System and method for converting waste carbon material into bio-methanol using hydrothermal gasification and catalytic methanol synthesis

Abstract

A system for converting waste carbon material into methanol comprising; a mixing and recirculation tank for receiving the waste material- a hydraulic pumping unit to mix waste carbon material with wat

Description

TECHNICAL FIELD The present disclosure relates generally to systems and methods for hydrothermal gasification and catalytic methanol synthesis; and more specifically, to conversion of waste carbon material into bio-methanol using hydrothermal gasification and catalytic methanol synthesis. In some instances, systems and methods for hydrothermal gasification and catalytic methanol synthesis according to the invention utilise a primary endothermic process and a secondary exothermic continual plug flow process, optionally using a plurality of heating formats and heat recycling technologies. BACKGROUND Globally, waste has become a significant issue in the world. Notably, massive volumes of waste generated annually causes pollution, such as for example, land pollution, water pollution and so forth. Specifically, 6,300,000,000 tons of plastic waste has been generated by humans and the production is expected to increase to 1,800 million tons per year by 2050. Presently, only 9% of plastic waste is recycled, 12% is incinerated and 80% has ended up in landfill. In such a context, attempts have been made to develop several methods for recycling and reusing a plastic waste without pollution, and for effectively utilizing the recycled plastics as resources. Methods for recycling and reusing plastic waste include conversion to char, oil, and / or gas using hydrothermal carbonisation, hydrothermal liquefaction and hydrothermal gasification, respectively. Currently, the heat required to initiate such processes is typically supplied either by combustion of fuels, or electricity. Notably, supplying heat using combustion of fuels from industries or electricity is problematic as the energy return upon creation of char, oil, and / or gas is too costly both energetically and economically. Additionally, the net gain in energy provision comes at the expense of the precombustion of other fuels, negating the formation of a renewable form of char, oil, and / or gas. Electrochemical hydrogen production is achieved by electrolysis of water with a proton exchange membrane, a polymer electrolyte membrane or an anion exchange membrane in low temperature electrolysis or a solid oxide electrolyser in high temperature electrolysis. Disadvantageously, water supply to the electrolyser must be of a high purity, typically with a minimum conductivity of <1 pS cm1 (>1 mQ CM) and total organic carbon of between <10 - <200 pg / L. The transition metals used in electrolysed hydrogen production include oxides of iridium, platinum, scandium, titanium or yttrium, which are expensive and rare earth elements. Hydrogen production from electrolysis typically requires compression which adds to production cost. Worldwide, most production of hydrogen is done via electrolysis of ultra-pure water using renewable electricity. Methanol is a good candidate as a molecular storage medium for hydrogen because it is a liquid at room temperature and pressure and already used both as a bunkering fuel in the shipping industry and as a platform chemical in the chemicals industry. Methanol can be used as a fuel via combustion with internal combustion engines or in fuel cells for electricity generation. Over 99% of worldwide methanol is produced as "grey methanol" derived from steam methane reformation of natural gas. Grey methanol produced via steam methane reformation is problematic because it produces carbon dioxide and consumes methane, which could otherwise be used as a fuel. "Blue methanol" is derived from catalytic methanol synthesis of hydrogen and carbon dioxide gases, hydrogen may be derived from electrolysis and carbon dioxide may be derived from carbon capture. There are few places in the world where hydrogen production and carbon dioxide are in physically close proximity to each other, meaning that distribution adds increasing complexity to blue methanol production and increases energetic and economic costs. Most blue methanol is produced via electrolytically derived hydrogen combined with carbon captured carbon dioxide. Hydrogen can also be produced from thermochemical rather than electrochemical processes, such as hydrothermal processing. Advantageously, energy savings making hydrogen by hydrothermal processing can recycle heat, reducing energy expenditure. Syngas is composed of variable fractions of carbon dioxide, hydrogen, carbon monoxide and methane, and the composition of syngas can be controlled by varying the temperature, pressure, pH, and / or feedstock to water ratio. For example, gas composition of hydrogen in syngas can be increased by modifying pH of the waste carbon source, combined with wastewater or other carbon-based wastewater that is used as a feedstock to make syngas. Therefore, in light of the foregoing discussion, there exists a need to make methanol while reducing or eliminating methane consumption and carbon dioxide production. There is also a need to lower the energetic and economic cost of methanol production. SUMMARY The present disclosure seeks to provide a system for converting waste carbon material into methanol using hydrothermal gasification and catalytic methanol synthesis. In some embodiments, the system is configured to achieve hydrothermal gasification and catalytic methanol synthesis in a single plug flow reactor. The present disclosure also seeks to provide a method for converting waste carbon material into methanol using hydrothermal gasification and catalytic methanol synthesis. An aim of the present disclosure is to provide a solution that overcomes at least partially the problems encountered in the prior art. In one aspect, the present disclosure provides a system for converting waste carbon material into bio-methanol using hydrothermal gasification and catalytic methanol synthesis, the system comprising: (a) a mixing and recirculation tank configured to receive the waste carbon material to undergo hydrothermal gasification; (b) a hydraulic pumping unit configured to mix waste carbon material with water and to increase the pressure of the mixture of waste carbon material and water; (c) a plug flow reactor configured to maintain the pressure of the mixture of the waste carbon material and water; wherein the plug flow reactor comprises: (i) a preheater configured to increase temperature of the mixture of waste carbon material and water to obtain waste flow; and (ii) a hydrothermal reactor unit configured to receive the waste flow from the preheater, wherein the hydrothermal reactor unit is configured to convert the waste flow into syngas and steam; (d) a methanol reactor chamber in fluid communication with the plug flow reactor for receiving the syngas therefrom, the methanol reactor chamber housing a catalyst for converting syngas to methanol; and (e) a heat exchanger configured to recirculate excess heat from downstream of the hydrothermal reactor and from the methanol reactor chamber to the preheater. In some embodiments, the methanol reactor chamber comprises a catalyst support and the methanol reactor chamber is configured to pass syngas over and through the catalyst support. In some embodiments, the catalyst support is a ceramic porous matrix providing a high surface area to volume ratio. In some embodiments, the catalyst support is a zeolite clinoptilolite ceramic porous matrix providing a high surface area to volume ratio. In some embodiments, the catalyst is selected from an oxide of zinc, copper, magnesium, aluminium and iron. In some embodiments, the system further comprises a distillation unit for distilling methanol from water. In some embodiments, the system further comprises a secondary heat exchanger configured to recirculate excess heat from the distillation unit to the preheater. In some embodiments, the plug flow reactor is connected to the methanol synthesis chamber via an interlock. The interlock is able to vent excess water and recycle heat from the hydrothermal gasification process but retain syngas. In some embodiments, the interlock is positioned in an upright position to separate