S4 where hydrocarbon and catalyst layers are separated. The heavier catalyst layer from S4 via line 25 is recycled to mixer M4/M6, trans-alkylation section or to mixer M1/M3 in alkylation section directly or through catalyst recovery unit CRU. The upper hydrocarbon layer from S4 comprising the light alkyl aromatic compound of interest is fed to mixer M6 via line 24 where fresh/recycled/regenerated/spent catalyst is added via line 3 or line 21. The outlet from M6 is fed into settler S5 where hydrocarbon layer comprising the light alkyl aromatic compound and catalyst layer are separated. The heavier catalyst layer from S5 via line 28 is recycled to mixer M4/M6 through CRU. The upper hydrocarbon layer comprising the light alkyl aromatic compound is fed to hydrocarbon layer purifier PR2 via line 27, where the hydrocarbon layer is washed with either water or alkali solution via line 29 or directly centrifuged without any addition of water or alkali solution to remove trace acid content in the hydrocarbon layer. The volume ratio of water or alkali solution to hydrocarbon layer comprising the light alkyl aromatic compound is in the range of about 0.2 to 1 & the concentration of alkali may range from about 2-50% in alkali solution. The said purifier PR2 can also be a packed column filled with alumina or evaporator or stripper to remove acidic traces in hydrocarbon layer. The outlet from PR is directly fed to settler S6 where layer separation occurs. In case of water or alkali wash the bottom layer will be aqueous layer with large quantity, which is sent for effluent treatment via line 31 while in case of centrifugation or crystallization the bottom layer will be catalyst layer with very small quantity which is fed to CRU via line 31A. The upper hydrocarbon layer from S6 comprising the light alkyl aromatic compound of interest is fed to fractionating column D4 where benzene is distilled off and recycled to line1 via line 33. The residue of D4 is fed to fractionating column D5 via line 34 to remove and recover light end aromatics generated during trans-alkylation reaction via line 35. The residue of fractionating D5 is fed to fractionating column D6 to separate linear alkyl benzene product by line 37 and unreacted heavy alkylated product by line 38. The distillation columns D4, D5 & D6 can be operated under pressure ranging from about about 1.05Kg/cm2 to 1.5kg/cm2 or atmospheric pressure or under vacuum condition ranging from about 0.05 kg/cm2 to 0.5 kg/cm2. This unreacted heavy alkylated product by line 38 is recycled back to mixer M4 or can be removed via line 39 either fully or partially.

In an embodiment, the integrated alkylation and transalkylation process of the present disclosure ,when performed in a batch mode takes about 24 hrs, wherein the duration of alkylation is about 10 minutes, duration of settling after alkylation is about 10 mins, duration of deacidification after settling is about 10 mins, duration of distillation after deacidification is about 15 hours, the duration of transalkylation is about 2 hrs, duration of settling and deacidification after transalkylation is about 30 mins, duration of distillation after settling and deacidification steps is about 6 hrs. However, a person skilled in the art will be aware that the integrated alkylation and transalkylation process may be conducted in batch modes of varying time periods by changing the time for each of the process steps.
Additional embodiments and features of the present disclosure will be apparent to one of ordinary skill in art based upon description provided herein. The embodiments herein provide various features and advantageous details thereof in the description. Descriptions of well-known/conventional methods and techniques are omitted so as to not unnecessarily obscure the embodiments herein. Further, the disclosure herein provides for examples illustrating the above described embodiments, and in order to illustrate the embodiments of the present disclosure certain aspects have been employed. The examples used herein for such illustration are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the following examples should not be construed as limiting the scope of the embodiments herein.
EXAMPLES EXAMPLE 1:
Alkylation reaction
About 120 litre/hr (104 kg/hr) of benzene and about 3.6 lit/hr of freshly prepared catalyst Al4(OH)3Cl9C6H6 are mixed in a first static mixer and this mixture is then contacted with about 500 litre/hr of olefin stream containing about 10% to 15% of C10-C14 olefins and about 85 % to 90% C10-C14 paraffins and about 150 litre/hr of benzene stream in a second static mixer. The reaction mixture from the second static mixer is sent into a vertical 2 stage separator, from where the top hydrocarbon layer comprising the light alkyl aromatic compound (linear alkyl benzene) of interest is sent to Deacidification

