TECHNICAL FIELD

The present disclosure pertains to the technical field of chemical synthesis. In particular, the present disclosure relates to an improved process for production of acephate that is cost effective, while affording superior yield.

BACKGROUND OF THE INVENTION

Background description includes information that may be useful in understanding the present invention. It is not an admission that any of the information provided herein is prior art or relevant to the presently claimed invention, or that any publication specifically or implicitly referenced is prior art.

Acephate is an organophosphate foliar and soil insecticide of moderate persistence with residual systemic activity. It is used primarily for control of aphids, including resistant species, in vegetables (such as potatoes, carrots, greenhouse tomatoes, and lettuce) and in horticulture (such as roses and greenhouse ornamentals). Commercially, acephate products are available in powders, liquids, granules, tablets, and in water-soluble packets.

Currently, it is one of the most widely used and accepted insecticides. Numerous methods were tried, tested and adopted by the scientists and researchers for the synthesis of Acephate. However, these conventional methods/processes are still suffering from certain drawbacks such as high cost, low yield, less purity (product quality), large number of reaction steps, removal of side-products/impurities and time required for the complete synthesis of Acephate. These limitations, apart from others, have so far restricted the continuous industrial or large-scale production of Acephate. There is therefore a need in the art to develop a new and improved process of production of acephate that may overcome one or more limitations associated with the conventional processes and provide a continuous and cost effective way of producing acephate at an industrial scale. The present invention satisfies the existing needs, as well as others, and generally overcomes the deficiencies found in the prior art. Thus, the present invention involves technical advancement as compared to the existing knowledge or having economic significance or both and that makes the invention not obvious to a person skilled in the art.

All publications herein are incorporated by reference to the same extent as if each individual publication or patent application were specifically and individually indicated to be incorporated by reference. Where a definition or use of a term in an incorporated reference is inconsistent or contrary to the definition of that term provided herein, the definition of that term provided herein applies and the definition of that term in the reference does not apply.

OBJECTS OF THE INVENTION

It is an object of the present disclosure to provide a method of production of acephate that overcomes one or more limitations associated with the conventional methods.

It is an object of the present disclosure to provide a continuous process for production of acephate.

It is an object of the present disclosure to provide a method of production of acephate that is cost-effective.

It is an object of the present disclosure to provide a continuous process for production of acephate that allows easy addition and removal of reactant, impurities and final product.

It is an object of the present disclosure to provide a process for production of acephate that produces acephate of high purity. It is an object of the present disclosure to provide a method of production of acephate that can be implemented at an industrial scale.

SUMMARY OF INVENTION

The present disclosure pertains to the technical field of chemical synthesis. In particular, the present disclosure relates to an improved process for production of acephate that is cost effective while affording superior yield.

An aspect of the present invention relates to a continuous flow process for synthesis of acephate and its intermediates.

In another aspect of the present disclosure relates to a process for production of acephate, said process comprising the steps of: contacting O,O-dimethyl phosphoroamidothioate (DMPAT) with dimethyl sulphate to obtain methamidophos; contacting methamidophos with a acetylating agent to obtain acephate.

Various objects, features, aspects and advantages of the inventive subject matter will become more apparent from the following detailed description of preferred embodiments.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings are included to provide a further understanding of the present disclosure, and are incorporated in and constitute a part of this specification. The drawings illustrate exemplary embodiments of the present disclosure and, together with the description, serve to explain the principles of the present disclosure.

FIG. 1A and FIG. IB provides the elevated and side view of an Advanced Flow Reactor, in accordance with an embodiment of the present disclosure. FIG. 2 is a schematic illustrating a process for production of acephate, in accordance with an embodiment of the present disclosure.

FIG. 3 provides a schematic illustrating a process for production of DMPAT, in accordance with an embodiment of the present disclosure.

DETAILED DESCRIPTION OF THE INVENTION

The following is a detailed description of embodiments of the present invention. The embodiments are in such detail as to clearly communicate the invention. However, the amount of detail offered is not intended to limit the anticipated variations of embodiments; on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the present invention as defined by the appended claims.

Each of the appended claims defines a separate invention, which for infringement purposes is recognized as including equivalents to the various elements or limitations specified in the claims. Depending on the context, all references below to the “invention” may in some cases refer to certain specific embodiments only. In other cases it will be recognized that references to the “invention” will refer to subject matter recited in one or more, but not necessarily all, of the claims.