syngas from liquid by density phase separation. In some embodiments, the system comprises a heat exchanger configured to recirculate excess heat from downstream of the hydrothermal reactor and / or the interlock to the preheater and / or the hydrothermal reactor. In some embodiments, the system comprises a heat exchanger configured to recirculate excess heat from downstream of the hydrothermal reactor to the preheater and / or the hydrothermal reactor. In some embodiments, the system comprises a heat exchanger configured to recirculate excess heat from the interlock to the preheater and / or the hydrothermal reactor. In some embodiments, the method comprises adding an alkali catalyst to the waste carbon material. In some embodiments, the plug flow reactor is configured to enable continuous flow of the mixture of waste carbon material and water to the preheater and the hydrothermal reactor unit. In some embodiments, the plug flow reactor is configured to maintain pressure of the waste carbon material and water mixture at about 250 bar. In some embodiments, the plug flow reactor comprises a back pressure valve positioned downstream of the hydrothermal reactor unit. In some embodiments, the hydrothermal reactor unit comprises a heater for increasing the temperature of the waste flow using a plurality of heating formats. In some embodiments, the hydrothermal reactor unit comprises a conduit configured to partially recirculate waste heat into the hydrothermal reactor unit. In some embodiments, the system further comprises a processing electronics module configured to regulate and control flowrates, temperatures and pressures in the system. In some embodiments, the plurality of heating formats in the hydrothermal reactor unit comprises at least one of: steam turbine waste heat; geothermal heat; waste heat from internal combustion engines; solar heat from solar concentrating parabolic troughs; and waste heat from combustion of waste material produced from hydrothermal gasification. In some embodiments, the preheater comprises a second plurality of heating formats to increase the temperature of the mixture of waste carbon material and water. In some embodiments, the plug flow reactor is tubular in structure. In some embodiments, the hydraulic pumping unit comprises a double acting piston. In some embodiments, the hydraulic pumping unit comprises a plurality of hydraulic pumps. In some embodiments, the hydraulic pumping unit comprises a two or more hydraulic pumps, optionally three or more, four or more, five or more, six or more, seven or more, eight or more, nine or more, or ten or more hydraulic pumps. In some embodiments, a temperature capacity of the hydrothermal reactor unit is 700 degrees Celsius, a pressure capacity of the hydrothermal reactor unit is 400 bars and flow rate capacity thereof is 100 kilograms per hour. In some embodiments, the preheater is configured to increase temperature of the mixture of waste carbon material and water up to 500-600 degrees Celsius. In another aspect, the present disclosure provides a method for converting waste carbon material into methanol using hydrothermal gasification and catalytic methanol synthesis, the method comprising: (a) receiving the waste carbon material configured to undergo hydrothermal gasification; (b) mixing waste carbon material with water; (c) increasing pressure of mixture of the waste carbon material and water using a hydraulic pumping unit to provide a pressurised mixture of waste carbon material and water; (d) transferring the pressurised mixture of waste carbon material and water to a plug flow reactor comprising a preheater and a hydrothermal reactor unit, wherein the plug flow reactor is configured to maintain the pressure of the mixture of the waste carbon material and water; (e) increasing temperature of the mixture of waste carbon material and water in the preheater to obtain waste flow; (f) converting the waste flow into syngas and steam in the hydrothermal reactor unit by increasing the temperature of the waste flow; (g) transferring the syngas to a methanol reactor chamber housing a catalyst for converting syngas to methanol and contacting the syngas with the catalyst under conditions suitable for the production of methanol; and (h) recirculating excess heat from the methanol reactor chamber to the preheater via a heat exchanger. In some embodiments, the waste flow is converted into supercritical and / or superheated steam. In some embodiments, the method of the invention is performed using the system of the invention. In some embodiments, the method further comprises distilling methanol from water in a distillation unit. In some embodiments, the method further comprises recirculating excess heat from the distillation unit to the preheater. In some embodiments, the method comprises adding an alkali catalyst to the waste carbon material. In some embodiments, the method comprises transferring syngas to a methanol reactor chamber via an interlock configured to separate syngas from liquid. In some embodiments, the method comprises recirculating heat from downstream of the hydrothermal reactor and / or the interlock to the preheater and / or the hydrothermal reactor via a heat exchanger. In some embodiments, the method comprises recirculating heat from downstream of the hydrothermal reactor to the preheater and / or the hydrothermal reactor via a heat exchanger. In some embodiments, the method comprises recirculating heat from downstream of the interlock to the preheater and / or the hydrothermal reactor via a heat exchanger. In some embodiments, increasing the temperature of the waste flow comprises using a plurality of heating formats. In some embodiments, the method comprises recirculating waste heat from the hydrothermal reactor unit into the waste flow. In some embodiments, the method further comprises decreasing temperature and pressure of the syngas and / or methanol. In some embodiments, the plurality of heating formats comprise at least one of: steam turbine waste heat; geothermal heat; waste heat from internal combustion engines; solar heat from solar concentrating parabolic troughs; and waste heat from combustion of waste material produced. In some embodiments, the preheater comprises a second plurality of heating formats to increase the temperature of the mixture of waste carbon material and water. In some embodiments, the method comprises increasing the temperature of the waste flow up to 600 degrees Celsius and pressure thereof up to 250 bars in the absence of oxygen. In some embodiments, the method comprises increasing temperature of the mixture of waste carbon material and water up to 600 degrees Celsius. Embodiments of the present disclosure substantially eliminate or at least partially address the aforementioned problems in the prior art, and enable efficient conversion of waste carbon material into methanol. In the system of the invention, the hydrothermal gasification reactor is part of a plug flow reactor which forms a single pressure chamber continuum. In some embodiments, the hydrothermal gasification reactor and catalytic methanol synthesis chamber are part of a plug flow reactor which forms a single pressure chamber continuum. Advantageously, the use of a single continuous pressure chamber (referred to herein as the plug flow reactor) allows the use of less equipment and enables lower-cost processing as compared to modular systems. The continuous plug flow reactor also reduces issues associated with restriction and / or modification of flow rate and internal pressure changes between adjacent chambers of a modular system, because pressure is maintained at a constant level throughout the plug flow reactor. A further benefit of the plug flow reactor is that pressure can be regulated independently of temperature and / or super-heated steam or supercritical steam accumulation by means of the hydraulic pumping unit at the input end of the plug flow reactor, and a back pressure valve at the output end of the plug flow reactor. The ability to control pressure within the plug flow reactor via the hydraulic pumping unit enables the system of the invention to be used to produce various desired outputs, e.g. char, oil, and / or gas from hydrothermal carbonisation, hydrothermal liquefaction and hydrothermal gasification respectively. Thus, the system of the invention is