Description:A METHOD FOR THE PRODUCTION OF AMMONIUM NITRATE AND METHANOL FROM COAL”
FIELD OF INVENTION
[0001] The present disclosure relates to reduction of CO2 emissions from coal to ammonium Nitrate and Methanol production facility. More particularly the invention relates to a method processes contains electrolyser running on green power to produce oxygen and hydrogen. The hydrogen from electrolyser is used with CO2 from CO2 capture to make value added products and oxygen from electrolyser is used in coal/biomass gasification.
BACKGROUND OF THE INVENTION
[0002] 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.
[0003] Usage of ammonium Nitrate as well as methanol derived from coal gasification is desired for explosive and mining industry and blending with petrol respectively . Coal derived Ammonium Nitrate & Methanol can reduce oil dependence of the country like India, China.
[0004] The typical method for producing Ammonium Nitrate from coal is shown in Fig.1. In this process, Syngas generation takes place in coal gasifier using steam, cola and oxygen. Oxygen is supplied from air separation unit and steam from auxiliary boiler/ process plant. The CO in the syngas is converted to CO2 and H2 in shift reactor. The CO2 and H2s is removed from CO2 capture process. The CO2 is vented and H2S is sent for sulfur recovery. The pure H2 from Syngas is used to make ammonia and Nitric acid and subsequently Ammonium Nitrate.
[0005] One of the drawback of producing Ammonium Nitrate from coal is high CO2 emissions as almost all carbon in the coal is vented out. Also, Air separation plant requires steam to drive air compressors which increases coal consumption in auxiliary boiler to produce steam and increases additional CO2 emissions from auxiliary boiler. The typical emissions from the process is 3-3.3 kg of CO2 per kg of Ammonium Nitrate. Where gasification island contributes 2 kg of CO2 per kg of Ammonium Nitrate and balance is contributed by auxiliary boiler.
[0006] Similarly, the typical method for producing methanol from coal is shown in Fig.2. In this process, Syngas generation takes place in coal gasifier using steam, coal and oxygen. Oxygen is supplied from air separation unit and steam from auxiliary boiler/ process plant. The CO in the syngas is partially converted to CO2 and H2 in shift reactor. The partial CO2 and all H2s is removed from CO2 capture process. The Co2 is vented and H2S is sent for sulfur recovery. The mixture of CO, CO2 and H2 having ratio H2 to CO of 2 is used to make methanol.
[0007] One of the drawback of producing methanol from coal is high CO2 emissions as 60-70 % carbon in the coal is vented out. Also, Air separation plant requires steam to drive air compressors which increases coal consumption in auxiliary boiler to produce steam and increases additional CO2 emissions from auxiliary boiler. The specific CO2 emissions are 3.4-4 kg of CO2 per kg of methanol. The coal gasification contributes nearly 60 % of emissions.
[0008] The present invention relates to reducing CO2 emissions by utilizing CO2 with hydrogen as well as minimizing steam usage in Water gas shift rector as well as air separation unit which reduces Coal consumption in Auxiliary boiler which reduces CO2 emissions.

PRIOR ART :
[0009] A state of art CN 114394883 relates to the field of methanol preparation with zero carbon emission, and particularly discloses a method for preparing methanol with near zero carbon emission by using pulverized coal waste boiler gasification coupled with green electro-green hydrogen, which comprises the following steps: oxygen generated by the air separation device and oxygen generated by the water electrolysis device react with coal in the pulverized coal waste boiler gasification device together to obtain synthesis gas; the pulverized coal waste boiler gasification device recovers heat of high-temperature synthesis gas through a waste heat boiler and a steam superheater to produce high-pressure superheated steam, and the high-pressure superheated steam is sent to an air separation device to drive an air compressor turbine; the synthesis gas is sent to a heat recovery device for further heat recovery; sending the synthesis gas out of the heat recovery device to a purification device, removing only sulfur-containing acid gas without decarburization, and obtaining purified gas containing carbon monoxide, hydrogen and carbon dioxide; and one part of the electric energy generated by the new energy power generation system is sent to the water electrolysis hydrogen production device, one part of the electric energy is used by other electricity utilization facilities of the whole plant, and the other part of the electric energy is sent to the energy storage device for storage. In work, power is generated from syngas and generated power is used to drive electrolyzer and hence does not address the CO2 coming out from gas turbine.