column and stored. The hydrocarbon layer is analysed for olefin content and the conversion of olefin obtained is 99.7%. The Linear alkyl benzene formation is confirmed by GC. The hydrocarbon layer is found to comprise of linear alkyl benzene (light aromatic compound) of interest along with heavier alkyl benzene (heavy aromatic compound). The bottom catalyst layer from the separator is continuously collected and stored in a HDPE container.
Trans-alkylation reaction
About 70 ml (61 gm) of heavier alkyl benzene stream obtained after the alkylation reaction containing 5% linear alkyl benzene, 95% heavier alkyl benzene containing diakylbenzenes and oligomers and about 70 ml (61 gm) of benzene are added to a 250 ml glass reactor equipped with an overhead stirrer. To the above mixture, about 35 g of catalyst layer obtained post the alkylation reaction after separation from other reaction products is added. The reaction mass is then heated to about 80 oC and maintained under stirring for about 2 hours. After about 2 hours the reaction mass is cooled to about 40oC and settled for about 20 minutes. The layers are then separated. The upper layer is the benzene rich hydrocarbon layer while the lower layer is catalyst layer. The upper layer is then analysed for gas chromatography to get heavier alkyl benzene (heavy aromatic compound) content. The conversion of heavier alkyl benzene to linear alkyl benzene (light aromatic compound) obtained is about 78%.
REFERENCE NUMERAL TABLE:

Reference No. Description
M1 First Mixer
M2 Second Mixer
M3 Third Mixer
M4 Fourth Mixer
M5 Fifth Mixer

M6
Sixth Mixer
S1 First Settler unit
S2 Second Settler unit
S3 Third Settler unit
S4 Fourth Settler unit
S5 Fifth Settler unit
S6 Sixth Settler unit
CF Centrifugal Separator
PR1 Purifier
PR2 Purifier
CRU Catalyst Recovery Unit
D1 First Fractionating Column
D2 Second Fractionating Colum
D3 Third Fractionating Column
D4 Fourth Fractionating Column
D5 Fifth Fractionating Column
D6 Sixth Fractionating Column
Line 1 Carries benzene for mixing with contents from Line 2.
Line 2 Carries olefins for mixing with contents of Line 1.
Line 3 Connected to first, second and third mixer for adding fresh/recycled/regenerated catalyst.
Line 4 Connects first mixer to second mixer.

Line 5 Connects second mixer to first settler .
Line 6 Connects first settler to third mixer for feeding upper hydrocarbon layer.
Line 7 Connects first settler to M1/M3 directly or through CRU for feeding heavier catalyst layer.
Line 8 Connects third mixer to second settler.
Line 9 Connects second settler to purifier PR1 where hydrocarbon layer is washed.
Line 10 Connects second settler to mixers M1/M3 through CRU.
Line 11 Carries water or alkali to PR1 for washing hydrocarbon layer
Line 12 Connects purifier PR1 to third settler.
Line 13 Carries aqueous layer from S3 post water/alkali wash for effluent treatment.
Line 13A Carries catalyst layer from S3 to CRU post centrifugation or crystallization.
Line 14 Connects third settler to first fractionating column.
Line 15 Connects D1 to Line 1 for recycling upper hydrocarbon layer from S3 after distilling off benzene.
Line 16 Connects first fractionating column to second fractionating column for removal and recovery of substituted or unsubstituted aromatic hydrocarbon or paraffin.
Line 17 Line originating from D2 for removal and recovery of substituted or unsubstituted

aromatic hydrocarbon or paraffin.
Line 18 Connects second fractionating column to third fractionating column.
Line 19 Connects D2 to D3 to separate alkyl benene product.
Line 20 Connects D3 to M4 carrying HAB pre-mixed with benzene stream from line 1.
Line 21 Carries spent catalyst from CF to mixers M4/M5.
Line 22 Connects fourth mixer to fifth mixer.
Line 23 Connects fifth mixer fourth settler unit.
Line 24 Connects fourth settler unit to sixth mixer carrying upper hydrocarbon layer.
Line 25 Connects S4 to M1/M3 or M4/M6 through CRU carrying heavier catalyst layer.
Line 26 Connects sixth mixer to fifth settler unit.
Line 27 Connects fifth settler unit to purifier PR2 carrying upper hydrocarbon layer.
Line 28 Connects S5 to mixers M4/M6 through CRU carrying heavier catalyst layer.
Line 29 Carries water or alkali to PR2 for washing hydrocarbon layer
Line 30 Connects purifier PR2 to sixth settler unit.
Line 31 Carries aqueous layer from S6 post water/alkali wash for effluent treatment.
Line 31A Carries catalyst layer to from S6 CRU post centrifugation or crystallization.