simple, resilient, and adaptable. Importantly, the system of the invention is not limited to hydrothermal gasification reactions. In some embodiments, the plug flow reactor comprises a back pressure valve at the output end. Back pressure valves are not routinely used on multi-phase flow materials, i.e. solid, liquid and gas mixtures, because they can clog. The high pressure and temperature achieved by the plug flow reactor of the invention results in changes to the material states of the waste carbon material from solid at the input end to liquids and gases at the output end. Therefore, by the time the waste carbon material reaches the back pressure valve, solids that cannot conventionally go through a back pressure valve due to the problem of clogging have been converted into liquids that can easily pass through the back pressure valve at the outlet end. Advantageously, the hydraulic pumping unit results in less equipment and lower-cost processing methodologies than systems requiring a single or double hydraulic peristaltic pump. In some embodiments, feedstock intake is by means of negative pressure air chamber and back pressurisation intake valves directly into the mixing and recirculation tank that can act in synchronicity with cyclical hydraulic piston injection of waste feedstock. The plug flow reactor comprises regions with distinct heating profiles, e.g. the heated hydrothermal reactor and the subsequent cooling zone. In some embodiments, regions with distinct heating profiles are isolated by thermal barriers, e.g. heat-blocking thermal barriers. In some embodiments, heat-blocking thermal barriers isolate the cross-sectional surface area of the reactor chamber throughput the hydrothermal gasification reaction heating and cooling zones (comprising lower temperature thermal barriers) such as water / ethylene glycol or other organic liquid mixtures. These thermal barriers advantageously circumnavigate the prerequisite utilisation of more expensive internal pressure flow valves which are tolerant to high extremes of both pressure and temperature. Consequently lower-cost pressure valves are able to be utilised at lower thermal tolerance and pressure criterion and with less specialist material characteristic outside of the zones of higher heat and pressure. Thermal barriers are constituted by multiple physical manifestations, as external conductive heating, insulation and coolant zones. In some embodiments, the system comprises inverter-controlled resistance heating or induction heating over the whole length of the plug flow reactor. This ensures that the primary heating system provides the bulk of the heating with insulation and maintenance heating on the output end, maintaining the reaction conditions at the desired temperature. With cost-effective insulation, the plug flow reactor of the invention has the capacity to be versatile and extend the active conditions of the reactor pressure and temperature zones, especially given the wall thickness required to maintain the high pressure of the reactor and proceeding pressure tubes and low thermal conductivity of stainless steel. In some embodiments, the thermal conductivity of the hydrothermal reactor is increased by provision of an aluminium block heater over the hydrothermal reactor. This aluminium block provides an inversed heat sync, which helps get heat into the reactor through the external reactor vessel walls directly and cost effectively, without excessive heat loss to the environment, thereby maximising energy consumption and utilisation. In some embodiments, the system comprises a "hot-valve" at the output end of the plug flow reactor. During priming of the system upon first use and when the reactor contents are exposed to atmospheric air, the detrimental effects of oxygen accumulation from air into the portion of the equipment downstream of the reactor can be negated, as well as ensuring that the reactor is maintained at the optimised operational pressure of 150 bar during "heat-up" from ambient to 350C. It is important to ensure that the system can be pressurised before, and during heating, because failure to do so exposes waste carbon material to hydrothermal carbonisation forming temperatures at 150-250C and <120 bar (char or charcoal-like formation). Consequently, the system of the invention enables the user to control product formation, maximising oil and aqueous fractions without undesired char formation that could potentially and detrimentally block the back pressure valve. The system of the invention typically provides for linear flow of waste feedstock through at least four zones: a cold waste feedstock intake zone; a pre-heat zone; a heat maintenance zone including the hydrothermal reactor; and a cooling zone following the hydrothermal reactor. The system of the invention facilitates multiple combination set-ups comprising variable volumetric reactor chambers, temperature profiles and heating methods. These are constituted by multiple volumetric reaction chambers enabled to be re-positioned for smaller or larger experiments. Consequently, hydrothermal pyrolysis, liquefaction or gasification at a range of temperatures between ambient and 700°C; are able to be provided with multiple heating inputs from either fuels', electricity or solar energy. Advantageously, this reactor system is able to be operationally processed within 2 hours, with a 20-minute turnaround time in between variable configurations of experiments. This set-up enables operatives to increase frequency rate and experimental research into hydrothermal liquefaction, pyrolysis and gasification technologies without requiring separate equipment to specialise these activities. Additional aspects, advantages, features and objects of the present disclosure would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present disclosure are susceptible to being combined in various combinations without departing from the scope of the present disclosure as defined by the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present disclosure, exemplary constructions of the disclosure are shown in the drawings. However, the present disclosure is not limited to specific methods and instrumentalities disclosed herein. Moreover, those skilled in the art will understand that the drawings are not to scale. Wherever possible, like elements have been indicated by identical numbers. Embodiments of the present disclosure will now be described, by way of example only, with reference to the following diagrams wherein: FIG.l is a schematic representation of an exemplary system according to the invention comprising a mixing and recirculation tank, hydraulic pumping unit, plug flow reactor with preheater, hydrothermal liquefaction reactor, back pressure valve, methanol reactor chamber and heat exchanger. FIG. 2 is a flowchart depicting steps of a method for converting waste carbon material into biomethanol using hydrothermal gasification and catalytic methanol synthesis, in accordance with an implementation of the present disclosure. In the accompanying drawings, an underlined number is employed to represent an item over which the underlined number is positioned or an item to which the underlined number is adjacent. A nonunderlined number relates to an item identified by a line linking the non-underlined number to the item. When a number is non-underlined and accompanied by an associated arrow, the nonunderlined number is used to identify a general item at which the arrow is pointing. DETAILED DESCRIPTION OF EMBODIMENTS The following detailed description illustrates embodiments of the present disclosure and ways in which they can be implemented. Although some modes of carrying out the present disclosure have been disclosed, those skilled in the art would recognize that other embodiments for carrying out or practising the present disclosure are also possible. The present disclosure provides the aforementioned process, system and method for efficient conversion of waste carbon material into syngas and methanol via hydrothermal gasification and catalytic methanol synthesis. Specifically hydrothermal gasification is a waste processing technology. Waste carbon comprises multiple formats and forms. In the present disclosure, temperature capacity of the hydrothermal gasification unit will reach supercritical water conditions, wherein the heater may be