[0010] Another state of art WO2010/135381 provides an ICTL process and system involving direct coal liquefaction, indirect coal liquefaction and biomass conversion processes, in which C02 generated by the coal-to-liquids processes and the biomass conversion is used as feedstock to produce algae and liquid products, such as liquid fuels and fuel additives, such that carbon dioxide emissions are minimized and carbon resources are efficiently utilized. In the indirect coal liquefaction and biomass conversion, the coal and biomass are first gasified for conversion into syngas and byproduct C02. Optionally, natural gas can also be converted to syngas by a conventional methane-steam reforming process. Portions of the syngas produced by the above processes are supplied to the direct coal liquefaction process, to an FT synthesis conversion process, and, in a preferred embodiment of the invention, to a methanol synthesis conversion process. C02 produced by the above processes is reacted with ammonia to produce urea. Methanol produced is reacted with urea to produce dimethyl carbonate (DMC) and ammonia. Ammonia from the DMC synthesis and/or from the direct coal liquefaction process is used as the ammonia for the urea synthesis. In this invention, it is desired to make algae , urea and DMC from ammonia which is needed as extra raw material.
[0011] Another state of art CN101440019A relates to a method of directly applying large-scale non-grid-connected wind power to producing methanol. The method mainly uses the large-scale non-grid-connected wind power as a working power supply for electrolyzing equipment, uses oxygen electrolyzed by water as gasifying agent, uses hydrogen electrolyzed by the water to adjust carbon-hydrogen ratio in desulfurized water gas, and uses the water gas with the obtained optimal carbon-hydrogen ratio to prepare the methanol. This method still uses water gas shift reactor to adjust H2 to CO2 ratio for methanol production.
[0012] Yet another state of art US 2011/0243828A1 process for producing ammonia from air and water com prizes producing nitrogen gas from air by pressure-swing adsorption; producing hydrogen gas by electrolysis of water; compressing the nitrogen gas in a first cylinder to produce pressurized nitrogen gas; compressing the hydrogen gas in a second cylinder to produce pressurized hydrogen gas; com pressing a mixture of the pressurized nitrogen and hydrogen gases in a third cylinder, heating the compressed mixture in Publication Classification the presence of a catalyst to react nitrogen and hydrogen to form ammonia; and extracting the ammonia from the mixture. A system for producing ammonia in the above process is also provided. In this invention , green power is used to produce H2 and N2 from independent source to produce Ammonia.
[0013] These challenges collectively hinder the efficiency and reliability. Thus there is a pressing need to achieve the same.
OBJECTS OF THE INVENTION
[0014] Some of the objects of the present disclosure, which at least one embodiment herein satisfy, are listed herein below.
[0015] It is an object of the present subject matter to provide title, which overcomes the aforementioned and other drawbacks existing in the prior art fixture and methods.
[0016] It is a principal object of the present subject matter to introduce a method for the synthesis of Ammonium Nitrate or Methanol via coal gasification by utilizing CO2 emissions derived from the gasification process for the production of methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG).
[0017] It is another significant object of the present subject matter to propose the method to minimize or eliminate the requirement for steam in the coal to synthesis ammonium nitrate or methanol conversion process.
[0018] It is another significant object of the present subject matter to propose the method by incorporating an electrolyser for oxygen production in the gasification phase and utilizing hydrogen for chemical synthesis from CO2 or blending with syngas for enhanced methanol production.
