Process of producing ethyl acetate with at least 95 WT% purity

Abstract

A method of producing ethyl acetate with at least 95 wt% purity, the method may comprise a first round, and a second round. The first round may comprise: forming a reaction product comprising an aqueous solution of ethyl acetate, an organic solvent, and acid catalyst through an esterification reaction in a reactor; forming an azeotropic mixture in form of gas comprising the organic solvent and water; accumulating the azeotropic mixture in form of gas in a first condenser; forming a two- phase liquid mixture by cooling the accumulated azeotropic mixture in form of gas; separating the organic phase of the two-phase liquid mixture from the aqueous phase of the two-phase liquid mixture using a phase-separator; removing the aqueous phase of the two-phase liquid mixture from the phase-separator; refluxing the organic phase of the two phase liquid mixture from the phase- separator to the reactor and the first distillation column. The second round may comprise: transferring the accumulated dehydrated reaction product to the evaporator; forming an evaporated mixture comprising the organic solvent and ethyl acetate by heating the accumulated dehydrated reaction product; feeding a second distillation column with the evaporated mixture; feeding a second condenser with the evaporated organic solvent; forming organic solvent in a form of liquid by cooling the evaporated organic solvent; and forming ethyl acetate in a form of liquid with at least 95 wt% purity comprises heating a downstream liquid mixture comprising the organic solvent and ethyl acetate.

Description

PROCESS OF PRODUCING ETHYL ACETATE WITH AT LEAST 95 WT%PURITYTECHNICAL FIELD

[0001] The present disclosure is generally related to an exemplary method for producing and purifying ethyl acetate, and more particularly to an exemplary method for producing highly pure ethyl acetate by removing water using azeotropic mixture comprising an exemplary organic solvent and water.BACKGROUND

[0002] Ethyl acetate, an organic solvent that is safe for the environment and is used in paint and glue, eliminates the need for aromatic compounds in the workplace. The Fischer esterification method, the acetaldehyde-Tishchenko reaction, and the addition of acetic acid to ethylene are the three industrial processes that may be used to produce ethyl acetate.

[0003] In Fisher's method, the continuous reaction-distillation method or the batch reaction-distillation method is used. In the reaction-distillation method, the reactants are mixed, and boiled in a stirred reactor, and distilled. The obtained crude product is an azeotropic mixture of ethanol, ethyl acetate, and water. The separation of this azeotropic mixture requires several stages of purification with distillation systems, molecular sieve adsorption, solvent separation, etc., which is expensive. The reaction-distillation method is a continuous method of producing ethyl acetate that uses a distillation column as a reactor. The purity of the product from said method is high, and the product does not need further purification, but the required equipment for this method is complicated, and its operation is difficult. It also has a high energy cost. Therefore, there is a need to design of a method to produce highly pure ethyl acetate without requirement of complicated equipment or materials.SUMMARY

[0004] This summary is intended to provide an overview of the subject matter of the present disclosure, and is not intended to identify essential elements or key elements of the subject matter, nor is it intended to be used to determine the scope of the claimed implementations. Its sole purpose is to present some concepts of one or more exemplary aspects in a simplified form as a prelude to the more detailed description that is presented later. The proper scope of the present disclosure may be ascertained from the claims set forth below in view of the detailed description below and the drawings.

[0005] One or more exemplary embodiments describe an exemplary method for producing high purity ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising methyl tert-butyl ether. In an exemplary embodiment, an exemplary method may comprise an exemplary first round, and an exemplary second round. In an exemplary embodiment, an exemplary first round may comprise: forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water), methyl tert-butyl ether, and an exemplary acid catalyst through an esterification reaction; and dehydrating an exemplary reaction product. In an exemplary embodiment, forming an exemplary reaction product may comprise mixing methyl tert-butyl ether, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) in an exemplary reactor at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm. In an exemplary embodiment, dehydrating an exemplary reaction product may comprise: forming an exemplary azeotropic mixture in form of gas comprising methyl tert-butyl ether and water with a molar ratio between 84:16 and 3:1 (methyl tert-butyl ether: water) in an exemplary first distillation column by heating an exemplary reaction product to a temperature level between 70 °C and 105 °C, and a pressurelevel between 1 atm and 4 atm; accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser; forming an exemplary two-phase liquid mixture comprising an exemplary organic phase comprising methyl tert-butyl ether, and an exemplary aqueous phase comprising water by cooling an exemplary accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 90 °C, and a pressure level between 1 atm and 3 atm in an exemplary first condenser; separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture using an exemplary phase- separator; removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase-separator; refluxing an exemplary organic phase of an exemplary two phase liquid mixture from an exemplary phase-separator to an exemplary reactor and an exemplary first distillation column; and accumulating an exemplary dehydrated reaction product in an exemplary reactor. In an exemplary embodiment, an exemplary second round may comprise: transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator; forming an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate by heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm in an exemplary evaporator; feeding an exemplary second distillation column with an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate; feeding an exemplary second condenser with the evaporated methyl tert-butyl ether; forming methyl tert-butyl ether in a form of liquid by cooling the evaporated methyl tert-butyl ether to a temperature level between 0 °C and 50 °C, and at a pressure level of 1 atm; extracting methyl tert-butyl ether in a form of liquid from an exemplary second condenser; re-feeding the top section of an exemplary second distillation column with methyl tert-butyl ether in a form of liquid; transferring an exemplary downstream liquid mixture to an exemplary re -boiler;forming ethyl acetate in a form of liquid with at least 95 wt% purity and an exemplary boil- up vapour mixture comprising ethyl acetate and methyl tert-butyl ether by heating an exemplary downstream liquid mixture to a temperature level between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm; extracting ethyl acetate with at least 95 wt% purity in a form of liquid from an exemplary re -boiler; and re-feeding the bottom section of an exemplary second distillation column with an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether.

[0006] In an exemplary embodiment, in an exemplary method for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising methyl tert-butyl ether, the top section of an exemplary first distillation column has a temperature level between 50 °C and 91 °C, and a pressure level between 1 atm and 3 atm, the top section of an exemplary second distillation column has a temperature level between 50 °C and 60 °C, and a pressure level of 1 atm, and the bottom section of an exemplary second distillation column has a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm. In an exemplary embodiment, forming ethyl acetate through esterification reaction may be coincides with forming an exemplary azeotropic mixture comprising methyl tert-butyl ether and water. In an exemplary embodiment, forming ethyl acetate through the esterification reaction may be a continuous reaction by removing water from an exemplary reaction product based on the Le Chatelier's principle.