powered by waste heat from industries, solar heat, and waste heat from combustion of waste material from the hydrothermal gasification unit. Notably, the present disclosure has potential for upscaling from 10 kg per hour to 10,000 tonnes per hour. Throughout the present disclosure, the term "hydrothermal gasification" refers to a thermochemical process within an enclosed hydrothermal reactor to convert waste carbon materials into syngas. Throughout the present disclosure, the term "methanol synthesis" refers to a thermochemical process within an enclosed syngas reactor to convert syngas into methanol and water. Hydrothermal gasification is typically carried out at optimal temperature of 500-600°C and 250 bar in the absence of oxygen. Furthermore, hydrothermal gasification is a fast process with a low residence time. Herein the term "residence time" is defined as the average length of time during which a mixture of waste carbon material and water is within a hydrothermal gasification unit. Furthermore the system described herein enables pressure and temperature to be vary to accommodate heating up, residence time and cooling down periods during startup, running and shutdown, respectively. Throughout the present disclosure, the term "waste carbon material" refers to carbon-rich resources that are generally discarded as unusable materials or trash. Herein, the waste carbon material may include any carbon material in a solid, liquid or gaseous state. Furthermore, the waste carbon material in the present disclosure may include, but is not limited to, solid products, liquid products, municipal solid waste, urban waste, forestry waste, plant materials, marine or freshwater macroalgae or microalgae, wood waste, fermentation waste, by-product of bio-crude, plastic waste, polymer waste, food waste, food process waste, sewage sludges, livestock waste, agricultural waste, plural waste, or combinations thereof. The system comprises a preheater configured to increase the temperature of the mixture of waste carbon material. Advantageously, excess heat from downstream of the hydrothermal reactor, the interlock and / or the exothermic methanol synthesis reactor is recirculated into the preheater. Hence the hydrothermal reactor can utilise both waste industrial or solar thermal heat, and recycled heat in-situ from downstream of the hydrothermal reactor, the interlock and / or the output of the methanol synthesis reactor via heat exchangers. Furthermore, recirculating heat from downstream of the hydrothermal reactor, the interlock and / or the methanol synthesis reactor into the preheater for hydrothermal gasification ensures the waste carbon material is preheated prior to attaining temperature required for conversion into syngas in the hydrothermal reactor. Hence the external demand for heat input into the hydrothermal reactor is reduced by making use of the heat generated within the system. Optionally, the preheater comprises a plurality of heating formats to increase the temperature of the mixture of waste carbon materials. Herein, the term "plurality of heating formats" refers to steam turbine waste heat, geothermal waste heat, waste heat from exhaust gas internal combustion engines used in industries, solar heat and waste heat produced during the combustion of byproducts of hydrothermal gasification, and any combination thereof. Furthermore, the plurality of heating formats may comprise oil and gas fuels with electrical and solar integration options. Optionally, the preheater is configured to increase the temperature of the mixture of waste carbon materials up to 600 °C. Subsequently, the mixture of waste carbon materials is exposed to reaction temperatures and pressures and transported under pressure to the hydrothermal gasification unit. The conduit of the hydrothermal gasification unit may be connected in tandem to the methanol synthesis unit via an interlock. The interlock is able to vent excess water and recycle heat from the hydrothermal gasification process but retain syngas. The interlock is typically positioned in an upright position to separate syngas from liquid by density phase separation. The interlock may contain actuated or manual control valves. Beneficially, the interlock is typically situated between the hydrothermal gasification reactor and the catalytic methanol synthesis reactor and the catalytic methanol reactor chamber is exposed to mainly input syngas, as the bulk of the post-hydrothermal gasification water is vented in the interlock and heat is recycled. A heat exchanger and / or chiller may be located between the interlock and the catalytic methanol reactor. The heat exchanger may function to reduce the temperature of the syngas within the catalytic methanol reaction chamber. For example, the heat exchanger may function to reduce the temperature of the syngas within the catalytic methanol reaction chamber from about 500°C to about 5°C. , e.g. from about 450°C, about 400°C, about 350°C, about 300°C, about 250°C, about 200°C, about 150°C, or about 100°C to about 10°C, about 20°C, about 30°C, about 40°C, about 50°C, about 60°C, about 70°C, about 80°C, or about 90°C. The catalytic methanol reaction chamber is in fluid communication with the hydrothermal gasification reactor. The catalytic methanol reaction chamber allows syngas to pass over a catalyst support containing a catalyst. The catalytic methanol reaction chamber ensures that all syngas in communication with and downstream of the hydrothermal gasification reactor passes over the catalyst and catalyst support in a plug flow continual process. The catalyst support maximises the surface area to volume ratio of exposure of the syngas mixture originating from the hydrothermal gasification reactor thereby promoting the catalytic reaction of hydrogen and carbon dioxide to form methanol and water. In some embodiments, the catalyst is selected from oxides of zinc, copper, magnesium, aluminium and iron. In some embodiments, the catalyst support is a ceramic porous matrix providing a high surface area to volume ratio. In some embodiments, the catalyst support is a ceramic zeolite clinoptilolite porous matrix providing a high surface area to volume ratio. The pH of the waste carbon material may be modified by addition of sodium hydroxide, sodium carbonate, potassium hydroxide, potassium carbonate or sodium bicarbonate. In some embodiments, the method comprises adding an alkali catalyst to the waste carbon material. Advantageously, the inclusion of alkali catalysts to the waste carbon material increases the production of hydrogen and reduces the production of carbon dioxide in the syngas. The inclusion of alkali catalysts may be controlled proportionally to the waste carbon material and water ratio within the waste carbon mixture of the feedstock into the hydrothermal gasification unit to optimise the production of both hydrogen and carbon dioxide in the syngas. The inclusion of alkali catalysts to the waste carbon material mixture can optimise the stoichiometric ratio of carbon dioxide to hydrogen production in the syngas to ensure that it provides the optimal conversion into methanol downstream of the hydrothermal gasification reactor and in the methanol synthesis reactor. The pressure of the syngas may be controlled at about 200-300 bar in the catalytic methanol reactor to ensure optimal stoichiometric conversion of carbon dioxide and hydrogen into methanol. For example, the pressure of the syngas may be controlled at about 200, 225, 250, 275 or 300 bar in the catalytic methanol reactor to ensure optimal stoichiometric conversion of carbon dioxide and hydrogen into methanol. The temperature of the syngas may be controlled at between 5°C- 250°C in the catalytic methanol reactor to ensure optimal stoichiometric conversion of carbon dioxide and hydrogen into methanol. For example, the temperature of the syngas may be controlled at between about 5°C, about 10°C, about 20°C, about 30°C, about 40°C, about 50°C, about 60°C, about 70°C, about 80°C, about 90°C, or about 100°C and about 110°C, about 120°C, about 130°C, about 140°C, about 150°C, about 160°C, about 170°C, about 180°C, about 190°C, about 200°C, about 210°C, about 220°C, about 230°C, about 240°C, or about 250 °C in the catalytic methanol reactor to ensure optimal stoichiometric conversion of carbon dioxide and hydrogen into methanol. The