[0019] These and other objects and advantages of the present subject matter will be apparent to a person skilled in the art after consideration of the following detailed description taking into consideration with accompanied drawings in which preferred embodiments of the present subject matter are illustrated.
SUMMARY OF THE INVENTION
[0020] This summary is provided to introduce the concept of a method for the production of Ammonium Nitrate and Methanol from coal. The concepts are further described below in the detailed description. This summary is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used to limit the scope of the claimed subject matter.
[0021] The present invention relates to a method for the production of Ammonium Nitrate and Methanol from coal. The method comprises of generating syngas from coal gasification, wherein oxygen for gasification is produced by an electrolyzer powered by green energy from solar or wind sources and particulates are removed from the syngas, passing the syngas through a water gas shift reactor to produce hydrogen (H2) and carbon dioxide (CO2), removing hydrogen sulphide (H2S) and CO2 from the syngas using a carbon capture process, wherein the concentration of H2S is less than 100 ppm and the concentration of CO2 is in the range of 0-0.5% by volume, mixing the pure CO2 from the carbon capture system with hydrogen from the electrolyzer to produce Methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG) and synthesising into Methanol and Ammonium Nitrate.
[0022] To further understand the characteristics and technical contents of the present subject matter, a description relating thereto will be made with reference to the accompanying drawings. However, the drawings are illustrative only but not used to limit the scope of the present subject matter.
[0023] Various objects, features, aspects, and advantages of the inventive subject matter will become more apparent from the following detailed description of preferred embodiments, along with the accompanying drawing figures in which like numerals represent like components.
BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWINGS
[0024] It is to be noted, however, that the appended drawings illustrate only typical embodiments of the present subject matter and are therefore not to be considered for limiting of its scope, for the invention may admit to other equally effective embodiments. The detailed description is described with reference to the accompanying figures. In the figures, a reference number identifies the figure in which the reference number first appears. The same numbers are used throughout the figures to reference like features and components. Some embodiments of improved fixture or methods or structure in accordance with embodiments of the present subject matter are now described, by way of example, and with reference to the accompanying figures, in which
[0025] Fig. 1 illustrates the schematic block diagram of the conventional method of Ammonium Nitrate production process from coal gasification in accordance with the disclosure;
[0026] Fig. 2 illustrates the schematic block diagram of the conventional method of methanol production process from coal gasification in accordance with the disclosure;
[0027] Fig. 3 illustrates the flow chart of a method for the production of Ammonium Nitrate and Methanol from coal in accordance with an embodiment of the present disclosure;
[0028] Fig. 4 illustrates the block diagram of a method for the production of Ammonium Nitrate from coal in accordance with an embodiment of the present disclosure;
[0029] Fig. 5 illustrates the block diagram of a method for the production of Methanol from coal with retrofit in accordance with an embodiment of the present disclosure;
[0030] Fig. 6 illustrates the flow chart of a method for the production of Ammonium Nitrate and Methanol from coal without shift reactor in accordance with an embodiment of the present disclosure.
[0031] The figures depict embodiments of the present subject matter for the purposes of illustration only. A person skilled in the art will easily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles of the disclosure described herein.

DETAILED DESCRIPTION OF THE INVENTION WITH REFERENCE TO THE ACCOMPANYING DRAWINGS
[0032] A few aspects of the present disclosure are explained in detail below with reference to the various figures. Example implementations are described to illustrate the disclosed subject matter, not to limit its scope, which is defined by the claims. Those of ordinary skill in the art will recognize a number of equivalent variations of the various features provided in the description that follows.
[0033] 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.
[0034] 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.
[0035] 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. When any such inclusion or deletion occurs, the specification is herein deemed to contain the group as modified thus fulfilling the written description of all groups used in the appended claims.