[0007] One or more exemplary embodiments describe an exemplary method for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising dichloromethane. In an exemplary embodiment, an exemplary method may comprise an exemplary first round, and an exemplary second round. In an exemplary embodiment, an exemplary first round may comprise: forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethylacetate: water), dichloromethane, and an exemplary acid catalyst through an esterification reaction; and dehydrating an exemplary reaction product. In an exemplary embodiment, forming an exemplary reaction product may comprise mixing dichloromethane, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) in an exemplary reactor at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm. In an exemplary embodiment, dehydrating an exemplary reaction product may comprise: forming an exemplary azeotropic mixture in form of gas comprising dichloromethane and water with a molar ratio between 81:18 and 61:39 (dichloromethane: water) in an exemplary first distillation column by heating an exemplary reaction product to a temperature level between 70 °C and 120 °C, and a pressure level between 1 atm and 4 atm; accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser; forming an exemplary two-phase liquid mixture comprising an exemplary organic phase comprising dichloromethane, and an exemplary aqueous phase comprising water by cooling an exemplary accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 105 °C, and a pressure level between 1 atm and 3 atm in an exemplary first condenser; separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture using an exemplary phase- separator; removing an exemplary aqueous phase of an exemplary two- phase liquid mixture from an exemplary phase-separator; refluxing an exemplary organic phase of an exemplary two phase liquid mixture from an exemplary phase-separator to an exemplary reactor and an exemplary first distillation column; and accumulating an exemplary dehydrated reaction product in an exemplary reactor. In an exemplary embodiment, an exemplary second round may comprise: transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator; forming an exemplary evaporated mixturecomprising dichloromethane and ethyl acetate by heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm in an exemplary evaporator; feeding an exemplary second distillation column with an exemplary evaporated mixture comprising dichloromethane and ethyl acetate; feeding an exemplary second condenser with the evaporated dichloromethane; forming dichloromethane in a form of liquid by cooling the evaporated dichloromethane to a temperature level between 10 °C and 40 °C, and at a pressure level of 1 atm; extracting dichloromethane in a form of liquid from an exemplary second condenser; re-feeding the top section of an exemplary second distillation column with dichloromethane in a form of liquid; transferring an exemplary downstream liquid mixture to an exemplary re-boiler; forming ethyl acetate in a form of liquid with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane by heating an exemplary downstream liquid mixture to a temperature level between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm; extracting ethyl acetate with at least 95 wt% purity in a form of liquid from an exemplary re-boiler; and re-feeding the bottom section of an exemplary second distillation column with an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane .

[0008] In an exemplary embodiment, in an exemplary method for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising dichloromethane, the top section of an exemplary first distillation column has a temperature level between 57 °C and 105 °C, and a pressure level between 1 atm and 3 atm, the top section of an exemplary second distillation column has a temperature level between 39 °C and 42 °C, and a pressure level of 1 atm, and the bottom section of an exemplary second distillation column has a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm. In an exemplary embodiment, forming ethyl acetate through esterification reaction maybe coincides with forming an exemplary azeotropic mixture comprising dichloromethane and water. In an exemplary embodiment, forming ethyl acetate through the esterification reaction may be a continuous reaction by removing water from an exemplary reaction product based on the Le Chatelier's principle.

[0009] This Summary may introduce a number of concepts in a simplified format; the concepts are further disclosed within the “Detailed Description” section. This Summary is not intended to configure essential / key features of the claimed subject matter, nor is intended to limit the scope of the claimed subject matter.BRIEF DESCRIPTION OF THE DRAWINGS

[0010] The novel features which are believed to be characteristic of the present disclosure, as to its structure, organization, use and method of operation, together with further objectives and advantages thereof, will be better understood from the following drawings in which an exemplary embodiment will now be illustrated by way of example. It is expressly understood, however, that the drawings are for the purpose of illustration and description only and are not intended as a definition of the limits of one or more exemplary embodiments. One or more exemplary embodiments will now be described by way of example in association with the accompanying drawings in which:

[0011] FIG. 1 is a schematic process flow diagram (pfd) of producing high-purity ethyl acetate, consistent with one or more exemplary embodiments of the present disclosure;

[0012] FIG. 2A illustrates flowcharts of an exemplary first round for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure; and FIG. 2B illustrates an exemplary method of step for dehydrating an exemplary reaction product, consistent with one or more exemplary embodiments of the present disclosure;

[0013] FIG. 3 illustrates flowcharts of exemplary second round for producing ethyl acetate with at least 95 wt% purity using an exemplary solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure;

[0014] FIG. 4A illustrates flowcharts of an exemplary first round for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure; and FIG. 4B illustrates an exemplary method of step for dehydrating an exemplary reaction product, consistent with one or more exemplary embodiments of the present disclosure;

[0015] FIG. 5 illustrates flowcharts of exemplary second round for producing ethyl acetate with at least 95 wt% purity using an exemplary solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure;

[0016] FIG. 6 illustrates diagram of Gas Chromatography-Flame ionization detection (GC-FID) analysis for ethyl acetate produced through an exemplary method described in the present disclosure using an exemplary solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure; and

[0017] FIG. 7 illustrates diagram of GC-FID analysis for ethyl acetate produced through an exemplary method described in the present disclosure using an exemplary solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure.DETAILED DESCRIPTION

[0018] In the following detailed description, numerous specific details are set forth by way of examples to provide a thorough understanding of the relevant teachings related to exemplary embodiments. However, it should be apparent that the present teachings may be practiced without such details. In other instances, well known methods, procedures,components, and / or circuitry have been described at a relatively high-level, without detail, in order to avoid unnecessarily obscuring aspects of the present teachings.

[0019] The following detailed description is presented to enable a person skilled in the art to make and use the methods and devices disclosed in one or more exemplary embodiments. For purposes of explanation, specific nomenclature is set forth to provide a thorough understanding of one or more exemplary embodiments. However, it will be apparent to one skilled in the art that these specific details are not required to practice the disclosed exemplary embodiments. Descriptions of specific exemplary embodiments are provided only as representative examples. Various modifications to exemplary implementations will be plain to one skilled in the art, and the general principles defined herein may be applied to other implementations and applications without departing from the scope of one or more exemplary embodiments. The present disclosure is not intended to be limited to the implementations shown, but is to be accorded the widest possible scope consistent with the principles and features disclosed herein.

[0020] An exemplary embodiment is directed to an exemplary method for producing ethyl acetate with at least 95 wt% purity. Ethyl acetate is a chemical compound with the molecular formula C4H8O2, also known as ethyl ethanoate. Ethyl acetate is known as a fruity- smelling, clear liquid with no colour. The primary method for producing ethyl acetate is the esterification reaction between acetic acid and ethanol in the presence of an acid catalyst, which results in producing water as a by-product. Therefore, it is important to isolate ethyl acetate from water to achieve high-purity ethyl acetate. Azeotropes are mixtures of a minimum of two liquids that have the same concentration in both the liquid and vapour phases. Raoult's Law is not applicable to azeotropes. This indicates that these mixes deviate from Raoult's Law and are not perfect solutions. One component in azeotropic mixture has a boiling point that is either greater or lower than that of another component. Components inthese combinations display the same mole percentage in both the liquid and vapor phases.Because of this, fractional distillation cannot separate them. The solution of an azeotropic mixture boils at a fixed temperature. Fractional distillation cannot be used to separate the components of an azeotropic mixture. The azeotropic solution of ethyl acetate and water, for instance, boils at 70.3 °C and cannot be separated by fractional distillation because the mole fraction of ethyl acetate is the same at the liquid phase and vapour phase and the mole fraction of water is also the same at the liquid phase and vapour phase. The components of azeotropic mixtures are separated using another azeotrope. For instance, it is quite challenging to produce pure ethyl acetate from an acetic acid, ethanol and water combination. Methyl tertbutyl ether and water combine to form an azeotrope that boils at 55.6 °C, and at atmospheric pressure. Dichloromethane and water combine to form an azeotrope that boils at 58.2 °C, and at atmospheric pressure. In order to separate water from the reaction product of the esterification reaction and extract almost pure ethyl acetate from the distillation column, a solvent such as methyl tert-butyl ether or dichloromethane is added to the combination of ethyl acetate and water as an entertainer (solvent).

