Description:FORM 2

THE PATENTS ACT, 1970
(39 of 1970)
&
THE PATENT RULES, 2003

COMPLETE SPECIFICATION
(See Section 10 and Rule 13)

TITLE OF INVENTION:
A SYSTEM FOR SYNTHESIS OF MIBT

APPLICANT
VINATI ORGANICS LIMITED
An Indian entity
having address,
Parinee Crescenzo, "A" Wing, 11th floor, 1102,
'G' Block, Behind MCA, Bandra-Kurla Complex, Bandra (east),
Mumbai – 400051, India

The following specification describes the invention and the manner in which it is to be performed.

CROSS-REFERENCE TO RELATED APPLICATIONS AND PRIORITY
The present application claims no priority from any of the patent application(s).

TECHNICAL FIELD
The present subject matter described herein, in general, is about a system for the preparation of alkyl aromatic hydrocarbons. More specifically, it is related to a system for the synthesis of m-isobutyl toluene (MIBT).

BACKGROUND
The production of alkyl aromatic hydrocarbons is an important industrial process. Although these hydrocarbons can be recovered from reaction products such as reformates or from naturally occurring petroleum, the most commercially feasible route to the production of alkyl aromatics appears to be the direct alkylation of a feed aromatic hydrocarbon with a feed acyclic olefinic hydrocarbon. A wide variety of alkyl aromatic product hydrocarbons can be produced because of the various feed hydrocarbons in both the aromatic and acyclic categories which can be supplied to the alkylation zone.

The alkylation of aromatic hydrocarbons wherein alkyl side chains are attached to the aromatic nucleus may be elected in the presence of a variety of alkylation catalysts, and with alkylating agents in various forms such as alkyl halides, alcohols, olefins, and the like.

In the traditional fractionation method of recovering the product alkyl aromatic hydrocarbon, the overhead streams of the fractionation columns have been condensed in water cooled heat exchangers resulting in the production of relatively low-pressure steam. The low-pressure steam generated results in all or most of the heat which is discharged in the overhead system of the column being unrecovered and being a net charge against the utility cost of operating the process.
In the process of alkylation, a succession of reactions may take place whereby the alkylated products comprise a mixture of mono, di- and tri-alkylated compounds, up to the limit of substitutable hydrogen atoms on the nucleus. Apparently, the introduction of the original alkyl group activates the nucleus for further substitution, so that the mono-alkyl benzenes are subject to further alkylation to an extent dependent on the catalyst, the olefinic alkylating agent, and the reaction conditions. Since the poly alkyl benzenes are often relatively unsatisfactory products, their formation represents a loss of valuable raw materials and decreased yield from the alkylation process.
The prior art WO2017058373A1 (hereinafter referred to as “WO’373 publication”) describes an apparatus for carrying out a process wherein an inert gas contacts with one or more catalyst compositions suitable for methylation of toluene and hydrogenation of phenol in a reactor. The WO’373 publication discloses a process and apparatus for the alkylation of toluene (aromatic hydrocarbon). The process involves contacting an inert gas with one or more catalysts under conditions effective to convert toluene to xylene, and then separating at least one para-xylene-enriched stream from the reactor effluent stream. The WO’373 publication also discloses dehydration unit, an aromatic hydrocarbon feed, reactor wherein the reactor is operated under conditions suitable for alkylation. The WO’373 publication further discloses about a separation unit comprising distillation tower, a simulated moving-bed separation unit, a high-pressure separator, a low-pressure separator, a flash drum, combinations. The said separation unit comprises of 3 separators wherein the third separator is a p-xylene recovery unit.
US4587370A (hereinafter referred to as “US’370 patent”) describes the apparatus for carrying out fractionation method for the recovery of product alkyl aromatic hydrocarbons produced by the alkylation of aromatic hydrocarbons. In the US’370 patent, three fractionation columns are employed in series. Aromatic feed hydrocarbons are recycled from the overhead of the first column, which is re-boiled by the overhead vapor of the second column. The product alkyl aromatic is recovered from the condensate produced in using the second column overhead as a heat source. The product alkyl aromatic is also present in the bottom of the second column which flows into a low-pressure stripping column. The entire overhead vapor of the stripping column is compressed and passed into the lower portion of the second column. The US’370 patent further discloses about alkyl aromatic hydrocarbon product and recovery wherein the reactants benzene and propylene are reacted in the presence of inert gas propane and alkylation catalyst.
The US’370 patent also discloses about a feed stream, effluent stream de-propanizing column, recycle column, fractionation column wherein the product cumene is separated from the other effluents like heavy hydrocarbons, light hydrocarbons. The fractionation columns are under distillation conditions.
A typical flow scheme suitable for commercial use is depicted in US4051191 (hereinafter referred to as “US’191 patent”). The US’191 patent describes in some detail catalyst, reaction conditions, and separatory methods suitable for the recovery of cumene. The reactor effluent is passed into a rectification zone in which propane, charged to the process in admixture with the feed propylene, is separated for recycling and for rejection from the process. Liquid phase hydrocarbons recovered in the rectification zone are then passed into a two-column fractionation train comprising a recycle column and a cumene or product column. The benzene feed aromatic hydrocarbon is recycled from the top of the first fractionation column. The product cumene is recovered from the top of the second fractionation column, with heavy aromatic by-products being withdrawn from the bottom of the second column. The by-products are produced by undesired oligomerization and alkylation reactions.