Groupings of alternative elements or embodiments of the invention disclosed herein are not to be construed as limitations. Each group member can be referred to and claimed individually or in any combination with other members of the group or other elements found herein. One or more members of a group can be included in, or deleted from, a group for reasons of convenience and/or patentability. Unless the context requires otherwise, throughout the specification which follow, the word “comprise” and variations thereof, such as, “comprises” and “comprising” are to be construed in an open, inclusive sense that is as “including, but not limited to.”

Reference throughout this specification to “one embodiment” or “an embodiment” means that a particular feature, structure or characteristic described in connection with the embodiment is included in at least one embodiment. Thus, the appearances of the phrases “in one embodiment’ ’ or “in an embodiment” in various places throughout this 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.

Various terms as used herein are shown below. To the extent a term used in a claim is not defined below, it should be given the broadest definition persons in the pertinent art have given that term as reflected in printed publications and issued patents at the time of filing.

As used in the description herein and throughout the claims that follow, the meaning of “a,” “an,” and “the” includes plural reference unless the context clearly dictates otherwise. Also, as used in the description herein, the meaning of “in” includes “in” and “on” unless the context clearly dictates otherwise.

In some embodiments, the numbers expressing quantities of ingredients, properties such as concentration, and so forth, used to describe and claim certain embodiments of the invention are to be understood as being modified in some instances by the term “about.” Accordingly, in some embodiments, the numerical parameters set forth in the written description are approximations that can vary depending upon the desired properties sought to be obtained by a particular embodiment. In some embodiments, the numerical parameters should be construed in light of the number of reported significant digits and by applying ordinary rounding techniques. Notwithstanding that the numerical ranges and parameters setting forth the broad scope of some embodiments of the invention are approximations, the numerical values set forth in the specific examples are reported as precisely as practicable.

The recitation of ranges of values herein is merely intended to serve as a shorthand method of referring individually to each separate value falling within the range. Unless otherwise indicated herein, each individual value is incorporated into the specification as if it were individually recited herein.

The headings and abstract of the invention provided herein are for convenience only and do not interpret the scope or meaning of the embodiments.

All methods described herein can be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. The use of any and all examples, or exemplary language (e.g. “such as”) provided with respect to certain embodiments herein is intended merely to better illuminate the invention and does not pose a limitation on the scope of the invention otherwise claimed. No language in the specification should be construed as indicating any non-claimed element essential to the practice of the invention.

The following discussion provides many example embodiments of the inventive subject matter. Although each embodiment represents a single combination of inventive elements, the inventive subject matter is considered to include all possible combinations of the disclosed elements. Thus if one embodiment comprises elements A, B, and C, and a second embodiment comprises elements B and D, then the inventive subject matter is also considered to include other remaining combinations of A, B, C, or D, even if not explicitly disclosed. The present disclosure pertains to the technical field of chemical synthesis. In particular, the present disclosure relates to an improved process for production of acephate that is cost effective while affording superior yield.

The present continuous flow process is beneficial over the traditional batch vessels with following advantages: (i) mass and heat transfer can be significantly improved by decreasing reactor size; (ii) fewer transport limitations can be offered by the feasibility and device flexibility of continuous flow synthesis; (iii) yield and selectivity can be improved due to the precise control of reaction variables such as temperature, pressure and residence time, (iv) scale-up of continuous flow synthesis is readily achieved by simply increasing the number of reactors or their sizes.

The present inventors motivated by these advantages and worked out a continuous flow synthesis in a flow reactor system for the manufacture of acephate. The present inventors performed various continuous flow screening experiments and surprisingly arrived at a process which result in the maximum yield and high purity of acephate.

An aspect of the present disclosure relates to a process for production of acephate, said process comprising the steps of: contacting O,O-dimethyl phosphoroamidothioate (DMPAT) with dimethyl sulphate to obtain methamidophos; contacting methamidophos with a acetylating agent to obtain acephate; adding a weak base to the crude product mass having acephate to adjust pH to a range of 6 to 8; separating an organic layer having acephate and an aqueous layer; and recovering acephate from said organic layer.