[0021] FIG. 1 is a schematic process flow diagram (pfd) 100 of producing high-purity ethyl acetate, consistent with one or more exemplary embodiments of the present disclosure. Exemplary pfd 100 may include an exemplary reactor 102, an exemplary first distillation column 104, an exemplary first condenser 106, an exemplary phase- separator 108, an exemplary evaporator 110, an exemplary second distillation column 112, an exemplary second condenser 114, and an exemplary re-boiler 116.

[0022] “High-purity ethyl acetate” may refer to at least 95% ethyl acetate by weight. “Reactor” may refer to an enclosed container where a chemical reaction takes place. “Distillation column” may refer to an apparatus or vessel that separates one or more feed streams into two or more exit streams, each of which has component concentrations that aredifferent from those of the feed stream(s). The components are redistributed between the liquid and vapor phases by vaporization and condensation to achieve separation. The distillate receiver, re -boiler, vacuum pump, steam jet, and any related recovery system are all considered components of a distillation column. “Condenser” may refer to any device for transferring heat that liquefies vapors by removing their latent heat from vaporization. Condensers of this type may include but are not limited to shell and tube, coil, surface, or contact types, among others. “Phase- separator” may refer to an instrument used to separate the components of an oil, gas, and water well stream. For instance, entrained fluids from natural gas streams are separated and collected using a gas-liquid separator. Two-phase and three-phase-separators are the two basic types of phase-separators. “Re-boiler” may refer to a heat exchanger that are commonly employed to supply heat to the bottom product of the distillation columns. To drive the distillation separation, they boil the liquid at the bottom of a distillation column to produce vapours that are then reintroduced into the column. The condenser at the top of the column removes the heat that the re-boiler at the bottom of the column supplies. A well-functioning re-boiler is essential for efficient distillation. The reboiler is the source of the vapor that powers the separation in a distillation column. A liquid stream is fed into the re-boiler from the bottom of the column, and it might evaporate all or part of the stream. Usually, the heat needed for vaporization comes from steam. In an exemplary embodiment, an exemplary re-boiler may be selected from the group consisting of Kettle Type re-boiler, Thermosyphon re -boiler, fired re -boiler, and Forced circulation reboiler.

[0023] In an exemplary embodiment, an exemplary method for preparing an exemplary ethyl acetate with at least 95 wt% purity may consist of an exemplary first round and an exemplary second round. In an exemplary embodiment, in an exemplary method for producing an exemplary ethyl acetate with at least 95 wt% purity, an exemplary second roundmay be performed after finishing an exemplary first round. In an exemplary embodiment, an exemplary first round may be performed to produce an exemplary aqueous solution of ethyl acetate and then producing an exemplary azeotropic mixture comprising an exemplary organic solvent and water, and finally separating an exemplary organic solvent from water.

[0024] Referring to the figures, FIG. 2A and FIG. 3 illustrate flowcharts of an exemplary first round 200 and an exemplary second round 300, respectively for preparing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure. Referring to the figures, FIG. 2A illustrates flowcharts of an exemplary first round 200 for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary first round 200 may comprise: forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, an exemplary organic solvent comprising methyl tert-butyl ether, and an exemplary acid catalyst (step 202); and dehydrating an exemplary reaction product (step 204).

[0025] In further detail with respect to step 202, step 202 may include forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, an exemplary organic solvent comprising methyl tert-butyl ether, and an exemplary acid catalyst. In an exemplary embodiment, forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, methyl tert-butyl ether, and an exemplary acid catalyst may include mixing methyl tert-butyl ether, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm. In an exemplaryembodiment, mixing methyl tert-butyl ether, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1 :0.001 : 1 : 1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and 4 atm may include adding acetic acid, ethanol, methyl tert-butyl ether, and an exemplary acid catalyst with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70°C and 105 °C, and at a pressure level between 1 atm and 4 atm. For example, adding acetic acid, ethanol, methyl tert-butyl ether, and an exemplary acid catalyst with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and 4 atm may include adding acetic acid, ethanol, methyl tert-butyl ether, and an exemplary acid catalyst comprising sulphuric acid with a molar ratio of 0.1 :0.001 : 1 : 1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and 4 atm. In an exemplary embodiment, mixing exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1 :0.001 : 1 : 1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and 4 atm may result in forming an exemplary aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water) through an esterification reaction. “Acid catalyst” may refer to any catalyst that prepare proton for the esterification reaction such as sulphuric acid, hydrochloric acid, derivatives of sulphuric acid, methanesulfonic acid, and p-toluenesulfonic acid. In an exemplary embodiment, acetic acid may have a purity of 99.9 %wt. In exemplary embodiment, ethanol may have a puritybetween 90 %wt and 99.9 %wt. In exemplary embodiment, sulphuric acid may have a purity of 98 %wt. In an exemplary embodiment, an exemplary reactor 102 may be selected from the group consisting of batch reactor, continuous stirred-tank reactor, plug flow reactor, fixed bed reactor, tabular reactor, moving bed reactor, and fluidized bed reactor.

[0026] In further detail with respect to step 204, step 204 may include dehydrating an exemplary reaction product. In an exemplary embodiment, details of step 204 for dehydrating an exemplary reaction product are described in context of elements presented in FIG. 2B. FIG. 2B illustrates an exemplary method of step 204 for dehydrating an exemplary reaction product, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary method of step 204 may comprise: forming an exemplary azeotropic mixture in form of gas comprising methyl tert-butyl ether and water in an exemplary first distillation column (step 206); accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser (step 208); forming an exemplary two-phase liquid mixture in an exemplary first condenser (step 210); separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture (step 212); removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase- separator (step 214); and returning an exemplary organic phase comprising methyl tert-butyl ether to an exemplary reactor and an exemplary first distillation column (step 216).

[0027] In further detail with respect to step 206, step 206 may include forming an exemplary azeotropic mixture in form of gas comprising methyl tert-butyl ether and water in an exemplary first distillation column 104. In an exemplary embodiment, forming an exemplary azeotropic mixture in form of gas comprising methyl tert-butyl ether and water in an exemplary first distillation column 104 may include heating an exemplary reaction product to a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and4 atm, that may result in forming an exemplary azeotropic mixture with a molar ratio between84:16 and 3:1 (methyl tert-butyl ether: water). In an exemplary embodiment, the top section of an exemplary first distillation column 104 may have a temperature level between 50 °C and 91 °C, and a pressure level between 1 atm and 3 atm. Forming ethyl acetate through esterification reaction may be coincides with forming an exemplary azeotropic mixture comprising methyl tert-butyl ether and water. In an exemplary embodiment, forming ethyl acetate may be a continuous reaction process by removing water from an exemplary reaction product based on the Le Chatelier's principle.

[0028] In further detail with respect to step 208, step 208 may include accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser 106. In an exemplary embodiment, accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser 106 may include transferring an exemplary azeotropic mixture in form of gas to an exemplary first condenser 106, therefore, after transferring an exemplary azeotropic mixture in form of gas to an exemplary first condenser 106, an exemplary first condenser 106 may be filled with an exemplary azeotropic mixture in form of gas. In an exemplary embodiment, an exemplary first condenser 106 may be selected from the group consisting of air-cooled condenser, water-cooled condenser, and evaporative condenser. In an exemplary embodiment, cooling water with a temperature level between 10 °C and 40 °C may be flowed to an exemplary first condenser 106 to cool an exemplary azeotropic mixture.