Also, in case of alkylation methods, a plurality of by-products may be generated which needs to be separated from a crude slurry of principal alkylation product. Further, in case of production of m-isobutyl toluene (MIBT) a system for maximum conversion of starting materials and further separation of aqueous and organic layer are vital factors.

Therefore, there is a long-felt need of a system for the synthesis of MIBT wherein the impurities and side-products are reduced, and any contaminant in the final product storage is removed. Further, there is a need of a system incorporating an efficient catalyst for the synthesis of alkylated aromatic hydrocarbons (e.g., MIBT) which may further reduce the time required for the reaction.

OBJECTIVES OF INVENTION
One of the objectives of the present invention is to provide a system for the synthesis of MIBT by the side-chain alkylated aromatic hydrocarbons.

Another objective is to provide a system for the synthesis of MIBT enabling the separation of different side products by separation and reducing the overall time required.

In one embodiment of the invention, the objective is to develop a system for the synthesis of MIBT enabling alkylation of the side-chain of aromatic compounds to obtain enhanced yield in a reduced reaction time.

SUMMARY
This summary is not intended to identify essential features of the claimed subject matter, nor is it intended for use in determining or limiting the scope of the claimed subject matter. This summary is provided to introduce concept related to system for the alkylation of aromatic hydrocarbons, and more particularly for the synthesis of MIBT and the concepts are further described below in the detailed description.

In an embodiment of the present disclosure, a system for synthesis of m-isobutyl toluene (MIBT) is disclosed. The system may comprise a catalyst preparation apparatus configured for mixing a catalyst and m-xylene to form a catalyst slurry. The system may further comprise a reactor system configured for combining catalyst slurry with propylene and m-xylene at a predetermined temperature and pressure forming crude MIBT by enabling a selective side chain alkylation reaction. The system may further comprise a neutralizer for mixing water with the crude MIBT and to dissolve catalyst slurry. The system may further comprise a separator assembly for separating an aqueous layer and an organic layer. The system may also comprise a MIBT storage tank for collecting the MIBT from the separated organic layer.
BRIEF DESCRIPTION OF DRAWINGS
The detailed description of the drawings is outlined with reference to the accompanying figures. In the figures, the left-most digit (s) of a reference number identifies the Figure in which the reference number first appears. The same numbers are used throughout the drawings to refer like features and components.

Figure 1 depicts a system (100) for the synthesis of m-isobutyl toluene (MIBT), in accordance with an embodiment of the present subject matter.

Figure 2 depicts a separator assembly (105) configured for separation of aqueous layer and MIBT crude layer, in accordance with an embodiment of the present subject matter.

DETAILED DESCRIPTION
Reference throughout the specification to "various embodiments," "some embodiments," "one embodiment," or "an embodiment" or “in one aspect” of “in an aspect” means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment. Thus, appearances of the phrases "in various embodiments," "in some embodiments," "in one embodiment," or "in an embodiment" or “in one aspect” of “in an aspect” in places throughout the specification are not necessarily all referring to the same embodiment. Furthermore, the particular features, structures or characteristics may be combined in any suitable manner in one or more embodiments.