[0036] Various embodiments are further described herein with reference to the accompanying figures. It should be noted that the description and figures relate to exemplary embodiments and should not be construed as a limitation to the subject matter of the present disclosure. It is also to be understood that various arrangements may be devised that, although not explicitly described or shown herein, embody the principles of the subject matter of the present disclosure. Moreover, all statements herein reciting principles, aspects, and embodiments of the subject matter of the present disclosure, as well as specific examples, are intended to encompass equivalents thereof. Yet further, for the sake of brevity, operation or working principles pertaining to the technical material that is known in the technical field of the present disclosure have not been described in detail so as not to unnecessarily obscure the present disclosure.
[0037] The present invention relates to a method for the production of Ammonium Nitrate and Methanol from coal.
[0038] Fig. 1 illustrates the schematic block diagram of the conventional method of Ammonium Nitrate production process from coal gasification in accordance with the disclosure. In the conventional process for generating Ammonium Nitrate, depicted in Figure 1, the following steps are typically undertaken. Firstly, syngas is produced from a coal gasification module, with particulate matter subsequently removed via a particulate system. Oxygen required for gasification is typically sourced from an air separation unit, while steam necessary for operating said unit is supplied from an auxiliary boiler, often fuelled by coal. Subsequently, the syngas undergoes a Water Gas Shift (WGS) reactor process, converting a majority of CO into H2 and CO2. H2S and CO2 are further removed using technologies such as rectisol or other carbon capture processes, ensuring that H2S concentration in the syngas remains below 100 ppm, and CO2 concentration falls within the range of 0-0.5% by volume. Pure CO2 separated through the carbon capture system is usually vented out. The resultant syngas, following H2S and CO2 removal, undergoes purification in a Liquid N2 wash system, where impurities such as CO2, methane, and CO are eliminated, and nitrogen (N2) is introduced to attain a desired H2:N2 mole ratio of 3:1. Finally, the syngas enriched in H2 is directed to an ammonia synthesis section, where produced ammonia is subsequently utilized in the production of Nitric acid and Ammonium Nitrate in a subsequent process.
[0040] Fig. 2 illustrates the schematic block diagram of the conventional method of methanol production process from coal gasification in accordance with the disclosure. In the conventional process for Methanol production, the following steps are typically followed. Initially, syngas is generated from a coal gasification module, with particulate matter being removed through a particulate system. Oxygen necessary for gasification is typically supplied from an air separation unit, while steam essential for the operation of said unit is sourced from an auxiliary boiler, often fueled by coal. Subsequently, the syngas undergoes a Water Gas Shift (WGS) reactor process, aimed at achieving a H2:CO ratio of 2:1 and converting CO into H2 and CO2. Steam required for the WGS system is typically provided by the auxiliary boiler. Following this, H2S and CO2 are removed using technologies such as Rectisol or other carbon capture processes, ensuring that H2S concentration in the syngas remains below 100 ppm, and CO2 concentration falls within the range of 1-3% by volume. Pure CO2 separated through the carbon capture system is typically vented out. The resulting syngas, post H2S and CO2 removal, possessing a H2:CO ratio of 2 and a R ratio (H2-CO2/CO+CO2) of 2, is then directed into a methanol reactor for the production of methanol.
[0041] Fig. 3 illustrates the flow chart of a method for the production of Ammonium Nitrate and Methanol from coal in accordance with an embodiment of the present disclosure.
[0042] A method(100) for the production of Ammonium Nitrate and Methanol from coal comprises of generating(102) syngas from coal gasification wherein oxygen for gasification is produced by an electrolyzer powered by green energy from solar or wind sources and particulates are removed from the syngas, passing(104) the syngas through a water gas shift reactor to produce hydrogen (H2) and carbon dioxide (CO2), removing(106) hydrogen sulfide (H2S) and CO2 from the syngas using a carbon capture process wherein the concentration of H2S is less than 100 ppm and the concentration of CO2 is in the range of 0-0.5% by volume, mixing(108) the pure CO2 from the carbon capture system with hydrogen from the electrolyzer to produce Methanol Dimethyl Ether (DME) or Synthetic Natural Gas (SNG) and synthesizing(110) into Methanol and Ammonium Nitrate..