[0029] In further detail with respect to step 210, step 210 may include forming an exemplary two-phase liquid mixture in an exemplary first condenser 106. In an exemplary embodiment, forming an exemplary two-phase liquid mixture in an exemplary first condenser 106 may include cooling an exemplary accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 90 °C, and at a pressure level between 1 atm and 3 atm in an exemplary first condenser 106. In an exemplary embodiment, an exemplary two-phaseliquid mixture may comprise an exemplary organic phase comprising methyl tert-butyl ether, and an exemplary aqueous phase comprising water.

[0030] In further detail with respect to step 212, step 212 may include separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture. In an exemplary embodiment, separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture may include transferring an exemplary two-phase liquid mixture to an exemplary phase-separator 108, therefore, after transferring an exemplary two-phase liquid mixture to an exemplary phase- separator 108, an exemplary phase-separator 108 may be filled with an exemplary two-phase liquid mixture, and then, an exemplary aqueous phase comprising water may be positioned at the lower section of an exemplary phase-separator 108 and an exemplary organic phase comprising methyl tert-butyl ether may be positioned at the upper section of an exemplary phaseseparator 108. In other words, an exemplary organic phase comprising methyl tert-butyl ether may be positioned on a surface of an exemplary aqueous phase comprising water.

[0031] In further detail with respect to step 214, step 214 may include removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase-separator 108. In an exemplary embodiment, removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase-separator 108 may include discharging an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108.

[0032] In further detail with respect to step 216, step 216 may include returning an exemplary organic phase comprising methyl tert-butyl ether to an exemplary reactor and an exemplary first distillation column. In an exemplary embodiment, returning an exemplary organic phase comprising methyl tert-butyl ether to an exemplary reactor 102 and anexemplary first distillation column 104 may include refluxing an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108 to an exemplary reactor 102 and an exemplary first distillation column 104. In an exemplary embodiment, refluxing an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108 to an exemplary reactor 102 and an exemplary first distillation column 104 may include refluxing an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108 to an exemplary reactor 102 and an exemplary first distillation column 104 using an exemplary pump, therefor, after refluxing methyl tert-butyl ether to an exemplary reactor 102 and an exemplary first distillation column 104, methyl tert-butyl ether may be used to form an exemplary azeotropic mixture comprising water and methyl tert-butyl ether during the esterification reaction in an exemplary reactor 102. In an exemplary embodiment, the refluxed methyl tert-butyl ether may be transferred to an exemplary first distillation column 104 and an exemplary reactor 102. In an exemplary embodiment, after finishing esterification reaction in an exemplary reactor 102, an exemplary dehydrated reaction product may be accumulated in an exemplary reactor 102. It should be noted that an exemplary process of producing ethyl acetate in an exemplary reactor 102 may be carried out simultaneously with producing an exemplary azeotropic mixture comprising methyl tertbutyl ether and water. In other words, an exemplary azeotropic mixture of water and methyl tert-butyl ether is produced as long as ethyl acetate and water are produced in the reactor 102.

[0033] Referring to the figures, FIG. 3 illustrates flowcharts of exemplary second round 300 for producing ethyl acetate with at least 95 wt% purity using an exemplary solvent comprising methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary second round 300 may comprise: transferring an exemplary accumulated dehydrated reaction product to anexemplary evaporator (step 302); forming an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate in an exemplary evaporator (step 304); feeding an exemplary second distillation column with an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate (step 306); extracting the evaporated methyl tertbutyl ether from the top section of an exemplary second distillation column and transferring to an exemplary second condenser (step 308); cooling the extracted methyl tert-butyl ether in an exemplary second condenser (step 310); extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column and transferring to an exemplary re -boiler (step 312); and forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether (step 314).

[0034] In further detail with respect to step 302, step 302 may include transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator. In an exemplary embodiment, transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator 110 may include feeding an exemplary evaporator 110 with an exemplary accumulated dehydrated reaction product, therefor, an exemplary evaporator 110 may be filled with an exemplary accumulated dehydrated reaction product.

[0035] In further detail with respect to step 304, step 304 may include forming an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate in an exemplary evaporator 110. In an exemplary embodiment, forming an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate in an exemplary evaporator 110 may include heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm in an exemplary evaporator 110. In an exemplary embodiment, heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressurelevel between 1 atm and 1.2 atm in an exemplary evaporator 110 may result in separating an exemplary acid catalyst from an exemplary accumulated dehydrated reaction product. In an exemplary embodiment, an exemplary acid catalyst may be discharged from an exemplary evaporator 110 after heating an exemplary accumulated dehydrated reaction product.

[0036] In further detail with respect to step 306, step 306 may include feeding an exemplary second distillation column 112 with an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate. In an exemplary embodiment, feeding an exemplary second distillation column 112 with an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate may include transferring an exemplary evaporated mixture comprising methyl tert-butyl ether and ethyl acetate to an exemplary second distillation column 112, that may result in forming the evaporated methyl tert-butyl ether at the top section of an exemplary second distillation column 112, and an exemplary downstream liquid mixture comprising the mixture of methyl tert-butyl ether and ethyl acetate at the bottom section of an exemplary second distillation column 112. In an exemplary embodiment, the top section of an exemplary second distillation column 112 may have a temperature level between 50 °C and 60 °C, and a pressure level of 1 atm. In an exemplary embodiment, the bottom section of an exemplary second distillation column 112 may have a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm.In further detail with respect to step 308, step 308 may include extracting the evaporated methyl tert-butyl ether from the top section of an exemplary second distillation column and transferring to an exemplary second condenser. In an exemplary embodiment, extracting the evaporated methyl tert-butyl ether from the top section of an exemplary second distillation column 112 and transferring to an exemplary second condenser 114 may include feeding an exemplary second condenser 114 with the evaporated methyl tert-butyl ether from the top section of exemplary second distillation column 112.

[0037] In further detail with respect to step 310, step 310 may include cooling the extracted methyl tert-butyl ether in an exemplary second condenser. In an exemplary embodiment, cooling the extracted methyl tert-butyl ether in an exemplary second condenser 114 may include cooling the extracted methyl tert-butyl ether to a temperature level between 0 °C and 50 °C, and at a pressure level of 1 atm in an exemplary second condenser 114. In an exemplary embodiment, the cooled methyl tert-butyl ether may be returning back to an exemplary second distillation column 112 or accumulating to an exemplary storage.

[0038] In further detail with respect to step 312, step 312 may include extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column and transferring to an exemplary re -boiler. In an exemplary embodiment, extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column 112 and transferring to an exemplary re-boiler 116 may include feeding an exemplary re-boiler 116 with an exemplary downstream liquid mixture comprising methyl tert-butyl ether and ethyl acetate.

[0039] In further detail with respect to step 314, step 314 may include forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether. In an exemplary embodiment, forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether may include heating an exemplary downstream liquid mixture to a temperature level between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm, that may result in separating ethyl acetate from an exemplary downstream liquid mixture. In an exemplary embodiment an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether may be returning back to an exemplary second distillation column 112. In an exemplary embodiment, a liquid mixture comprising ethyl acetate with atleast 95 wt% purity may be accumulating to an exemplary storage. In an exemplary embodiment, returning back an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether to an exemplary second distillation column 112 may include reboiling an exemplary boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether by heating to a temperature level between 77 °C and 91 °C.

[0040] Referring to the figures, FIG. 4A and FIG. 5 illustrate flowcharts of an exemplary first round 400 and an exemplary second round 500, respectively for preparing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure. Referring to the figures, FIG. 4A illustrates flowcharts of an exemplary first round 400 for producing ethyl acetate with at least 95 wt% purity using an exemplary organic solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary first round 400 may comprise: forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, an exemplary organic solvent comprising dichloromethane, and an exemplary acid catalyst (step 402); and dehydrating an exemplary reaction product (step 404).