The words "comprising," "having," "containing," and "including," and other forms thereof are intended to be equivalent in meaning and be open-ended in that an item or items following any one of these words is not meant to be an exhaustive listing of such item or items or meant to be limited to only the listed item or items.
It must also be noted that the singular forms "a," "an," and "the" include plural references unless the context clearly dictates otherwise. Although any methods similar or equivalent to those described herein can be used in the practice or testing of embodiments of the present disclosure, the exemplary methods are described. The disclosed embodiments are merely exemplary of the disclosure, which may be embodied in various forms.
Various modifications to the embodiment may be readily apparent to those skilled in the art, and the generic principles herein may be applied to other embodiments. However, one of ordinary skill in the art may readily recognize that the present disclosure is not intended to be limited to the embodiments illustrated but is to be accorded the widest scope consistent with the principles and features described herein. The detailed description of the invention will be described hereinafter referring to accompanied drawings.
The invention relates to a system for hydrocarbon conversion process by side chain alkylation. The invention more specifically relates to the system for the synthesis of alkyl aromatic hydrocarbons by the reaction of an acrylic olefinic hydrocarbon with an aromatic feed hydrocarbon. The present disclosure is also related to a separation assembly configured to recover the crude yield of alkyl aromatic hydrocarbons from the effluent of the alkylation reactor system. The present disclosure further implements a system enabling separation and recovery of propane gas from propylene.
In one embodiment, the system is enabled to carry out MIBT production process in continuous mode, semi-continuous mode, or batch mode. Preferably, the system is enabled to carry out MIBT production process in semi-continuous mode, or batch mode.
The present disclosure aims to provide a system capable of enhancing conversion ratio of aromatic hydrocarbon of a reaction substance and manufacturing alkyl substituted aromatic hydrocarbon at high selectivity and high yield. There is provided a system wherein alkyl substituted aromatic hydrocarbon including alkylating an alkyl group in aromatic hydrocarbon having the alkyl group having a hydrogen atom at the meta position with alkene.
In one embodiment of the present disclosure, the alkylation of m-xylene with propylene in presence of a catalyst is carried out to form the MIBT. However, it is not thereby intended to preclude from the scope of the invention those other alkylation processes and hydrocarbon mixtures to which the subject invention may be applicable.
One of the known methods for production MIBT, selectively involves the side chain alkylation of m-xylene with propylene over a solid catalyst. Known processes suffer from the presence of higher content of side-products heavy hydrocarbons (HHC), low hydrocarbons (LHC) and catalyst residue and therefore substantially increase the reaction time of the m-xylene alkylation and hence reduces the yield.
It has been found that deleterious effects on downstream processes of the presence of free-radical reaction inhibitors in the m-xylene stream may be reduced by treatment of the catalyst with an inert atmosphere and a reducing atmosphere, thereby reducing the presence of undesirable catalyst impurities that are believed to produce free-radical reaction inhibitors.
In an embodiment of the present disclosure, referring to Figure 1, a system (100) for the synthesis of m-isobutyl toluene (MIBT) is illustrated, in accordance with an embodiment of the present disclosure. As shown, the system (100) may comprise a catalyst preparation apparatus (102) configured for mixing a catalyst and m-xylene received from a dryer (101) to form a catalyst slurry. The system may comprise a reactor system (103) for combining the catalyst slurry with propylene and m-xylene at a predetermined temperature and pressure forming a crude MIBT enriched stream by enabling a selective side chain alkylation reaction. The system may comprise a neutralizer (104) for mixing water with the crude MIBT and to dissolve the catalyst. The system may comprise a separator assembly (105) for separating an aqueous layer and an organic layer. The system may further comprise a MIBT storage tank (108) for collecting the MIBT from the separated organic layer.
In one embodiment, the dryer (101) is configured to remove moisture from the catalyst carrier and the m-xylene. In one embodiment, the catalyst carrier and the m-xylene are incorporated in the dryer (101) before feeding of these starting materials to the catalyst preparation apparatus (102) in order to remove the moisture. In one embodiment, the dryer (101) is configured to dry m-xylene and is in communication with the catalyst preparation apparatus (102). In one embodiment, the catalyst preparation apparatus (102) is enabled to carry out preparation of a catalyst slurry in a closed system to disallow contact of air/oxygen by N2 blanketing. The catalyst slurry prepared in the catalyst preparation apparatus (102) comprises of alkali metal catalyst such as sodium, which is highly reactive in presence of air/moisture/water. Thus, a controlled closed system enabling on-line transfer of catalyst to the reactor system (103) is highly important to improve safety and service life of all the reactors involved. As the catalyst preparation apparatus (102) enables coating of reactive molten sodium over a carrier and mixing with m-xylene solvent to form a catalyst slurry, a total selective conversion of m-xylene to MIBT improves surprisingly.