methanol synthesis reaction in the catalytic methanol reactor is exothermic and the system of the invention advantageously extracts heat generated by the methanol reactor and recirculates it to the hydrothermal gasification preheater and / or the hydrothermal reactor via a heat exchanger. Beneficially, this reduces the external energy demand of the hydrothermal gasification reactor, thereby reducing the energetic cost of methanol production. Additionally, the system of the invention presents scientists and academics, with a professional scientific apparatus for processing waste feedstocks whereby the scientists and the academics will be able to assess and analyse multiple batches of waste carbon material samples sequentially in a system comprising continuous hydrothermal gasification. Notably, the system of the invention has potential for upscaling via steam turbine electricity generation. Herein, the steam turbine electricity generation has capacity to upscale the potential of the system of the invention from the professional scientific apparatus of 100 litres per hour to 10,000 tonnes per hour steam turbine derived heat source hydrothermal gasification production system. Advantageously, the system of the invention enables multiple series of experiments with different variables to be performed in a short time, due to the ability for the equipment to be emptied, cleaned, re-filled and re-operated in quick succession. Furthermore, the system used for hydrothermal gasification and catalytic methanol synthesis in the present disclosure is well suited to lower production throughputs analogous to academics comprising research and development, wherein flow rate may be maintained from 1 kilogram per hour up to 50 kilograms per hour. The flow rate may for example be maintained at 1,15, 30 or 45 kilograms per hour up to 15, 30, 45 or 50 kilograms per hour. Additionally, the system of the invention may be upscaled and used for hydrothermal gasification and catalytic methanol synthesis which is aligned to higher production throughputs analogous to the steam turbine derived heat source hydrothermal gasification and catalytic methanol production system, wherein the flow rate may be maintained from 100 kilograms per hour up to 10,000 tonnes per hour. Moreover, the system used for hydrothermal gasification in the present disclosure may fluctuate between different pressures and temperatures to accommodate different types of waste carbon material and therefore accommodate either hydrothermal carbonisation or hydrothermal liquefaction, or pyrolysis. Herein, approximate temperature for hydrothermal carbonisation is 150 degrees Celsius up to 250 degrees Celsius, for hydrothermal liquefaction is 250 degrees Celsius up to 370 degrees Celsius, for hydrothermal gasification is 370 degrees Celsius up to 600 degrees Celsius, and for pyrolysis is 500 degrees Celsius up to 800 degrees Celsius. The approximate temperature for hydrothermal carbonisation may be from 150,175, 200 or 225 degrees Celsius up to 175, 200, 225 or 250 degrees Celsius. The approximate temperature for hydrothermal liquefaction may be from 250, 275, 300, 325 or 350 degrees Celsius up to 275, 300, 325, 350 or 370 degrees Celsius. The approximate temperature for hydrothermal gasification may be from 370, 375 or 380 degrees Celsius up to 375, 380, 400, 500 or 600 degrees Celsius. The approximate temperature for pyrolysis may be from 500, 550, 600, 650 or 700 degrees Celsius up to 550,600, 650, 700, 750 or 800 degrees Celsius. The system comprises a mixing and recirculation tank configured to receive the waste carbon material to undergo hydrothermal gasification. In some embodiments, the mixing and recirculation tank contains a small amount of pre-existing water to be mixed with waste carbon material. In some embodiments, waste carbon material is mixed with water in the mixing and recirculation tank at a temperature from 60 degrees Celsius up to 90 degrees Celsius. The mixing and recirculation tank may for example contain water mixed with waste carbon material at temperatures of at least 60°C, at least 65°C, at least 70°C, at least 75°C, at least 80°C, or at least 85°C. The mixing and recirculation tank may for example contain water mixed with waste carbon material at temperatures of up to 70°C, up to 75°C, up to 80°C, up to 85°C, or up to 90°C. Furthermore, the mixing and recirculation tank may have a capacity of 30 litres. The mixing and recirculation tank may have a capacity of at least 30 litres, at least 40 litres, at least 50 litres, at least 60 litres, at least 70 litres, at least 80 litres, at least 90 litres, or at least 100 litres. In some embodiments, the system is configured for industrial scale methanol production and the mixing and recirculation tank has a capacity of at least 1000 tonnes; optionally at least 2000, at least 3000, at least 4000, at least 5000, at least 10,000, at least 15,000, or at least 20,000 tonnes. In some embodiments, a motor is operatively coupled with the mixing and recirculation tank. In some embodiments, the motor is used for thorough mixing of the waste carbon materials with the small amount of pre-existing water. In some embodiments, the mixing and recirculation tank is a partially negative pressurized vessel. Advantageously, a negatively pressurized mixing and recirculation tank promotes injection of the waste carbon material into the hydraulic piston chamber during refilling of the piston stroke. Moreover, the mixing and recirculation tank acts as a pre-feeder into a hydraulic pumping unit. In some embodiments, the waste carbon material is introduced into the mixing and recirculation tank by a piston plunger. The system comprises a hydraulic pumping unit configured to mix waste carbon material with water and to increase the pressure of the waste carbon material and water mixture. The hydraulic pumping unit typically comprises a hydraulic chamber for receiving waste carbon material from the mixing and recirculation tank and water, and a hydraulic piston for compressing the waste carbon material within the hydraulic chamber. The hydraulic chamber typically comprises: (a) a feed intake chamber valve through which waste carbon material enters the hydraulic chamber; and (b) a manually or automatically activated hydraulic valve for releasing the pressurised waste carbon material and water mixture from the hydraulic chamber into the plug flow reactor. When the piston moves forward, the feed intake chamber valve is closed and the hydraulic valve at the end of the hydraulic pumping unit is open. When the piston moves back the hydraulic valve at the end of the hydraulic pumping unit is closed and the feed intake chamber valve is open. The two valves thus operate in asymmetric synchronicity, i.e. one is open when the other is closed. As described above, the waste carbon material is pressurized by the hydraulic piston before entering a plug flow reactor via an ambient temperature manually or automatically actuated hydraulic valve. The hydraulic valve separates the cold pressurised zone from the hot pressurised zone via the cooling thermal barrier on the outlet end of the hydraulic valve. Beneficially, this means that heat is concentrated in the reaction zone and does not permeate backwards due to the forward motion of the pressurised waste carbon material and water mixture being heated. The hydraulic piston creates the pressure. The plug flow reactor provides the thermal barrier and pressure tolerance to maintain the desired heat and pressure for the duration of the reaction. In some embodiments, the pressure is maintained at 200 bars. In some embodiments, the system of the invention can tolerate ranges of pressure between 50 bar and 300 bar, with ideal pressure of between 100 and 200 bar. Additionally, the hydraulic pumping unit may have a capacity of at least 10 litres. Moreover, the hydraulic pumping unit may have a power capacity of 10 Kilowatts. In some embodiments, the hydraulic pumping unit has a hydraulic fluid flow of between 20 and 200,000 litres per hours, optionally between 100 and 200,000, between 500 and 200,000, between 1000 and 200,000, between 5000 and 200,000, between 10,000 and 200,000, between 50,000 and 200,000, between 20 and 150,000, between 20 and 100,000, or between 20 and 50,000 litres per hour. In some embodiments, the hydraulic pumping unit has a