In an embodiment, a mixture of dimethyl sulphate and solvent is contacted with 0,0- dimethyl phosphoroamidothioate (BMP AT) in a volumetric ratio ranging from 0.10- 1:0.10-0.50 preferably 0.46 to 0.50 at a temperature ranging from 50°C to 100°C preferably 70°C to 90°C. In an embodiment, O,O-dimethyl phosphoroamidothioate (DMPAT) is contacted with dimethyl sulphate for a time period ranging from 5 minutes to 40 minutes, preferably, for a time period ranging from 10 minutes to 30 minutes, more preferably, for a time period ranging from 10 minutes to 20 minutes, and most preferably, for a time period ranging from 12 minutes to 18 minutes.

In an embodiment, the process is optionally carried out in presence of solvent for example halogenated hydrocarbon solvent such as dichloromethane, chloroform, carbon tetrachloride, 1,2-dichloroethane, chlorobenzene, etc, preferably dichloromethane. However, any other organic solvent as known to persons skilled in the art can also be used.

In an embodiment, the production of acephate according to the present invention is continuously prepared in the absence of a solvent.

In an embodiment, the step of contacting O,O-dimethyl phosphoroamidothioate (DMPAT) with dimethyl sulphate in a first reactor selected from Advanced Flow Reactor (AFR), Spin Disc Reactor (SDR), Moving Bed Reactor (MBR), Plug Flow reactor (PFR), Continuous Stirred Tank Reactors (CSTR), Tubular Reactor Oscillatory Reactor, Loop Reactor, and Pump Reactor Static Mixer Reactor (SMR).

In an embodiment, the step of contacting O,O-dimethyl phosphoroamidothioate (DMPAT) with dimethyl sulphate to obtain methamidophos is performed in a first Advanced Flow Reactor (AFR).

In an embodiment, methamidophos thus formed is contacted with acetylating agent for example a mixture of acetic anhydride and sulfuric acid in a volumetric ratio ranging from 0.30 to 0.40 at a temperature ranging from 50°C to 65°C. In an embodiment, advantageously the reaction is carried out for a time period ranging from 1 minutes to 30 minutes, preferably, for a time period ranging from 5 minutes to 20 minutes, more preferably, for a time period ranging from 5 minutes to 10 minutes, and most preferably, for a time period ranging from 5 minutes to 8 minutes.

In an embodiment, the step of contacting methamidophos with acetylating agent is performed in a second reactor selected from advanced Flow Reactor (AFR), Spin Disc Reactor (SDR), Moving Bed Reactor (MBR), Plug Flow reactor (PFR), Continuous Stirred Tank Reactors (CSTR), Tubular Reactor Oscillatory Reactor, Loop Reactor, and Pump Reactor Static Mixer Reactor (SMR).

The acetylating agent used in the present process is selected from Acetyl halides and Anhydrides, ketene, preferably the acetylating agent is Acetic Anhydride.

In an embodiment, the step of contacting methamidophos with acetylating agent in a continuous flow is done in a second Advanced Flow Reactor (AFR). In an embodiment, the process is a continuous process.

Accordingly, the present invention provides a process for production of acephate comprising converting methamidophos into acephate, wherein said methamidophos is prepared continuously by reacting O, O-dimethyl phosphoramidothioate and dimethyl sulphate in a advanced flow reactor.

In an embodiment, 0,0-dimethyl phosphoramidothioate is prepared by: contacting PSCI3 (thiophosphoryl chloride) with methanol to form O-methyl phosphorodichloridothioate; contacting O-methyl phosphorodichloridothioate with caustic soda lye to form 0,0-dimethyl phosphorochloridothioate; and contacting 0,0- dimethyl phosphorochloridothioate with an ammonia solution to form 0,0-dimethyl phosphoroamidothioate. In an embodiment, methanol is contacted with PSCh in a volumetric ratio ranging from 0.80 to 0.90 preferably in the range of 0.84 to 0.88 at a temperature ranging from 0°C to 15°C for a time period ranging from 1 minutes to 30 minutes, preferably, for a time period ranging from 5 minutes to 20 minutes, more preferably, for a time period ranging from 5 minutes to 10 minutes, and most preferably, for a time period ranging from 5 minutes to 8 minutes.

In an embodiment, the step of O,O-dimethyl phosphoroamidothioate is done in a third reactor selected from Advanced Flow Reactor (AFR), Spin Disc Reactor (SDR), Moving Bed Reactor (MBR), Plug Flow reactor (PFR), Continuous Stirred Tank Reactors (CSTR), Tubular Reactor Oscillatory Reactor, Loop Reactor, and Pump Reactor Static Mixer Reactor (SMR).