[0043] At the step 102, syngas is generated from coal gasification, where the oxygen necessary for the gasification process is produced by an electrolyzer powered by renewable energy sources such as solar or wind power. Additionally, particulate matter is removed from the syngas to ensure its purity.
[0044] At the step 104, the generated syngas is passed through a water gas shift reactor to facilitate the conversion of a majority of carbon monoxide (CO) into hydrogen (H2) and carbon dioxide (CO2).
[0045] At the step 106, the syngas undergoes a carbon capture process to remove impurities such as hydrogen sulfide (H2S) and CO2. This process ensures that the concentration of H2S remains below 100 parts per million (ppm), while the concentration of CO2 falls within the range of 0-0.5% by volume.
[0046] At the step 108, the pure CO2 obtained from the carbon capture system is combined with hydrogen produced by the electrolyzer. This mixture can be utilized to produce various valuable products, including Methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG).
[0047] At the step 110, the syngas is utilized for the synthesis of Methanol and Ammonium Nitrate, representing the culmination of the production process. The oxygen required for the Claus process and nitric acid plant is provided by the electrolyzer.
EXAMPLES :
Example 1:
[0048] Fig. 4 illustrates the block diagram of a method for the production of Ammonium Nitrate from coal in accordance with an embodiment of the present disclosure. The method for the production of ammonia and ammonium nitrate begins with the generation of syngas through a coal gasification module, followed by the removal of particulate matter from the system. Notably, oxygen essential for gasification is produced by an electrolyzer powered by renewable energy sources such as wind or solar power, eliminating the need for an air separation unit. Subsequently, the syngas undergoes a Water Gas Shift (WGS) reactor process to primarily convert CO into H2 and CO2.
[0049] The following reactions takes place in Water Gas Shift (WGS) reactor
CO + H2O ↔ CO2 +H2
[0050] Following reactions takes place in Ammonia reactor , typical concentration of feed gas to ammonia reactor is 25 % H2 and 75 % N2
N2 + 3H2 ↔ 2 NH3
[0051] Following reactions takes place in Ammonia oxidation and NOX absorption for Nitric acid production.

[0052] Nitric acid composition is 60-75 wt % and balance water.Following reactions takes place for ammonium Nitrate production
NH3 + HNO3 ↔ NH4NO3
[0053] A typical composition of ammonium Nitrate is 80-85 % by wt.
[0054] Following this, H2S and CO2 are efficiently removed from the syngas through processes like rectisol or other carbon capture methods, ensuring that H2S concentration remains below 100 ppm and CO2 concentration falls within the range of 0-0.5% by volume. The pure CO2 obtained from the carbon capture system is then combined with hydrogen from the electrolyzer to produce valuable products such as Methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG).
[0055] Moreover, the syngas from which H2S and CO2 have been removed is directed into a Liquid N2 wash system, where impurities including CO2, methane, and CO are further eliminated, and nitrogen (N2) is added to achieve a H2:N2 mole ratio of 3:1. Subsequently, the hydrogen-rich syngas is utilized in the ammonia synthesis section to produce ammonia, which is subsequently sent to the Nitric acid and ammonium Nitrate plant.
[0056] Furthermore, the oxygen necessary for the Claus process and the nitric acid plant can be conveniently sourced from the electrolyzer, completing a closed-loop system that underscores efficiency and sustainability in ammonia and ammonium nitrate production.
Example 2:
[0057] Fig. 5 illustrates the block diagram of a method for the production of Methanol from coal with retrofit in accordance with an embodiment of the present disclosure.The method for generating methanol begins with the production of syngas from a coal gasification module, followed by the removal of particulate matter through a dedicated system. Oxygen required for gasification is generated from an electrolyser powered by green energy sources such as wind or solar power, eliminating the need for an air separation unit. The syngas is then directed through a Water Gas Shift (WGS) reactor system, where a portion of the CO is converted into H2 and CO2, aiming to achieve a H2:CO ratio of 2 and an R ratio of 2.