[0041] In further detail with respect to step 402, step 402 may include forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, an exemplary organic solvent comprising dichloromethane, and an exemplary acid catalyst. In an exemplary embodiment, forming an exemplary reaction product comprising an exemplary aqueous solution of ethyl acetate, dichloromethane, and an exemplary acid catalyst may include mixing dichloromethane, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm. In an exemplary embodiment, mixingdichloromethane, an exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm may include adding acetic acid, ethanol, dichloromethane, and an exemplary acid catalyst with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70°C and 120 °C, and at a pressure level between 1 atm and 4 atm. For example, adding acetic acid, ethanol, dichloromethane, and an exemplary acid catalyst with a molar ratio of 0.1:0.001:1: 1 to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm may include adding acetic acid, ethanol, dichloromethane, and an exemplary acid catalyst comprising sulphuric acid with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) to an exemplary reactor 102 while mixing using stirrer of an exemplary reactor 102 at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm. In an exemplary embodiment, mixing exemplary acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) in an exemplary reactor 102 at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm may result in forming an exemplary aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water) through an esterification reaction. “Acid catalyst” may refer to any catalyst that prepare proton for the esterification reaction such as sulphuric acid, hydrochloric acid, derivatives of sulphuric acid, methanesulfonic acid, and p-toluenesulfonic acid. In an exemplary embodiment, acetic acid may have a purity of 99.9 %wt. In exemplary embodiment, ethanol may have a purity between 90 %wt and 99.9 %wt. In exemplary embodiment, sulphuric acid may have a purity of 98 %wt. In an exemplary embodiment, anexemplary reactor 102 may be selected from the group consisting of batch reactor, continuous stirred-tank reactor, plug flow reactor, fixed bed reactor, tabular reactor, moving bed reactor, and fluidized bed reactor.

[0042] In further detail with respect to step 404, step 404 may include dehydrating an exemplary reaction product. In an exemplary embodiment, details of step 404 for dehydrating an exemplary reaction product are described in context of elements presented in FIG. 4B. FIG. 4B illustrates an exemplary method of step 404 for dehydrating an exemplary reaction product, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary method of step 404 may comprise: forming an exemplary azeotropic mixture in form of gas comprising dichloromethane and water in an exemplary first distillation column (step 406); accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser (step 408); forming an exemplary two-phase liquid mixture in an exemplary first condenser (step 410); separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two- phase liquid mixture (step 412); removing an exemplary aqueous phase of an exemplary two- phase liquid mixture from an exemplary phase- separator (step 414); and returning an exemplary organic phase comprising dichloromethane to an exemplary reactor and an exemplary first distillation column (step 416).

[0043] In further detail with respect to step 406, step 406 may include forming an exemplary azeotropic mixture in form of gas comprising dichloromethane and water in an exemplary first distillation column. In an exemplary embodiment, forming an exemplary azeotropic mixture in form of gas comprising dichloromethane and water in an exemplary first distillation column 104 may include heating an exemplary reaction product to a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm, that may result in forming an exemplary azeotropic mixture with a molar ratio between84:18 and 61:39 (dichloromethane: water). In an exemplary embodiment, the top section of an exemplary first distillation column 104 may have a temperature level between 57 °C and105 °C, and a pressure level between 1 atm and 3 atm. Forming ethyl acetate through esterification reaction may be coincides with forming an exemplary azeotropic mixture comprising dichloromethane and water. In an exemplary embodiment, forming ethyl acetate may be a continuous reaction process by removing water from an exemplary reaction product based on the Le Chatelier's principle.

[0044] In further detail with respect to step 408, step 408 may include accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser. In an exemplary embodiment, accumulating an exemplary azeotropic mixture in form of gas in an exemplary first condenser 106 may include transferring an exemplary azeotropic mixture in form of gas to an exemplary first condenser 106, therefore, after transferring an exemplary azeotropic mixture in form of gas to an exemplary first condenser 106, an exemplary first condenser 106 may be filled with an exemplary azeotropic mixture in form of gas. In an exemplary embodiment, an exemplary first condenser 106 may be selected from the group consisting of air-cooled condenser, water-cooled condenser, and evaporative condenser. In an exemplary embodiment, cooling water with a temperature level between 10 °C and 40 °C may be flowed to an exemplary first condenser 106 to cool an exemplary azeotropic mixture.

[0045] In further detail with respect to step 410, step 410 may include forming an exemplary two-phase liquid mixture in an exemplary first condenser. In an exemplary embodiment, forming an exemplary two-phase liquid mixture in an exemplary first condenser106 may include cooling an exemplary accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 90 °C, and at a pressure level between 1 atm and 3 atm in an exemplary first condenser 106. In an exemplary embodiment, an exemplary two-phaseliquid mixture may comprise an exemplary organic phase comprising dichloromethane, and an exemplary aqueous phase comprising water.

[0046] In further detail with respect to step 412, step 412 may include separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture. In an exemplary embodiment, separating an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary aqueous phase of an exemplary two-phase liquid mixture may include transferring an exemplary two-phase liquid mixture to an exemplary phase-separator 108, therefore, after transferring an exemplary two-phase liquid mixture to an exemplary phase- separator 108, an exemplary phase-separator 108 may be filled with an exemplary two-phase liquid mixture, and then, an exemplary aqueous phase comprising water may be positioned at the upper section of an exemplary phase-separator 108 and an exemplary organic phase comprising dichloromethane may be positioned at the lower section of an exemplary phase-separator 108. In other words, an exemplary aqueous phase comprising water may be positioned on a surface of an exemplary organic phase comprising dichloromethane.

[0047] In further detail with respect to step 414, step 414 may include removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase-separator 108. In an exemplary embodiment, removing an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase-separator 108 may include discharging an exemplary aqueous phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108.

[0048] In further detail with respect to step 416, step 416 may include returning an exemplary organic phase comprising dichloromethane to an exemplary reactor 102 and an exemplary first distillation column 104. In an exemplary embodiment, returning an exemplary organic phase comprising dichloromethane may include refluxing an exemplaryorganic phase of an exemplary two-phase liquid mixture from an exemplary phase-separator108 to an exemplary reactor 102 and an exemplary first distillation column 104. In an exemplary embodiment, refluxing an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108 to an exemplary reactor 102 and an exemplary first distillation column 104 may include refluxing an exemplary organic phase of an exemplary two-phase liquid mixture from an exemplary phase- separator 108 to an exemplary reactor 102 and an exemplary first distillation column 104 using an exemplary pump, therefor, after refluxing dichloromethane to an exemplary reactor 102 and an exemplary first distillation column 104, dichloromethane may be used to form an exemplary azeotropic mixture comprising water and dichloromethane during the esterification reaction in an exemplary reactor 102. In an exemplary embodiment, the refluxed dichloromethane may be transferred to an exemplary first distillation column 104 and an exemplary reactor 102. In an exemplary embodiment, after finishing esterification reaction in an exemplary reactor 102, an exemplary dehydrated reaction product may be accumulated in an exemplary reactor 102. It should be noted that an exemplary process of producing ethyl acetate in an exemplary reactor 102 may be carried out simultaneously with producing an exemplary azeotropic mixture comprising dichloromethane and water. In other words, an exemplary azeotropic mixture of water and dichloromethane may be produced as long as ethyl acetate and water are produced in the reactor 102.