In an embodiment, the step of contacting PSCh with methanol is done in a third Advanced Flow Reactor (AFR).

In an embodiment, the ammonia solution is contacted with O,O-dimethyl phosphorochloridothioate in a volumetric ratio ranging from 2.25 to 2.60 at a temperature ranging from 25°C to 45°C. In an embodiment, the ammonia solution comprises 12% to 20% NH3.

In an embodiment, the step of contacting O,O-dimethyl phosphorochloridothioate with an ammonia solution is done in a fourth reactor selected from Advanced Flow Reactor

(AFR), Spin Disc Reactor (SDR), Moving Bed Reactor (MBR), Plug Flow reactor (PFR), Continuous Stirred Tank Reactors (CSTR), Tubular Reactor Oscillatory Reactor, Loop Reactor, and Pump Reactor Static Mixer Reactor (SMR). In an embodiment, the step of contacting 0,0-dimethyl phosphorochloridothioate with an ammonia solution is done in a fourth Advanced Flow Reactor (APR). In an embodiment, the process is a continuous process.

In an embodiment of the present invention, the continuous flow process for the synthesis of acephate is carried out by combining the reactors selected from Advanced Flow Reactor (AFR), Spin Disc Reactor (SDR), Moving Bed Reactor (MBR), Plug Flow reactor (PFR), Continuous Stirred Tank Reactors (CSTR), Tubular Reactor Oscillatory Reactor, Loop Reactor, and Pump Reactor Static Mixer Reactor (SMR).

The reactor system of the present invention can further comprise 1 to 100 parallel reactor systems in order to increase the production capacity. Typically, the reactor systems comprise one or more mixing reactors, one or more reaction reactors, one or more mixing and reaction reactors, one or more heating and cooling element or any combinations thereof, which may be designed in such a way that it is jacketed to maintain desired temperature and pressure of the reaction vessels in the system.

A continuous flow process as used herein is not particularly limited and can be further modified by a person of ordinary skill in the art within the scope of invention. In general, for example and without limitation, a continuous flow process can allow a continuous flow of reactants that can be charged in a reactor, vessel or line, allowing mixing or reaction of the reactants in order to form products. This is followed by continuous flow (discharge) of the products from the reactor, vessel or line. Thus, a continuous flow process can be considered as a process where reactants are charged or fed into a reactor, vessel or line, while a product is simultaneously removed during part of the reaction process. A continuous flow process can allow a single step or multiple steps to be performed, where each step independently of the other can be a reaction, separation or purification. The inventors of the present disclosure, through significant research and experimentation, have found that utilization of continuous reactor, particularly, the continuous flow reactors (against the conventional batch reactors) impart distinct technical advantages such as easy addition and removal of reaction mixture and products, high yield, high purity, consistency of the product quality, and constant heat load throughout the reaction during the synthesis of Acephate. It could also be found that the critical reaction parameters viz. temperature and volumetric ratios of the reactants coupled with the utilization of continuous flow reactor leads to a significant economic advantage and reduction in downtime in the process of synthesis of DMPAT and Acephate, in comparison to the existing commercially implemented methods.

Thus, present invention is encompasses a feature that involves technical advance as compared to the existing knowledge or having economic significance or both and that makes the invention not obvious to a person skilled in the art.

The present invention thus provides a commercially viable, economical, friendly and continuous flow process for synthesis of acephate, by reducing unfavorable environmental effects.

According to some embodiments, synthesis of acephate occurs in shorter reaction time, relative to known methods.

In some embodiments, residence time of reactants in the reactor to synthesize acephate may be about 1 hours or less, about 30 min or less or, in some cases, about 20 min or less.

According to an embodiment of the present invention, residence time of reactants in the reactor to synthesize acephate is about 1 hour or less than 1 hour. According to an embodiment of the present invention, residence time of reactants in the reactor to synthesize acephate is about 30 minutes or less.

According to one preferred embodiment of the present invention, residence time of reactants in the reaction vessel to synthesize acephate may be about 6 min or less.

Without wishing to be bound by theory, such residence times may be attributed to increase in the rate of a chemical reaction within a microreactor, relative to other processes (e.g., batch processes), due to rapid mass and heat transfer, high temperatures, and high pressures attainable within a microreactor, as described more fully below.