[0058] Following reactions take place for methanol, DME and SNG production.
CO +2H2 ↔ CH3OH
CO2+ 3H2 ↔ CH3OH + H2O
[0059] Typical methanol concentration is 80-90 % by wt and balance water
[0060] For DME production following reactions take place.
2 CH3OH↔ CH3OCH3 + H2O
[0061] Typical concentration of DME is 87-99 %
[0062] For SNG following reactions take place
CO +3H2 ↔ CH4 +H2O
CO2 +4H2 ↔ CH4 +2H2O
[0063] Typical concentration of CH4 is 95-96 % and balance water.
[0064] Subsequently, H2S and CO2 are removed from the syngas using technologies like rectisol or other carbon capture processes, ensuring that H2S concentration remains below 100 ppm and CO2 concentration falls within the range of 1-3% by volume. The pure CO2 separated from the carbon capture system is then combined with hydrogen derived from the electrolyser to produce value-added products such as methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG).
[0065] Finally, the syngas, now purified of H2S and CO2, is fed into a methanol synthesis reactor to undergo the conversion process into methanol. This integrated approach offers a streamlined and environmentally conscious method for methanol production, effectively utilizing renewable energy sources and minimizing carbon emissions throughout the process.
Example 3:
[0066] Fig. 6 illustrates the flow chart of a method for the production of Methanol from coal without shift reactor in accordance with an embodiment of the present disclosure.
[0067] The method for methanol production involves several key steps. Initially, syngas is produced through coal gasification, with a subsequent purification step to remove particulate matter. Notably, the oxygen necessary for gasification is generated by an electrolyzer powered by renewable sources such as wind or solar energy, obviating the need for an air separation unit. Following this, hydrogen from the electrolyzer is carefully blended with syngas to achieve desired ratios without the use of a shift reactor, ensuring a precise H2:CO ratio of 2 and an optimal R ratio of 2.
[0068] Subsequently, impurities such as H2S and CO2 are efficiently eliminated from the syngas through processes like rectisol or other carbon capture methods, achieving stringent thresholds of less than 100 ppm for H2S and maintaining CO2 concentrations within the range of 1-3% by volume. Moreover, the purified CO2 obtained from the carbon capture system is effectively combined with hydrogen from the electrolyzer to yield versatile products such as Methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG).
[0069] Finally, the purified syngas, free from H2S and CO2 contaminants, is directed into a methanol synthesis reactor, where it undergoes the necessary chemical transformations to yield high-quality methanol.

ADVANTAGES OF THE INVENTION

[0070] The proposed method has the following advantages over the contemporary prior arts:
• Enhanced resource utilization: Efficiently utilizes CO2 emissions from the coal gasification process for the production of valuable chemicals like methanol, DME, or SNG.
• Reduced environmental impact: Decreases CO2 emissions by eliminating or reducing the need for steam and water gas shift reactors, as well as air separation units.
• Energy efficiency: Utilizes green energy sources for oxygen generation, reducing reliance on non-renewable energy and improving overall process sustainability.
• Cost-effectiveness: Eliminates or reduces the need for certain equipment and energy-intensive processes, potentially lowering production costs.
• Versatility: Enables the production of multiple valuable chemical products from coal gasification, contributing to the diversification of industrial outputs.

TEST RESULT:

[0071] Low emission Ammonium nitrate(AN) production process via coal gasification where O2 is supplied from electrolyzer using green power and H2 produced from electrolyzer is used to make methanol or DME or SNG .which reduces CO2 emissions from 3.8 kg of CO2/kg of AN to 1.5 kg of CO2 per kg of AN. The 20 %reduction in steam requirement from auxiliary boiler for running air separation unit is achieved which in turn reduces emissions from auxiliary boiler.