In an embodiment, the catalyst preparation apparatus (102) is configured for forming a catalyst slurry suspension comprising m-xylene and the catalyst. In an aspect of the present invention, the catalyst preparation apparatus (102) is typically configured to provide a convenient source of fresh catalyst coated over a carrier. In one embodiment, the catalyst carrier may be selected as but not limited to K2CO3.
In one embodiment, the reactor system (103) is configured for enabling a selective side chain alkylation reaction at meta position of xylene.
In a related embodiment, the reactor system (103) having a catalyst composition therein is charged with a liquified propylene from a conduit line (111), connected to the reactor system (103). Further, a feed comprising m-xylene is provided to the reactor system (103) via a conduit line (112) connected to the said the reactor system (103).
In an embodiment, the reactor system (103) may be operated under conditions suitable for alkylation of m-xylene in presence of the propylene and the catalyst. The reactor system (103) may be configured for maximum selective conversion of derivative and yield comprising MIBT based on the feeding rate of m-xylene, the catalyst slurry, and the propylene. In one embodiment, the reactor system (103) may be configured to maintain temperature at a predetermined range of 150 to 250ºC and preferably 190 to 220ºC and further combining the catalyst slurry with the propylene and m-xylene at a predetermined pressure of 30-50Kg/cm2G thereby forming the crude MIBT.
In one embodiment of the present disclosure, the reactor system (103) is operated at a temperature of 205ºC and a predetermined pressure of 30-50 Kg/cm2G (and preferably 35Kg/cm2G).
In another embodiment of the present disclosure, the reactor system (103) may be configured for admixing the feed stream of m-xylene from the conduit line (112) with a propylene feed stream from the conduit line (111) and the catalyst slurry from the catalyst preparation apparatus (102) in the reactor system (103) to obtain a crude MIBT enriched stream.
In one embodiment, the reactor system (103) may be configured to transfer the MIBT enriched stream to the neutralizer (104). The said stream comprising crude MIBT may also comprise admixture of side-products such as unreacted m-xylene, propane, crude MIBT, light-hydrocarbons (LHC), the heavy hydrocarbons (HHC) formed in the reactor system (103), and the catalyst slurry.
In one embodiment, the neutralizer (104) may be configured to mix the crude MIBT received from the reactor system (103) with water for catalyst destruction by dissolving in water. In one embodiment, the neutraliser (104) is in communication with the conduit line (113) to receive the water for dissolution of the water-soluble catalyst effluent such as sodium catalyst.
It must be noted that, the propene raw material comprises a mixture of 90% propene and 10% propane gas. The said propane gas remains unreacted in the MIBT preparation and therefore is necessary to be removed from the reaction mixture before final distillation, purification, and recovery of MIBT. According to an embodiment of the present invention, the unreacted propane gas separated from the crude MIBT enriched stream in the neutraliser (104) through the conduit is recovered and recycled into a utility chamber (104-b) through a gas holder (104-a). In one aspect of the present invention, the reactor (103) may be configured to transfer the crude MIBT enriched stream into a neutraliser (104) also acting as a depropanizing zone. The said neutralizer (104) is configured to remove unreacted propane gas and for directing further transfer of propane gas through a gas holder (104-a) to a utility unit (104-b), for recycle. The separated propane gas may be used is many applications such as fuel, and heater means. Therefore, an in-stream separation of propane gas from the system (100) is one of the advantage of components of the system (100) as implemented herewith.
In another embodiment, the system (100) may further comprise a separator assembly (105) for separation of effluents in aqueous layer and organic compounds comprising crude MIBT in an organic layer. In one embodiment, the system (100) is configured for incorporation of one or more separator assembly units connected in series for separation of aqueous and organic layer to larger extent. In one embodiment, the separator assembly (105) comprises one or more separators depending on reaction quantum.
In an embodiment, referring to Figure 2, a separator assembly (105) is illustrated in detail. As shown, the separator assembly (105) may comprise an inlet (205) receiving the crude MIBT enriched stream from the neutralizer (104) connected to the separator assembly (105). The separator assembly (105) may further comprise an outlet (204) for separating and removing the organic layer from an aqueous layer.