The present invention has the advantage of short residence time of the material, high selectivity, high yield, less equipment investment, manufacturing cost savings, reduced material consumption, reducing the amount of by-products. Accordingly, the entire process is technically advanced over the conventional process, continuous, low energy consumption, an efficient and feasible continuous synthesis of acephate and intermediates thereof.

Thus, the present invention provides an advanced flow reactor synthesis in continuous operation for production of acephate in high yield and purity.

The process of the present invention provides acephate having purity at least 90% by HPLC.

The process of the present invention provides acephate having purity at least 95% by HPLC.

The process of the present invention provides acephate with an high yield of at least 80% and high purity of more than 95%, preferably more than 98%. A system comprising an advanced flow reactor for producing acephate by continuous flow process wherein the process comprising continuously reacting O, O-dimethyl phosphoramidothioate and dimethyl sulphate to obtain methamidophos and converting methamidophos into acephate.

The process for the production of acephate according to the present invention is illustrated in following embodiments, but not limited to, the subsequent description and the figures/drawings referred therein.

Referring to FIG. 1A and FIG. IB provides exemplary elevated and side view of an Advanced Flow Reactor, in accordance with an embodiment of the present disclosure. As can be seen in FIG. 1A, the Advanced Flow Reactor 100 defines two reaction mixture feeding inlets 102 and 104, and an outlet 112 to extract the product mass obtained by the reaction of reaction mixture fed into the reactor via inlets 102 and 104. 106, 108 and 110 define the utility inlet nozzles; and 114, 116 and 118 define the utility outlet nozzles. Reactor 100 may also be equipped with other inlets/outlets such as N2 gas flushing nozzle 120, a vent 122 for removal of any exhaust gases, a shell drain nozzle 124 and a process drain nozzle 126. As can be seen in FIG. IB, Reactor 100 also defines nine thermowell 128 housing the temperature measuring device forming part of the Reactor 100.

FIG. 2 provides a schematic illustrating a process for production of acephate utilizing 2 Advanced Flow Reactors 100 (herein referred to as reactor 100-1 and reactor 100-2), such as the one illustrated in FIG. 1, in accordance with an embodiment of the present disclosure. As can be seen in FIG. 2, O,O-dimethyl phosphoroamidothioate (DMPAT) and a mixture of dimethyl sulphate and solvent are fed into the reactor 100-1 via inlets/feeding lines 102-1 and 104-1 to obtain methamidophos. The product stream (containing methamidophos) is removed from reactor 100-1 via outlet 112-1, and is fed into the reactor 100-2 via inlet 102-2. A mixture of acetic anhydride and sulfuric acid is fed into the reactor 100-2 via inlet 104-2 containing methamidophos and are allowed to react to obtain a crude product mass having acephate. The crude product mass is removed from reactor 100-2 via outlet 112-2 and a weak base is added to it to adjust the pH of crude product to a range of 6.5 to 7.5. The crude product mass is then separated into an organic layer having acephate and an aqueous layer having ammonium acetate. Acephate can be recovered from the organic layer by removal of the solvent.

FIG. 3 provides a schematic illustrating a process for production of DMPAT utilizing 2 Advanced Flow Reactors 100 (herein referred to as reactor 100-3 and reactor 100-4), such as the one illustrated in FIG. 1, in accordance with an embodiment of the present disclosure. As can be seen in FIG. 3, PSCh is obtained by reaction of sulphur and PCI3 at 70°C to 125°C, and the same is fed into the reactor 100-3 along with methanol via inlets 102-3 and 104-3 to obtain O-methyl phosphorodichloridothioate. O-methyl phosphorodichloridothioate is removed from reactor 100-3 via outlet 112-3 and is fed into another reactor 130. Caustic soda lye along with methanol is added thereto to produce O,O-dimethyl phosphorochloridothioate. O,O-dimethyl phosphorochloridothioate is removed from the reactor 130, and is fed into the reactor 100-4 via inlet 102-4. An ammonia solution is fed into the reactor 100-4 containing O,O-dimethyl phosphorochloridothioate via inlet 104-4 and allowed to react to obtain a crude product mass having O,O-dimethyl phosphoroamidothioate (DMPAT). The crude product mass is removed from the reactor 100-4 via outlet 112-4, and a solvent is added thereto to allow separation of crude product mass into an aqueous layer and an organic layer having DMPAT. DMPAT is recovered from the organic layer by removing the solvent.