[0072] The low emissions Methanol production via coal gasification where the oxygen is supplied from electrolyzer operating on green power to gasifier. The hydrogen from electrolyzer was used to make chemicals like methanol/DME/SNG. The Co2 emissions are reduced from 4 kg of CO2/ kg of methanol to 1.5 kg of CO2 per kg of methanol.
[0073] Another variant of the process for producing methanol from coal, hydrogen from electrolyzer is mixed with syngas from gasification system to produce methanol which reduces CO2 emissions from 4 kg of Co2/kg of methanol to 1.2 kg of Co2 per kg of methanol. This approaches eliminate the need of WGS as well as steam requirement associated with it.
WORKING OF INVENTION:
[0074] The produced Methanol and Ammonium Nitrate can find wide-ranging applications across various industries. Methanol is a versatile chemical used in the production of fuels, solvents, plastics, and other industrial products. Ammonium Nitrate is primarily utilized in the manufacture of fertilizers and explosives, making it crucial for agricultural and mining sectors.
[0075] The above description does not provide specific details of the manufacture or design of the various components. Those of skill in the art are familiar with such details, and unless departures from those techniques are set out, techniques, known, related art or later developed designs and materials should be employed. Those in the art are capable of choosing suitable manufacturing and design details.
[0076] Further, the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. It will be appreciated that several of the above-disclosed and other features and functions, or alternatives thereof, may be combined into other fixture or applications. Various presently unforeseen or unanticipated alternatives, modifications, variations, or improvements therein may subsequently be made by those skilled in the art without departing from the scope of the present disclosure as encompassed by the following claims.
[0077] The claims, as originally presented and as they may be amended, encompass variations, alternatives, modifications, improvements, equivalents, and substantial equivalents of the embodiments and teachings disclosed herein, including those that are presently unforeseen or unappreciated, and that, for example, may arise from applicants/patentees and others.
[0078] It will be appreciated that variants of the above-disclosed and other features and functions, or alternatives thereof, may be combined into many other different fixture or applications. Various presently unforeseen or unanticipated alternatives, modifications, variations, or improvements therein may be subsequently made by those skilled in the art which are also intended to be encompassed by the following claims.
, Claims:We Claim:
1. A method(100) for the production of Ammonium Nitrate and Methanol from coal, the method(100) comprising:
generating(102), syngas from coal gasification, wherein oxygen for gasification is produced by an electrolyzer and particulates are removed from the syngas;
passing(104), the syngas through a water gas shift reactor to produce hydrogen (H2) and carbon dioxide (CO2);
removing(106), hydrogen sulphide (H2S) and CO2 from the syngas using a carbon capture process, wherein the concentration of H2S is less than 100 ppm and the concentration of CO2 is in the range of 0-0.5% by volume;
mixing(108), the pure CO2 from the carbon capture system with hydrogen from the electrolyzer to produce Methanol, Dimethyl Ether (DME), or Synthetic Natural Gas (SNG); and
synthesising(110), into Methanol and Ammonium Nitrate.
2. The method(100) as claimed in the claim 1, wherein oxygen required for the Claus process and nitric acid plant is provided by the electrolyzer powered by green energy from solar or wind sources.
3. The method(100) as claimed in the claim 1, wherein the syngas rich in hydrogen is utilised for ammonia synthesis, followed by Nitric acid and Ammonium Nitrate production.
4. The method(100) as claimed in the claim 1, wherein the syngas is utilised for Methanol synthesis.
5. The method(100) as claimed in the claim 1,wherein methanol can be produced from coal with retrofit or without a Water Gas Shift (WGS) reactor system.
6. The method(100) as claimed in the claim 1, wherein the adjustment of the H2:CO ratio is achieved without using a water gas shift reactor.