In one embodiment, the separator assembly (105) may be selected from suitable separation units such as, but not limited to, a distillation tower, a simulated moving-bed separation unit, a high-pressure separator, a low-pressure separator, a flash drum, or the like. In a preferred embodiment, the separator assembly (105) is a pressure generated overflow-separator.

In one aspect, the separator assembly (105) may also be provided with outlet for wastewater (206). In an embodiment, the separator assembly (105) comprises at least two baffles (201, 202) configured for separation of the aqueous layer and the organic layer by overflow mechanism. In one embodiment, the at least two baffles (201, 202) may have a same height or predefined height difference for the proper separation of aqueous and organic layer. In an exemplary embodiment the height difference ration of at least two baffles is 1:0.7. In one embodiment, the separation assembly (105) may be any separation means suitable to separate a crude MIBT enriched organic stream from the aqueous layer comprising effluent catalyst slurry and other water-soluble impurities. The mechanism in the separator assembly (105) separating the crude MIBT enriched organic stream is free from catalyst or has low catalyst impurities.

In one related embodiment, the separator assembly (105) is a pressure generated overflow-separator. In an embodiment, the said separator assembly (105) is configured for directing the separated aqueous layer to a wastewater tank (107) from a bottom portion the separator assembly (105) and transferring a separated crude MIBT enriched organic stream overflow to a distillation system from the upper portion of the separator assembly (105). Further, said separator assembly (105) is configured for transferring the separated organic layer overflow to distillation column from an upper portion of the separator assembly (105). In some embodiments, the separator assembly (105) may comprise at least two pumping units for maintaining level of organic layer above the second baffle and enabling removal of aqueous layer comprising spent from bottom of the separator.
In one embodiment, the separator assembly (105) is connected with at least one levelling pump (203).

The separator assembly (105) is configured for continuous separation of crude MIBT enriched organic stream from MIBT enriched stream and water-soluble effluents. In one embodiment, the separator assembly (105) is a horizontal separator configured for separation of crude MIBT enriched organic stream from the upper portion and the aqueous layer comprising water soluble effluents such as sodium catalyst from the lower portion. In one embodiment, the separator assembly (105) is configured for transferring the crude MIBT enriched organic stream to the distillation unit for obtaining a purified MIBT product.

In an embodiment, the system (100) further comprises of an internal inspection tank (106) for checking of purified MIBT before storing in the MIBT storage tank (108) obtained from the distillation unit (not shown in figures). In one embodiment, the internal inspection tank (106) is particularly enabled to determine the purity and quality of the purified MIBT to avoid any contamination in main MIBT storage tank. The internal inspection tank (106) enables control over an individual batch of MIBT and ensures addition of good quality MIBT product to the storage tank (108) that may be configured to store a MIBT product obtained from a plurality of batches.

In one embodiment, system (100) is configured to obtain a 35-40% yield of m-isobutyl toluene (MIBT) compound. In one embodiment, the system (100) is configured to complete the production of MIBT within 2-4 Hrs of time.
The system (100) is also configured for maximum utilization of starting materials to produce and separate side-products from MIBT stream, wherein the side-products include propane gas, HHCs, LHCs, hydrocarbons having high calorific value, fuel applications.
The preferred embodiment of the invention may accordingly be described as a system for the synthesis of an alkyl aromatic hydrocarbon which comprises contacting a feed cyclic olefinic hydrocarbon and a feed aromatic hydrocarbon with a solid alkylation catalyst in an alkylation reaction zone maintained at alkylation-promoting conditions and producing a reaction system effluent stream comprising the feed aromatic hydrocarbon, a mono-alkyl aromatic product hydrocarbon, LHC, HHC and subsequently recovering the product alkyl aromatic hydrocarbon.
Experimental examples:
Example 1:
Synthesis of MIBT (m-isobutyl toluene) by implementing system (100)
A catalyst carrier is prepared by adding K2CO3 and m-xylene in the dryer (101). The dried K2CO3 and m-xylene are added in the catalyst preparation apparatus (102). Sodium is added in the catalyst preparation apparatus (102) and a uniform catalyst slurry obtained is directly added to the reactor system (103) for the preparation of MIBT. The crude MIBT is directed to the neutraliser (104) which directs the propane gas to the utility (104-b) through the gas holder (104-a).
The reaction is carried out with higher m-xylene charged to check the effect on quantity of MIBT product yield.
A crude MIBT product obtained from reaction of predefined molar ratios of m-xylene and propylene as disclosed in Table 1 below. The crude MIBT product was then charged to the separation assembly (105). In this example, the separator assembly (105) having at least two baffles having a predetermined height difference of 1:0.7 enabling separation of organic and aqueous layers was used along with specific molar ratio of m-xylene and propylene was incorporated.