While the foregoing description discloses various embodiments of the disclosure, other and further embodiments of the invention may be devised without departing from the basic scope of the disclosure. The invention is not limited to the described embodiments, versions or examples, which are included to enable a person having ordinary skill in the art to make and use the invention when combined with information and knowledge available to the person having ordinary skill in the art.

EXAMPLES

SYNTHESIS OF DMPAT

2 commercially available Advanced Flow reactors were used in tandem for production of DMPAT in a continuous mode.

Synthesis of O-methyl phosphorodichloridothioate

PSCI3 and Methanol were fed into an advanced flow reactor at a flow rate of about

1200 kg/hr and aabboouutt 1050 kg/hr, respectively, to obtain O-methyl phosphorodichloridothioate of about 97% purity with about 96% yield. Table 1 illustrates the effect of volumetric ratios of reactants and temperature conditions of reaction on the yield of final product.

Table 1: Effect of different parameters on yield of O-methyl phosphorodichloridothioate

Synthesis of O,O-dimethyl phosphoroamidothioate (DMPAT)

O,O-dimethyl phosphorochloridothioate and 13% NH3 were fed into an advanced flow reactor at a flow rate of about 1060 kg/hr and 2300 kg/hr, respectively, to obtain DMPAT of about 95% purity with yield of about 95%. Table 2 illustrates the effect of volumetric ratios of reactants and temperature conditions of reaction on the yield of final product. Table 2: Effect of different parameter on yield of DMPAT

PRODUCTION OF ACEPHATE

Two commercially available Advanced Flow reactors were used in tandem for the production of acephate in a continuous mode.

Synthesis of Methamidophos

O,O-dimethyl phosphoroamidothioate (DMPAT) and a mixture of dimethyl sulphate and dichloromethane (solvent) (Solvent: DMPAT volumetric ratio being about 0.4, and dimethyl sulphate:DMPAT volumetric ratio being about 0.15) were fed into an advanced flow reactor at a flow rate of about 4000 kg/hr and about 1920 kg/hr, respectively, to obtain methamidophos of about 92% product purity and with a yield of about 84.5%. Table 3 illustrates the effect of volumetric ratios of reactants and temperature conditions of reaction on the yield of final product.

Table 3: Effect of different parameter on yield of methamidophos Synthesis of Acephate

Methamidophos in dichloromethane and a mixture of acetic anhydride and sulfuric acid were fed into the second advanced flow reactor at a flow rate of about 5050 kg/hr and 1995 kg/hr, respectively. Crude Acephate containing acetic acid and solvent is neutralized with liquor ammonia. Acetic acid gets converted to ammonium acetate, which goes in the aqueous layer. Organic layer containing crude Acephate is processed further and crystallized to get Acephate of 98% purity with a yield of about 84.5%.

Table 4 below illustrates the effect of volumetric ratios of reactants and temperature conditions on the yield of final product.

Table 4: Effect of different parameter on yield of Acephate

The inventors of the present disclosure found that utilization of continuous reactor, such as advanced flow reactor (AFR) (against the conventional batch reactors) coupled with optimization of reaction parameters such as temperature and volumetric ratios of the reaction mixtures/reactants impart several fold technical advantages such as ease of addition and removal of reaction mixture/reactants and products, improved yield, high purity, consistency of the product quality, constant heat load throughout the reaction, decrease in requirement of solvent and significant reduction in cost of production of Acephate. This leads to a significant economic advantage and annualised saving of about 1087 Lakhs with production of about 8600 metric tons (MT). Table 5 hereinbelow illustrates the comparative advantages of process of production of Acephate of the present disclosure over the conventional production method using the batch reactors.

Table 5

ADVANTAGES OF THE PRESENT INVENTION

The present disclosure provides a method of production of acephate that overcomes one or more limitations associated with the conventional methods.

The present disclosure provides a continuous process for production of acephate.

The present disclosure provides a method of production of acephate that is cost- effective.

An important advantage of the present invention is that the reaction is operated in continuous manner in a advanced flow reactor with or without any solvent and the capacity of the production of the desired product can be increased by connecting two or more reactors in a simplified and friendly manner. The present disclosure provides a continuous process for production of acephate that allows easy addition and removal of reactant, impurities and final product.

The present disclosure provides a process for production of acephate that produces acephate of high purity.

The present disclosure provides a method of production of acephate that is implementable at an industrial scale.