[0049] Referring to the figures, FIG. 5 illustrates flowcharts of exemplary second round 500 for producing ethyl acetate with at least 95 wt% purity using an exemplary solvent comprising dichloromethane, consistent with one or more exemplary embodiments of the present disclosure. In an exemplary embodiment, an exemplary second round 500 may comprise: transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator (step 502); forming an exemplary evaporated mixture comprisingdichloromethane and ethyl acetate in an exemplary evaporator (step 504); feeding an exemplary second distillation column with an exemplary evaporated mixture comprising dichloromethane and ethyl acetate (step 506); extracting the evaporated dichloromethane from the top section of an exemplary second distillation column and transferring to an exemplary second condenser (step 508); cooling the extracted dichloromethane in an exemplary second condenser (step 510); extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column and transferring to an exemplary re-boiler (step 512); and forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane (step 514).

[0050] In further detail with respect to step 502, step 502 may include transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator. In an exemplary embodiment, transferring an exemplary accumulated dehydrated reaction product to an exemplary evaporator 110 may include feeding an exemplary evaporator 110 with an exemplary accumulated dehydrated reaction product, therefor, an exemplary evaporator 110 may be filled with an exemplary accumulated dehydrated reaction product.

[0051] In further detail with respect to step 504, step 504 may include forming an exemplary evaporated mixture comprising dichloromethane and ethyl acetate in an exemplary evaporator. In an exemplary embodiment, forming an exemplary evaporated mixture comprising dichloromethane and ethyl acetate in an exemplary evaporator 110 may include heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm in an exemplary evaporator 110. In an exemplary embodiment, heating an exemplary accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm in an exemplary evaporator 110 may result in separating anexemplary acid catalyst from an exemplary accumulated dehydrated reaction product. In an exemplary embodiment, an exemplary acid catalyst may be discharged from an exemplary evaporator 110 after heating an exemplary accumulated dehydrated reaction product.

[0052] In further detail with respect to step 506, step 506 may include feeding an exemplary second distillation column with an exemplary evaporated mixture comprising dichloromethane and ethyl acetate. In an exemplary embodiment, feeding an exemplary second distillation column 112 with an exemplary evaporated mixture comprising dichloromethane and ethyl acetate may include transferring an exemplary evaporated mixture comprising dichloromethane and ethyl acetate to an exemplary second distillation column 112, that may result in forming the evaporated dichloromethane at the top section of an exemplary second distillation column 112, and an exemplary downstream liquid mixture comprising the mixture of dichloromethane and ethyl acetate at the bottom section of an exemplary second distillation column 112. In an exemplary embodiment, the top section of an exemplary second distillation column 112 may have a temperature level between 39 °C and 42 °C, and a pressure level of 1 atm. In an exemplary embodiment, the bottom section of an exemplary second distillation column 112 may have a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm.

[0053] In further detail with respect to step 508, step 508 may include extracting the evaporated dichloromethane from the top section of an exemplary second distillation column and transferring to an exemplary second condenser. In an exemplary embodiment, extracting the evaporated dichloromethane from the top section of an exemplary second distillation column 112 and transferring to an exemplary second condenser 114 may include feeding an exemplary second condenser 114 with the evaporated dichloromethane from the top section of exemplary second distillation column 112.

[0054] In further detail with respect to step 510, step 510 may include cooling the extracted dichloromethane in an exemplary second condenser. In an exemplary embodiment, cooling the extracted dichloromethane in an exemplary second condenser 114 may include cooling the extracted dichloromethane to a temperature level between 0 °C and 39 °C, and at a pressure level of 1 atm in an exemplary second condenser 114. In an exemplary embodiment, the cooled dichloromethane may be returning back to an exemplary second distillation column 112 or accumulating to an exemplary storage.

[0055] In further detail with respect to step 512, step 512 may include extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column and transferring to an exemplary re-boiler. In an exemplary embodiment, extracting an exemplary downstream liquid mixture from the bottom section of an exemplary second distillation column 112 and transferring to an exemplary re-boiler 116 may include feeding an exemplary re-boiler 116 with an exemplary downstream liquid mixture.

[0056] In further detail with respect to step 514, step 514 may include forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane. In an exemplary embodiment, forming an exemplary liquid mixture comprising ethyl acetate with at least 95 wt% purity and an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane may include heating an exemplary downstream liquid mixture to a temperature level between between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm, that may result in separating ethyl acetate from an exemplary downstream liquid mixture. In an exemplary embodiment an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane may be returning back to an exemplary second distillation column 112. In an exemplary embodiment, a liquid mixture comprising ethyl acetate with at least 95 wt% purity may be accumulating to an exemplary storage. In an exemplaryembodiment, returning back an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane to an exemplary second distillation column 112 may include re-boiling an exemplary boil-up vapour mixture comprising ethyl acetate and dichloromethane by heating to a temperature level between 77 °C and 91 °C.EXAMPLES

[0057] Hereinafter, one or more exemplary embodiments will be described in further detail with reference to examples. It will be obvious to a person having ordinary skill in the art that these examples may be for illustrative purposes only and are not to be interpreted to limit the scope of one or more exemplary embodiments.Example 1: Producing ethyl acetate with at least 95 wt% purity in the industrial scale using an exemplary organic solvent comprising methyl tert-butyl ether

[0058] In this example, a procedure for preparing ethyl acetate with at least 95 wt% purity in the industrial scale using an exemplary organic solvent comprising methyl tert-butyl ether was described. For this purpose, methyl tert-butyl ether, an acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) was added to a reactor while mixing at a temperature level of 70 °C, and at a pressure level of 1.2 atmosphere (atm) and a reaction product comprising an aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water), methyl tert-butyl ether, and acid catalyst was produced. In order to dehydrate the reaction product, the reaction product was heated to a temperature level of 70 °C, and at a pressure level of 1.1 atm, and an azeotropic mixture comprising methyl tert-butyl ether and water with a molar ratio of 84:16 (methyl tert-butyl ether: water) was formed in a first distillation column. Then the azeotropic mixture was cooled to a temperature level of 30 °C in a first condenser and a two-phase liquid mixture was produced. The two-phase liquid mixture comprises an aqueous phase comprising water, and an organic phase comprising methyl tert-butyl ether. Then, the two phase of two-phase liquid mixture was separated using a phase- separator. The organic phase was returned to the first distillation column and the reactor, and the dehydrated reaction product was accumulated in the reactor over the time. The accumulated dehydrated reaction product was transferred to an evaporator. An evaporated mixture comprising methyl tert-butyl ether and ethyl acetate was formed in the evaporator by heating the accumulated dehydrated reaction product to a temperature level of 57°C, and at a pressure level of 1 atm. Then a second distillation column was fed with the evaporated mixture. The evaporated methyl tert-butyl ether was extracted from the top section of the second distillation column, The extracted methyl tert-butyl ether was cooled in a second condenser to a temperature level of 30 °C and methyl tert-butyl ether in a form of liquid was formed. The methyl tert- butyl ether was extracted from the second condenser or returned to the second distillation column. The downstream liquid mixture was transferred to a re-boiler and was heated to a temperature level of 80 °C and ethyl acetate in a form of liquid and a boil-up vapour mixture comprising methyl tert-butyl ether and ethyl acetate was produced. The ethyl acetate in a form of liquid was extracted from the re-boiler. The boil-up vapour mixture comprising methyl tert-butyl ether and ethyl acetate may be returned to the second distillation column.Example 2: Producing ethyl acetate with at least 95 wt% purity in the industrial scale using an exemplary organic solvent comprising dichloromethane