hydraulic system pressure of between 2 and 200 bar, optionally between 5 and 200 bar, between 10 and 200 bar, between 25 and 200 bar, between 50 and 200 bar, between 75 and 200 bar, between 2 and 175 bar, between 2 and 150 bar, between 2 and 125 bar, or between 2 and 100 bar. In some embodiments, the hydraulic pumping unit has a hydraulic system power of between 2 and 200 kWh, optionally between 5 and 200 kWh, between 10 and 200 kWh, between 25 and 200 kWh, between 50 and 200 kWh, between 75 and 200 kWh, between 2 and 175 kWh, between 2 and 150 kWh, between 2 and 125 kWh, or between 2 and 100 kWh. In some embodiments, the hydraulic pumping unit is coupled with a high-pressure pump. In some embodiments, the high pressure pump pumps waste carbon and water material into the hydraulic pumping unit hydraulic chamber under partial negative pressure of the negative pressurized vessel via a linking conduit containing a hydraulic valve. The hydraulic valves at the end of the piston and at the end of the high pressure waste carbon feed pump act in alternating unison - i.e. upon beginning forward motion and pressurisation of the hydraulic pumping unit, the high pressure waste carbon feed intake pump valve is closed, and the hydraulic valve on the outlet of the hydraulic pumping unit connecting to the reaction chamber is open. Conversely, at the end of the hydraulic piston stroke and upon the return of the piston head stroke to a subsequent hydraulic refill charge, the hydraulic valve on the outlet of the hydraulic pumping unit connecting to the reaction chamber is closed, and the high pressure waste carbon feed intake pump valve is open, to re-charge the hydraulic pumping unit with waste carbon and water material. Herein, pressure in the high-pressure pump is maintained from 100 bars up to 400 bars. The pressure may for example be maintained at 100, 150, 200, 250, 300 or 350 bars up to 150, 200, 250, 300, 350 or 400 bars. Specifically, the waste carbon material may be maintained at pressure of 150 bars for the duration of residence time. In an embodiment, the hydraulic pumping unit is operatively coupled with a flow control unit. The flow control unit is a function of volumetric capacity measured by the known cross-sectional area, length and hence volume of the piston cycle. A length-rule marker on the piston and the time for the piston to complete its cycle enables the operator to know how much volume of waste carbon material has entered the chamber, as a result of the waste to liquids mixture ratio make-up in the mixing tank. Additionally the flow control unit may be supported by either constant or pulsed hydraulics that can either be constant or timed with 3 seconds on, 57 seconds off; or 5 seconds on, 55 seconds off; or 20 seconds on, 40 seconds off etc. Herein, the flow control unit comprises a processing electronics module to control the flow of the waste carbon material. In some embodiments, the waste carbon material flows from the mixing and recirculation tank (or a feed recharge cylinder located between the mixing and recirculation tank and the hydraulic chamber) to a feeder head and feed cylinder. Herein, the hydraulic slave cylinder is a smaller cylinder connected to the high-pressure pump. The hydraulic pumping unit completes successive piston charges, but does not "know" when a piston cycle has been completed. To mitigate this, an added feature of a control return switch engages at the culmination of each piston cycle, interceding with the electronic interface system to return the piston to its refill charge position. As the piston gets to the end of its cycle, it pushes against an electronic control push switch, sending a signal for the piston to return to its start position. Furthermore, the hydraulic slave cylinder and the high-pressure pump are parts of the hydraulic pumping unit for engaging a clutch. Subsequently, when the clutch is pushed, a plunge inside the high-pressure pump forces high pressure through to the hydraulic slave cylinder. Additionally, a piston indicator is operatively coupled to the hydraulic slave cylinder. Herein, the piston indicator is a mechanical indicator comprising piston, spring, stylus and recording system. Typically, the piston indicator indicates the volume of the waste carbon material when the waste carbon material pushes against the spring, creating a linear relationship between the pressure of the volume of the waste carbon material and deflection of the piston against the spring. The pressurised waste carbon material and water mixture exits the hydraulic pumping unit via the hydraulic valve and enters the plug flow reactor. The plug flow reactor is configured to maintain the pressure of the mixture of waste carbon material and water. Herein, the plug flow reactor may be configured as one long tube or a number of shorter tubes for reconfiguration. Furthermore, the mixture of waste carbon material and water is introduced to the plug flow reactor continuously and moves through the plug flow reactor. Additionally, the plug flow reactor comprises a forward flow rate and a reverse flow rate. Herein, the forward flow rate may have a value of 1 litre per minute, and the reverse flow rate may possibly have a value of 5 litres per minute. It will be understood that the faster reverse flow rate typically enables the piston head to complete its return and feedstock filling stroke faster than the forward pressurisation and feedstock injection stroke. Once feedstock enters the plug flow reactor it only shunts forward, there is no reverse flow as described below. In some embodiments, the plug flow reactor comprises a feeder head. The feeder head is the intermediary ported component between the hydraulic pumping unit, plug flow reactor and mixing and recirculation tank. The feeder head provides adjacent port way entry into the hydraulic valve on the outlet of the hydraulic pumping unit and the high pressure waste carbon feed intake pump valve. The physical design structure configuration of the feeder head is manufactured so that upon reverse refilling with waste carbon and water material, the material easily refills the hydraulic chamber. Additionally, upon pumping waste material forward into the reaction chamber, the design structure facilitates this movement. Herein, thecapacity of the feeder head is upto 400 bars. Subsequently, the feeder head is mechanically coupled a three-way feed valve, wherein the three-way feed valve is mainly used for two-way usage. Furthermore, a feed recharge cylinder is operatively coupled to the feeder head via the three-way feed valve. Herein, the feed recharge cylinder may have a capacity of 10 litres. It will be understood that in industrial scale applications, the feed recharge cylinder may have a capacity of at least 100 litres, e.g. at least 200, at least 300, at least 400, at least 500, at least 600, at least 700, at least 800, at least 900, or at least 1000 litres. In some embodiments, the feeder head is operatively coupled with a pressure isolating valve. Herein, the pressure isolating valve allows to perform maintenance without shutting any line. Thereafter, the pressure isolating valve is further connected to a pressure sensor, wherein the pressure sensor is controlled by the processing electronics module. Optionally, the plug flow reactor is tubular in structure. Optionally the plug flow reactor is oval in structure. Herein, the plug flow reactor comprises a conduit possessing an input end and an output end. Furthermore, the conduit may be made of stainless steel, or nickel-alloy composite stainless steel, or Inconel 741, Inconel 625 or stainless steel. Typically, the internal space of the conduit contains the mixture of waste carbon material for hydrothermal gasification to occur. Additionally, the mixture of waste carbon material flows from the input end of the conduit to the output end of the conduit. In some embodiments, the hydraulic pumping unit comprises a double acting piston. Herein, the double acting piston moves and with each cycle a known volume of the mixture of waste carbon material and water is transported. Furthermore, the double acting piston comprises a first piston head and a second piston head. Herein, the first piston head may have a larger diameter than the second piston head. In some embodiments, the first piston head has a diameter that is at least double