Line 32 Connects sixth settler unit to fourth fractionating column carrying upper hydrocarbon layer.
Line 33 Connects D4 to Line 1 for recycling of benzene.
Line 34 Connects fourth fractionating column to fifth fractionating column. Removes light end aromatics.
Line 35 Removes light end aromatics from D5.
Line 36 Connects D5 to D6.
Line 37 Connects D2 to D3 to separate linear alkyl benzene product.
Line 38 Connects D2 to D3 to separate heavy alkylated benzene product.

We Claim:
1. An integrated alkylation and transalkylation process to obtain light aromatic
compound, said process comprising steps of:
a) contacting aromatic hydrocarbon or paraffin with olefin in presence of
ionic liquid compound of formula I - [(M1)p(M2)q(M3)r (OH)m(X)n(Y)o
(solvent)]wherein,
M1, M2 & M3 are metals independently selected from a group comprising
Al, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Ge, In, Sn, Ti, Pb, Cd and Hg, or any
combination thereof,
X & Y are halides,
p represents 0 to 5,
q represents 0 to 5,
r represents 0 to 5,
‘m’ represents 0 to 20,
‘n’ represents 0 to 20,
‘o’ represents 0 to 20,
M1, M2 and M3 are same or different with respect to each other,
respectively,
X=Y or X≠Y,
OH is hydroxyl group,
the solvent is at least one selected from a group comprising benzene,
toluene, xylene, chlorobenzene, bromobenzene, hexamethyl benzene and
ethylene dichloride, or any combination thereof,
to obtain light alkyl aromatic compound and heavy aromatic compound;
b) contacting the heavy aromatic compound of step a) with alkyl
substituted aromatic compound in presence of said ionic liquid compound,
to obtain the light aromatic compound.
2. The integrated alkylation and transalkylation process as claimed in claim 1,
wherein the aromatic hydrocarbon is selected from a group comprising substituted
and unsubstituted aromatic hydrocarbon, or a combination thereof; wherein the
unsubstituted aromatic hydrocarbon is benzene and the substituted hydrocarbon is

selected from a group comprising toluene, ethylbenzene, xylenes, cumene, ;wherein, the paraffin having carbon atoms about 2 to 50 is selected from a group comprising straight chain or isomers of butane, pentane, hexane, heptane, octane, nonane, decane, undecane, dodecane, tridecane and tetradecane or combinations thereof; wherein the olefin having carbon atoms about 2 to 50 is selected from a group comprising straight chain or isomers of butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, tridecene and tetradecene or combinations thereof; wherein the heavy aromatic compound is selected from a group comprising isomers of dimethyl benzene, trimethyl benzene, diethyl benzene, triethyl benzene, dibutyl benzene, dipentyl benzene, diheptyl benzene, dioctyl benzene, didecyl benzene, didodecyl benzene, diundecyl benzene, ditridecyl benzene and ditetradecyl benzene or combinations thereof; the alkyl substituted aromatic compound is selected from a group comprising decyl benzene, undecyl benzene, dodecyl benzene, tridecyl benzene and tetradecyl benzene or combinations thereof and the light aromatic compound is selected from a group comprising isomers of methyl benzene, ethyl benzene, propyl benzene, butyl benzene, pentyl enzene, hexyl benzene and heptyl benzene or combinations thereof.
3. The integrated alkylation and transalkylation process as claimed in claim 1, wherein molar ratio of the aromatic hydrocarbon or paraffin to olefin ranges from about 2:1 to 20:1.
4. The integrated alkylation and transalkylation process as claimed in claim 1, wherein molar ratio of the alkyl substituted aromatic hydrocarbon to heavy alkyl aromatic compound ranges from about 1:1 to 20:1, preferably about 2:1 to 8:1.
5. The integrated alkylation and transalkylation process as claimed in claim 1, wherein volume ratio of the ionic liquid compound of formula I to the aromatic hydrocarbon or the paraffin and the olefin ranges from about 0.001 to 1.5 and wherein volume ratio of the ionic liquid compound of formula I to the alkyl substituted aromatic hydrocarbon and heavy alkyl aromatic compound ranges from about 0.01 to 1.5.