[0059] In this example, a procedure for preparing ethyl acetate with at least 95 wt% purity in the industrial scale using an exemplary organic solvent comprising dichloromethane was described. For this purpose, dichloromethane, an acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) was added to a reactor while mixing at a temperature level of 70 °C, and at a pressure level of 1.2 atmosphere (atm) and a reaction product comprising an aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water), dichloromethane, and acid catalyst was produced.In order to dehydrate the reaction product, the reaction product was heated to a temperature level of 70 °C, and at a pressure level of 1.1 atm, and an azeotropic mixture comprising dichloromethane and water with a molar ratio of 84:16 (dichloromethane: water) was formed in a first distillation column. Then the azeotropic mixture was cooled to a temperature level of 30 °C in a first condenser and a two-phase liquid mixture was produced. The two-phase liquid mixture comprises an aqueous phase comprising water, and an organic phase comprising dichloromethane. Then, the two phase of two-phase liquid mixture was separated using a phase-separator. The organic phase was returned to the first distillation column and the reactor, and the dehydrated reaction product was accumulated in the reactor. The accumulated dehydrated reaction product was transferred to an evaporator. An evaporated mixture comprising dichloromethane and ethyl acetate was formed in the evaporator by heating the accumulated dehydrated reaction product to a temperature level of 57 °C, and at a pressure level of 1 atm. The evaporated dichloromethane was extracted from the top section of the second distillation column. The extracted dichloromethane was cooled in a second condenser to a temperature level of 30 °C and dichloromethane in a form of liquid was formed. Dichloromethane was extracted from the second condenser or returned to the second distillation column. The downstream liquid mixture was transferred to a re-boiler and was heated to a temperature level of 80 °C and ethyl acetate in a form of liquid and a boil-up vapour mixture comprising dichloromethane and ethyl acetate was produced. The ethyl acetate in a form of liquid was extracted from the re-boiler. The boil-up vapour mixture comprising dichloromethane and ethyl acetate may be returned to the second distillation column.Example 3: Gas Chromatography (GC) analysis to evaluated the purity of the produced ethyl acetate through an exemplary method described in the present disclosure

[0060] For this purpose, the extracted ethyl acetate was analyzed through GC with flameionization detection (FID). The result of this analysis was showed in Table 1, and Table 2. Table 1 showed the approximate result of GC-FID analysis for ethyl acetated produced with method of the present disclosure using methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosure. Table 2 showed the approximate result of GC-FID analysis for ethyl acetate produced with method of the present disclosure using dichloromethane, consistent with one or more exemplary embodiments of the present disclosure. FIG. 6 illustrates diagram 600 of GC-FID analysis for ethyl acetate produced through an exemplary method described in the present disclosure using an exemplary solvent comprising methyl tert-butyl ether. FIG. 7 illustrates diagram 700 of GC-FID analysis for ethyl acetate produced through an exemplary method described in the present disclosure using an exemplary solvent comprising dichloromethane.Table 1: The approximate result of GC-FID analysis for ethyl acetate produced with method of the present disclosure using methyl tert-butyl ether, consistent with one or more exemplary embodiments of the present disclosureTable 2: The approximate result of GC-FID analysis for ethyl acetated produced with method of the present disclosure using dichloromethane, consistent with one or more exemplary embodiments of the present disclosure

[0061] While the foregoing has described what are considered to be the best mode and / or other examples, it is understood that various modifications may be made therein and that the subject matter disclosed herein may be implemented in various forms and examples, and that the teachings may be applied in numerous applications, only some of which have been described herein. It is intended by the following claims to claim any and all applications, modifications and variations that fall within the true scope of the present teachings.

[0062] Unless otherwise stated, all measurements, values, ratings, positions, magnitudes, sizes, and other specifications that are set forth in this specification, including in the claims that follow, are approximate, not exact. They are intended to have a reasonable range that is consistent with the functions to which they relate and with what is customary in the art to which they pertain.

[0063] The scope of protection is limited solely by the claims that now follow. That scope is intended and should be interpreted to be as broad as is consistent with the ordinary meaning of the language that is used in the claims when interpreted in light of this specification and the prosecution history that follows and to encompass all structural and functional equivalents. Notwithstanding, none of the claims are intended to embrace subject matter that fails to satisfy the requirement of Sections 101, 102, or 103 of the Patent Act, nor should they be interpreted in such a way. Any unintended embracement of such subject matter is hereby disclaimed.

[0064] Except as stated immediately above, nothing that has been stated or illustrated is intended or should be interpreted to cause a dedication of any component, step, feature, object, benefit, advantage, or equivalent to the public, regardless of whether it is or is not recited in the claims.

[0065] It will be understood that the terms and expressions used herein have the ordinary meaning as is accorded to such terms and expressions with respect to their corresponding respective areas of inquiry and study except where specific meanings have otherwise been set forth herein. Relational terms such as first and second and the like may be used solely to distinguish one entity or action from another without necessarily requiring or implying any actual such relationship or order between such entities or actions. An element proceeded by “a” or “an” does not, without further constraints, preclude the existence of additional identical elements in the process, method, article, or apparatus that comprises the element.

[0066] Unless otherwise stated, all measurements, values, ratings, positions, magnitudes, sizes, and other specifications that are set forth in this specification, are approximate, not exact. They are intended to have a reasonable range that is consistent with the functions to which they relate and with what is customary in the art to which they pertain.

[0067] It will be understood that the terms and expressions used herein have the ordinary meaning as is accorded to such terms and expressions with respect to their corresponding respective areas of inquiry and study, except where specific meanings have otherwise been set forth herein. Relational terms such as “first” and “second” and the like may be used solely to distinguish one entity or action from another without necessarily requiring or implying any actual such relationship or order between such entities or actions.

[0068] The Abstract of the Disclosure is provided to allow the reader to quickly ascertain the nature of the technical disclosure. It is submitted with the understanding that it will not be used to interpret or limit the scope or meaning of the claims. In addition, in the foregoingDetailed Description, it may be seen that various features are grouped together in various implementations. This is for purposes of streamlining the disclosure, and is not to be interpreted as reflecting an intention that the claimed implementations require more features than are expressly recited in each claim. Rather, as the following claims reflect, inventive subject matter lies in less than all features of a single disclosed implementation. Thus, the following claims are hereby incorporated into the Detailed Description, with each claim standing on its own as a separately claimed subject matter.

[0069] While various implementations have been described, the description is intended to be exemplary, rather than limiting and it will be apparent to those of ordinary skill in the art that many more implementations and implementations are possible that are within the scope of the implementations. Although many possible combinations of features are shown in the accompanying figures and discussed in this detailed description, many other combinations of the disclosed features are possible. Any feature of any implementation may be used in combination with or substituted for any other feature or element in any other implementation unless specifically restricted. Therefore, it will be understood that any of the features shown and / or discussed in the present disclosure may be implemented together in any suitable combination. Accordingly, the implementations are not to be restricted except in light of the attached claims and their equivalents. Also, various modifications and changes may be made within the scope of the attached claims.