the diameter of the second piston head, e.g. the first piston head may have a diameter of 200 millimetres and the second piston head may have a diameter of 100 millimetres. In some embodiments, the first piston head has a diameter that is at least three times the diameter of the second piston head, optionally the first piston head has a diameter that is at least four times the diameter of the second piston head. Beneficially, a reduction in surface area of the second piston head in contact with the feedstock results in a lower pressure requirement from the first hydraulic piston which is proportional to the differential in surface area between the two piston heads. Additionally, a tally counter of the double piston movement corresponds to a shunted flow rate, depending on length of the tubular plug flow reactor and pre-designated temperature and pressure profiles. Moreover, an automatic valve actuator is interfaced with a thermocouple feedback startstop regulatory mechanism which senses thermostatic control of pressure, temperature and flow rate according to desired values for the mixture of waste carbon material and water. In case the temperature of the mixture of waste carbon material and water is higher than required, the flow rate of the plug flow reactor may be increased. Conversely, in case the temperature of the mixture of waste carbon material and water is lower than required, the flow rate of the plug flow reactor may be decreased. Additionally, during the forward movement of the double acting piston, the mixture of waste carbon material and water is discharged from a feed cylinder into a discharge line. Simultaneously, a cylinder behind the double acting piston is being filled with the mixture of waste carbon material and water through an inlet valve of the cylinder. In some embodiments, the hydraulic pumping unit comprises a plurality of hydraulic pumps acting in tandem, threefold, fourfold, fivefold or sixfold. Beneficially, more than one hydraulic pumps acting in tandem converts a shunted plug flow into a continual plug flow process by avoiding the time taken for the hydraulic piston to return to its starting position. Advantageously, more than two hydraulic pumps acting in unison allows one hydraulic pump to be offline for replacement of seals or component parts while avoiding the need to shutdown the whole system. For example, three or more hydraulic pumps acting in unison allows at least two hydraulic pumps to be offline for replacement of seals and / or component parts while avoiding the need to shutdown the whole system. In some embodiments, hydraulic pumps may be connected by a manifold to connect the hydraulic pumps to the plug flow reactor system. The system comprises a preheater configured to increase temperature of the mixture of waste carbon material and water in the plug flow reactor to obtain waste flow. Herein, the preheater acts as a precursor to increase the temperature of the mixture of waste carbon material and water before entering hydrothermal reactor unit. Furthermore, preheating ensures that the mixture of waste carbon material and water is pre-heated to temperatures that do not compromise the integrity or durability of the valves or seals of hydraulic valves before heating it further in the hydrothermal reactor unit. Hence, the hydrothermal reactor unit need not expend much energy to increase the temperature of the mixture of waste carbon material and water. Advantageously, excess heat from downstream of the hydrothermal reactor, the interlock and / or the exothermic methanol synthesis reactor is recirculated into the preheater thereby reducing the external energy demand of the preheater. There exists a myriad of heating applications and sources being heated. In the plug flow reactor system of the invention, the application of heating is simplified because it is heat from the outside going into the middle of the reactor. In some embodiments, the heat is conductive heat via electrical heating elements. In some embodiments, the heat is inductive heating acting via a magnetic interface mechanism directly onto the outside metal of the reaction chamber. In some embodiments, the heat is thermal and visible light concentrated by the focal point of a solar parabolic trough. In some embodiments, the heat is industrial exhaust waste heat from coal, oil, gas, or other fuel combustion. In some embodiments, the heat is geothermal heat from a hot spring, geyser or volcanic rock. In some embodiments, the heat is direct heat from combustion, rather than exhaust from combustion. The number of heating elements affects the rate at which the heater gets to the desired temperature, typically 500-600 °C. Optionally, the preheater is configured to increase temperature of the mixture of waste carbon material and water up to 600 degrees Celsius. Herein, the preheater is mechanically coupled with the plug flow reactor. In some embodiments, the preheater is heated up to 350 degrees Celsius so that the mixture of waste carbon material and water require less supplementary heat to maintain at holding temperature for the duration of the hydrothermal gasification reaction. Subsequently, the mixture of waste carbon material and water present inside the preheater is transported to a hydrothermal reactor unit via the pressure created by the hydraulic pumping unit. The hydraulic pumping unit controls the flow rate of mixture throughout the plug flow reactor. In some embodiments, the input end of the conduit of the plug flow reactor acts as a preheater to rapidly increase the temperature of the conduit to 500-600 degrees Celsius. Furthermore, in some embodiments, the output end of the conduit of the plug flow reactor acts as a preheater to rapidly increase the temperature of the conduit to 500-600 degrees Celsius. In some embodiments, the plug flow reactor comprises a cooling tank for cooling the products of the hydrothermal gasification reaction. Furthermore, a cooling tank may be used to thermally isolate the plug flow reactor. Additionally, the cooling tank may be operatively coupled with a chiller which operates at 4 degrees Celsius. Moreover, the cooling tank may be operatively coupled with a hydrothermal reactor unit. The cooling tank acts as a heat exchanger or heat transfer unit. The cooling tank at the output end of the hydrothermal gasification reactor collects heat from the output of the hydrothermal gasification reactor and recirculates it, returning it to the pre-heater. Advantageously, this means that both insulated heat and excessive waste latent heat are regenerated and reutilised within the reactor configuration. The cooling tank typically reduces the temperature of the waste carbon material (now converted into crude oil) from 500-600°Cto <80°C. The system comprises a hydrothermal reactor unit configured to receive the waste flow from the preheater, wherein the hydrothermal reactor unit is configured to convert the waste flow into syngas and steam, e.g. supercritical and / or superheated steam. Herein, the hydrothermal reactor unit is used to carry out hydrothermal reaction at high pressure and at a high temperature. Beneficially, the hydrothermal reactor unit reduces cycle times, reduces transfer compositions of the waste flow and increases productivities to procure better yields. Notably, the hydrothermal reactor unit is an adaptable research unit, wherein scientists may research hydrothermal gasification in a fully automatic microsystem. Furthermore, the hydrothermal reactor unit may have a cooling unit, such as for example a fan, mechanically coupled on the outer periphery of the hydrothermal reactor unit. Herein, the fan is mechanically coupled as a heater present inside the hydrothermal reactor unit. Additionally, the hydrothermal reactor unit may comprise a main exhaust system on the top. Herein, the main exhaust system is a manual control vent for hot gases to flow out of the hydrothermal reactor unit. Moreover, the hydrothermal reactor unit comprises an inlet valve and an outlet valve, wherein the waste flow enters through the inlet valve, and posthydrothermal gasification mixture leaves the hydrothermal reactor unit through the outlet valve. The outlet valve may be a back pressure valve as described herein. Optionally, a temperature capacity of the hydrothermal reactor unit is 700 degrees Celsius, a pressure capacity of