6. The integrated alkylation and transalkylation process as claimed in claim 1, wherein the ionic liquid compound of formula I is Al4(OH)3Cl9C6H6.
7. The integrated alkylation and transalkylation process as claimed in claim 1, wherein the contacting of the step a) is at a temperature ranging from about 5oC to 150oC, preferably ranging from about 10oC to 100oC, and at a pressure of about 50 atmosphere, preferably at a pressure of about 10 atmosphere.
8. The integrated alkylation and transalkylation process as claimed in claim 1, wherein the contacting of the step b) is at a temperature ranging from about 5oC to 170oC, preferably ranging from about 50oC to 150oC, and at a pressure ranging from about 1 atmosphere to 50 atmosphere, preferably about 1 atmosphere to 10 atmosphere.
9. The integrated alkylation and transalkylation process as claimed in claim 1, wherein the step a) and the step b) independently further comprises deacidification of the light alkyl aromatic compound by method selected from a group comprising washing with alkali solution, centrifugation, alumina treatment and acid stripping, or any combination thereof.
10. The integrated alkylation and transalkylation process as claimed in claim 9, wherein the deacidification of the light alkyl aromatic compound is carried out by washing the light alkyl aromatic compound with the alkali solution having a concentration of about 2% to 50%, wherein the alkali is selected from a group comprising sodium hydroxide, potassium hydroxide and calcium hydroxide, or any combination thereof, and wherein the volume ratio of the alkali solution to the light alkyl aromatic compound ranges from about 0.2 to 1.
11. The integrated alkylation and transalkylation process as claimed in claim 1, wherein in the step a) conversion of the olefin ranges from about 99% to 99.7%
12. The integrated alkylation and transalkylation process as claimed in claim 1, wherein in the step b) conversion of the heavy alkyl aromatic compound to the light aromatic compound ranges from about 40% to 80%.

13. A system for an integrated alkylation and transalkylation process of claim 1 to obtain light alkyl aromatic compound, said system comprising:
a) at least one mixer adapted to independently receive substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, paraffin, olefin or heavy aromatic compound and ionic liquid compound of formula I and wherein the mixer is adapted to convert the substituted aromatic hydrocarbon or unsubstituted aromatic hydrocarbon or paraffin or heavy aromatic compound to the light alkyl aromatic compound in presence of ionic liquid compound of formula I and olefin or alkyl substituted aromatic compound;
b) at least one settler unit fluidly connected to the mixer, wherein the settler unit is adapted to receive at least one of the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon the paraffin, the olefin and the ionic liquid compound of formula I, the light alkyl aromatic compound, the alkyl substituted aromatic compound and the heavy aromatic compound from the mixer, and wherein the settler unit is adapted to cause settling of at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the olefin, the alkyl substituted aromatic compound and the paraffin;
c) at least one purifier fluidly connected to the settler unit, wherein the purifier is adapted to receive at least one of the light alkyl aromatic compound, the ionic liquid compound of formula I, the olefin, the substituted aromatic hydrocarbon, unsubstituted aromatic hydrocarbon, the paraffin, the olefin, the heavy aromatic compound, the alkyl substituted aromatic compound and alkali solution and wherein the purifier is adapted to purify the light alkyl aromatic compound;
d) at least one fractionating column adapted to receive at least one of the light alkyl aromatic compound, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin, the olefin and the ionic liquid compound of formula I from the settler unit and wherein the fractionating column is adapted to separate at least one of the light alkyl aromatic compound, the heavy aromatic

compound, the unsubstituted aromatic hydrocarbon, the alkyl substituted aromatic compound, the ionic liquid compound of formula I and the paraffin; and e) at least one catalyst recovery unit adapted to receive at least one of the ionic liquid compound of formula I, the heavy aromatic compound, the substituted aromatic hydrocarbon, the unsubstituted aromatic hydrocarbon, the paraffin the alkyl aromatic compound and the light alkyl aromatic compound, independently from the settler unit and the fractionating column and wherein the catalyst recovery unit is adapted to regenerate the ionic liquid compound of formula I.
14. The system as claimed in claim 13, wherein the mixer is selected from a group comprising stirred vessel, plug flow reactor, static mixer, jet mixer and pump mixer, or any combination thereof.
15. The system as claimed in claim 13, wherein the settler unit is selected from a group comprising gravity settling vessel and decanter, and wherein the settler unit is arranged horizontally or vertically comprising series of settlers arranged inside the settler unit either horizontally or vertically, or a combination thereof.
16. The system as claimed in claim 13, wherein the purifier is selected from a group comprising stirred vessel, centrifuge separator, column packed with alumina, evaporation and stripper, or any combination thereof.
17. The system as claimed in claim 13, wherein the mixer is at a temperature ranging from about 5oC to 170oC and at a pressure ranging from about 1 atmosphere to 50 atmospheres.
18. The system as claimed in claim 13, wherein the conversion of heavy alkyl
aromatic compound ranges from about 40% to 80%.