Table 1
Expt.no. Moles of m- xylene Moles of propylene Mole ratio Separator type MIBT
(%) Total Heavies (%)
1 9.46 11.31 0.84 With ordinary separator 26.79 7.41
2 7.60 5.95 1.28 With ordinary separator 9.42 2.98
3 7.60 15.48 0.49 Separator assembly (105) 34.1 17.61
4 7.60 13.10 0.58 Separator assembly (105) 35.74 12.75
5 7.60 13.10 0.58 Separator assembly (105) 36.97 11.33
6 7.60 13.10 0.58 Separator assembly (105) 37.19 13.45
7 7.60 15.48 0.49 Separator assembly (105) 37.19 17.57

Referring to Table 1, it was observed that the MIBT yield increased when a quick and better online separation by implementing the separator assembly (105) as disclosed in the embodiments of the present invention. In conclusion, the quantity of m-xylene and propylene charged to be in a certain range along proper separation of aqueous and organic layer by separator assembly (105) the enabled obtaining of good product recovery.

In another embodiment of the invention, the system (100) is in accordance with the present invention may have the following advantages, including but not limited to:
• An improved system for synthesis of MIBT improves conversion of m-xylene to obtain up to 40% selective yield
• Reduced impurities formed during the formation of the desired product
• Separation and recovery of side products such as propane which can be used as a fuel in various industrial processes

Although implementations for an apparatus and process implemented thereon for the preparation catalyst used for the synthesis of alkylated aromatic hydrocarbons have been described in language specific to structural features and/or processes, it is to be understood that the appended claims are not necessarily limited to the specific features or processes described. Rather, the specific features and processes are disclosed as examples of implementations of for an apparatus and process implemented thereon for the preparation of catalyst used for the synthesis of alkylated aromatic hydrocarbons.
, Claims:WE CLAIM:
1. A system (100) for synthesis of m-isobutyl toluene (MIBT) comprising:
a catalyst preparation apparatus (102) configured for mixing a catalyst and m-xylene to form a catalyst slurry;
a reactor system (103) for combining the catalyst slurry with propylene and m-xylene at a predetermined temperature and pressure forming crude MIBT by enabling a selective side chain alkylation reaction;
a neutralizer (104) for mixing water with the crude MIBT and to dissolve the catalyst;
a separator assembly (105) for separating an aqueous layer and an organic layer; and
a MIBT storage tank (108) for collecting the MIBT from the separated organic layer.

2. The system (100) as claimed in claim 1, wherein the reactor system (103) is configured for enabling a selective side chain alkylation reaction at meta position of xylene.
3. The system (100) as claimed in claim 1, comprising a dryer (101), wherein the dryer (101) is configured to remove moisture from the catalyst carrier and the m-xylene.
4. The system (100) as claimed in claim 1, wherein the catalyst preparation apparatus (102) is configured for forming a catalyst slurry suspension comprising m-xylene and the catalyst.
5. The system (100) as claimed in claim 2, wherein the reactor system (103) is configured to maintain temperature at a predetermined range of 190-220 oC and further combining catalyst slurry with propylene and m-xylene at a predetermined pressure of 30-50 Kg/cm2G thereby forming the crude MIBT.
6. The system (100) as claimed in claim 1, wherein the neutralizer (104) is configured to mix the crude MIBT received from the reactor system (103) with water for catalyst destruction by dissolving in water.
7. The system (100) as claimed in claim 6, wherein the neutralizer (104) is configured to remove unreacted propane gas and for directing further transfer of propane gas through a gas holder (104-a) to a utility unit (104-b), for recycle.
8. The system (100) as claimed in claim 1, wherein the separator assembly (105) comprises one or more separators depending on reaction quantum.
9. The system (100) as claimed in claim 8, wherein the separator assembly (105) comprising at least two baffles (201, 202) configured for separation of the aqueous layer and the organic layer by overflow mechanism.
10. The system (100) as claimed in claim 9, wherein the separator assembly (105) is a pressure generated overflow-separator.
11. The system (100) as claimed in claim 10, wherein the separator assembly (105) is configured for:
directing the separated aqueous layer to a wastewater tank (107) from a bottom portion the separator assembly (105); and transferring a separated crude MIBT enriched organic stream overflow to a distillation system from the upper portion of the separator assembly (105).

12. The system (100) as claimed in claim 11, wherein the separator assembly (105) is connected with at least one levelling pump (203).

13. The system (100) as claimed in claim 1, comprising an internal inspection tank (106) for checking of the MIBT before storing in the MIBT storage tank (108).

14. The system (100) as claimed in claim 1, wherein the system is configured to obtain a 35-40% yield of m-isobutyl toluene (MIBT) compound.
Dated this 02nd Day of August 2022

Priyank Gupta
Agent for the Applicant
IN/PA-1454