Claims

What is claimed is:

1. A method of producing ethyl acetate with at least 95 wt% purity, the method comprising:A first round comprising: forming a reaction product comprising an aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water), methyl tert-butyl ether, and an acid catalyst through an esterification reaction, wherein forming the reaction product comprises mixing methyl tert-butyl ether, the acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (methyl tert-butyl ether: acid catalyst: acetic acid: ethanol) in a reactor, at a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm; and dehydrating the reaction product comprising: forming an azeotropic mixture in form of gas comprising methyl tert-butyl ether and water with a molar ratio between 84:16 and 3:1 (methyl tert-butyl ether: water) in a first distillation column by heating the reaction product to a temperature level between 70 °C and 105 °C, and at a pressure level between 1 atm and 4 atm; accumulating the azeotropic mixture in form of gas in a first condenser; forming a two-phase liquid mixture by cooling the accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 90 °C, and a pressure level between 1 atm and 4 atm in the first condenser, wherein the two-phase liquid mixture comprises an organic phase comprising methyl tert-butyl ether, and an aqueous phase comprising water;separating the organic phase of the two-phase liquid mixture from the aqueous phase of the two-phase liquid mixture using a phase-separator; removing the aqueous phase of the two-phase liquid mixture from the phaseseparator; refluxing the organic phase of the two-phase liquid mixture from the phaseseparator to the reactor and the first distillation column; and accumulating the dehydrated reaction product in the reactor; and a second round comprising: transferring the accumulated dehydrated reaction product to an evaporator; forming an evaporated mixture comprising methyl tert-butyl ether and ethyl acetate by heating the accumulated dehydrated reaction product to a temperature level between 55 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm, wherein after evaporating methyl tert-butyl ether and ethyl acetate, the acid catalyst remains in the evaporator; discharging the acid catalyst from the evaporator; feeding a second distillation column with the evaporated mixture; extracting an evaporated methyl tert-butyl ether from the top section of the second distillation column; feeding a second condenser with the extracted methyl tert-butyl ether;forming methyl tert-butyl ether in a form of liquid, wherein forming methyl tert-butyl ether in a form of liquid comprises cooling the evaporated methyl tert-butyl ether to a temperature level between 0 °C and 50 °C, and at a pressure level of 1 atm; extracting methyl tert-butyl ether in a form of liquid from the second condenser; re-feeding the top section of the second distillation column with methyl tert-butyl ether in a form of liquid; extracting a downstream liquid mixture comprising methyl tert-butyl ether and ethyl acetate from the bottom section of the second distillation column; feeding a re-boiler with the extracted downstream liquid mixture comprising methyl tert-butyl ether and ethyl acetate; forming ethyl acetate in a form of liquid with at least 95 wt% purity and a boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether, wherein forming ethyl acetate in a form of liquid with at least 95 wt% purity, and the boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether comprises heating the extracted downstream liquid mixture to a temperature level between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm; extracting ethyl acetate with at least 95 wt% purity in a form of liquid from the reboiler; and re-feeding the bottom section of the second distillation column with the boil-up vapour mixture comprising ethyl acetate and methyl tert-butyl ether.

2. The method of producing ethyl acetate of claim 1, wherein the top section of the first distillation column has a temperature level between 50 °C and 91 °C, and a pressure level between 1 atm and 3 atm.

3. The method of producing ethyl acetate of claim 1, wherein the top section of the second distillation column has a temperature level between 50 °C and 60 °C, and a pressure level of 1 atm.

4. The method of producing ethyl acetate of claim 1, wherein the bottom section of the second distillation column has a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm.

5. The method of producing ethyl acetate of claim 1, wherein forming ethyl acetate through the esterification reaction is coincides with forming the azeotropic mixture comprising methyl tertbutyl ether and water, wherein forming ethyl acetate is a continuous reaction process by removing water from the reaction product based on the Le Chatelier's principle.

6. A method of producing ethyl acetate with at least 95 wt% purity, the method comprising:A first round comprising: forming a reaction product comprising an aqueous solution of ethyl acetate with a molar ratio of 1:1 (ethyl acetate: water), dichloromethane, and an acid catalyst through an esterification reaction, wherein forming the reaction product comprises mixing dichloromethane, the acid catalyst, acetic acid, and ethanol with a molar ratio of 0.1:0.001:1:1 (dichloromethane: acid catalyst: acetic acid: ethanol) in a reactor, at a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atmosphere (atm) and 4 atm; andIdehydrating the reaction product comprising: forming an azeotropic mixture in form of gas comprising dichloromethane and water with a molar ratio between 81:18 and 61:39 (dichloromethane: water) in a first distillation column by heating the reaction product to a temperature level between 70 °C and 120 °C, and at a pressure level between 1 atm and 4 atm; accumulating the azeotropic mixture in form of gas in a first condenser; forming a two-phase liquid mixture by cooling the accumulated azeotropic mixture in form of gas to a temperature level between 25 °C and 105 °C, and a pressure level between 1 atm and 3 atm in the first condenser, wherein the two-phase liquid mixture comprises an organic phase comprising dichloromethane, and an aqueous phase comprising water; separating the organic phase of the two-phase liquid mixture from the aqueous phase of the two-phase liquid mixture using a phase-separator; removing the aqueous phase of the two-phase liquid mixture from the phaseseparator; refluxing the organic phase of the two-phase liquid mixture from the phaseseparator to the reactor and the first distillation column; and accumulating the dehydrated reaction product in the reactor; and a second round comprising: transferring the accumulated dehydrated reaction product to an evaporator;forming an evaporated mixture comprising dichloromethane and ethyl acetate by heating the accumulated dehydrated reaction product to a temperature level between 50 °C and 65 °C, and at a pressure level between 1 atm and 1.2 atm, wherein after evaporating dichloromethane and ethyl acetate, the acid catalyst remains in the evaporator; discharging the acid catalyst from the evaporator; feeding a second distillation column with the evaporated mixture; extracting an evaporated dichloromethane from the top section of the second distillation column; feeding a second condenser with the extracted dichloromethane; forming dichloromethane in a form of liquid, wherein forming dichloromethane in a form of liquid comprises cooling the evaporated dichloromethane to a temperature level between 10 °C and 40 °C, and at a pressure level of 1 atm; extracting dichloromethane in a form of liquid from the second condenser; re-feeding the top section of the second distillation column with dichloromethane in a form of liquid; extracting a downstream liquid mixture comprising dichloromethane and ethyl acetate from the bottom section of the second distillation column; forming ethyl acetate in a form of liquid with at least 95 wt% purity, and a boil-up vapour mixture comprising ethyl acetate and dichloromethane, wherein forming ethyl acetate in a form of liquid with at least 95 wt% purity and the boil-up vapour mixture comprising ethyl acetate and dichloromethane comprises heating the downstream liquid mixture to atemperature level between 77 °C and 91 °C, and at a pressure level between 1 atm and 1.5 atm; extracting ethyl acetate with at least 95 wt% purity in a form of liquid from the reboiler; and re-feeding the bottom section of the second distillation column with the boil-up vapour mixture comprising ethyl acetate and dichloromethane.

7. The method of producing ethyl acetate of claim 6, wherein the top section of the first distillation column has a temperature level between 57 °C and 105 °C, and a pressure level between 1 atm and 3 atm.

8. The method of producing ethyl acetate of claim 6, wherein the top section of the second distillation column has a temperature level between 39 °C and 42 °C, and a pressure level of 1 atm.

9. The method of producing ethyl acetate of claim 6, wherein the bottom section of the second distillation column has a temperature level between 80 °C and 90 °C, and a pressure level between 1.2 atm and 1.5 atm.

10. The method of producing ethyl acetate of claim 6, wherein forming ethyl acetate through the esterification reaction is coincides with forming the azeotropic mixture comprising dichloromethane and water, wherein forming ethyl acetate is a continuous reaction process by removing water from the reaction product based on the Le Chatelier's principle.

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