the hydrothermal reactor unit is 400 bars and flow rate capacity thereof is 100 kilograms per hour. Herein, the temperature capacity of the hydrothermal reactor unit of 700 degrees Celsius, the pressure capacity of the hydrothermal reactor unit of 400 bars and flow rate capacity of 100 kilograms per hour are designated interim parameters. Furthermore, higher efficiency and a more stable operation condition is achieved at the temperature capacity of 700 degrees Celsius and the pressure capacity of 400 bars for hydrothermal gasification. Temperature may be recorded with a thermocouple sited on or within the metal of the hydrothermal reactor. In some embodiments, the thermocouple is placed between the aluminium block and the outside of the steel reactor. Pressure may be recorded with an in-line pressure gauge. For example, a T or X tubular connector where an appendage of a pressure gauge is connected. To avoid clogging with oil, a U-bend may be placed just before the gauge filled with water, so that only water gets into the gauge, not viscous oil. Flow rate is measured via the hydraulic pumping unit. In summary, as the piston moves forward, a ruler on the hydraulic piston measures its forward movement. The total volume of the piston stroke is known, so as a function of tubular volumetric capacity, and the time it takes for the piston to complete its stroke, the amount of waste carbon material processed by unit of time can be determined. In some embodiments, the hydrothermal reactor unit comprises a heater for increasing the temperature of the waste flow using a plurality of heating formats. Herein, the plurality of heating formats is implemented in the same manner as the second plurality of heating formats. Additionally, the plurality of heating formats may further comprise steam turbine waste heat and / or geothermal heat. Specifically, the steam turbine waste heat and or geothermal heat may be used as main functionality in upscaling of the present disclosure. Furthermore, the heater used is typically a pencil heater encased in an aluminium heater block so as to not let any of the heat escape. Additionally, the heater may be energized by a 5000 watts transformer which is connected to a source comprising voltage of 220 volts AC and current of 30 amperes. Moreover, the heater may be operatively coupled with the transformer via a switch block which is controlled by the processing electronics module. Furthermore, the plurality of heating formats may be used to rapidly increase the temperature of the waste flow up to 700 degrees Celsius. Additionally, the temperature of the waste flow is increased up to required temperatures for designated reactant profile. Subsequently, the temperature of the waste flow should be maintained at required holding temperature for the remainder of reaction phase time period. Optionally, the plurality of heating formats in the hydrothermal reactor unit comprises at least one of waste heat from internal combustion engines, solar heat from solar concentrating parabolic troughs, and waste heat from combustion of products of hydrothermal gasification, or geothermal heat. Herein, the waste heat from the exhaust generator set of the internal combustion engine flows across feed coils of hydrothermal gasification into the preheater via an inlet. Furthermore, the generator set may have a power of 1 megawatt. Additionally, a coolant system may be mechanically coupled with the generator set. Subsequently, the temperature of the waste heat in the feed coils is increased up to 500-600 degrees Celsius. Furthermore, the waste heat may be passed through a bypass that is thermally controlled via a bypass thermal control to maintain the temperature constant at 500-600 degrees Celsius. Additionally, the waste heat may continue to flow towards a reformer zone, wherein the temperature is maintained at a constant temperature of 500-600 degrees Celsius. Consequently, the waste heat flows out with a temperature of 500-600 degrees Celsius, which is used as one of the plurality of heating formats. Notably, the waste heat flowing out of the preheater may be used by the heater to maintain the temperature of the hydrothermal reactor unit at 700 degrees Celsius. Furthermore, the solar heat is compatible with mass produced parabolic-trough solar concentrating systems. Furthermore, gas and oil-based fuels with electrical and solar option aggregate modules may also be used. Consequently, the plurality of heating formats may be used to raise the temperature of the hydrothermal reactor unit to 700 degrees Celsius via the heater. In an embodiment, a thermocouple is operatively coupled with the hydrothermal reactor unit. Herein, the thermocouple is controlled by the processing electronics module. Furthermore, the thermocouple may be used for temperatures ranging from 150 degrees Celsius up to 700 degrees Celsius. The temperature may for example be maintained from 150,250,350 or 450 degrees Celsius up to 250, 350, 450, 500, 600 or 700 degrees Celsius. Additionally, the thermocouple may work in conjunction with a switch block. The switch block is a thermostatically controlled electronic control system to ensure that the heating elements are on and off in line with a software algorithm programme to ensure homeostasis of temperature control as temperature either increases or falls above or below threshold limits. In an embodiment, the system comprises a processing electronics module configured to regulate and control flow rates, temperatures and pressures in the system. Herein, the processing electronics module may be an Arduino* based system. Furthermore, the processing electronics module ensures highly accurate dosing of mixture of the waste carbon material and water by low interference telemetry data signals. Herein, telemetry data signal is an automatic measurement and wireless transmission of data from the processing electronics module, wherein sensors measure either electrical telemetry data or physical telemetry data. Furthermore, the electrical telemetry data may be for example, voltage or electric current, and physical telemetry data may be for example, temperature or pressure. Additionally, the processing electronics module may be operatively coupled with the hydraulic pumping unit. Herein, the processing electronics module controls the pressure of the waste carbon material and water. Moreover, the processing electronics module may be electrically controlled via electrical telemetry data. Notably, the processing electronics module may be operatively coupled with the conduit which is configured to partially recirculate waste heat into the hydrothermal reactor unit. Herein, the volume and the temperature of the waste heat is controlled which is passing through the exhaust gas bypass system. The exhaust gas bypass system acts as a supplementary gas offtake to additionally control gas volumes and temperatures from exhaust gas. Beneficial features of the exhaust gas bypass system are that it prevents any increased back pressure on the engine which would otherwise detrimentally affect the engine combustion cycles of the generator. An adjacent flue gas conduit releases supplementary exhaust gas via a mechanical flap to ensure that in times of excessive exhaust gas production, the pressure differential between the exhaust and the generator engine are maintained at specified operational limits. Furthermore, the processing electronics module may be encased in a cabinet for structure and protection. In an embodiment, a separation refining unit is connected to the cooling tank via a pressure regulating valve. Herein, the pressure of the waste flow is lowered before entering the separation refining unit using the processing electronics module. Furthermore, the separation refining unit comprises various technologies to affect outcome of the waste flow. Herein, the technologies may comprise gravimetric sedimentation, filtration, centrifugation and flocculation. Furthermore, all the technologies are handled with their own settings of processing electronics module. Additionally, the separation refining unit may comprise at least three refined outlets. Subsequently, the at least three refined outlets separate the waste flow in at least three storage tanks. Herein, the at least three storage tanks may be used for storing solid, liquid and gaseous waste flow. The present disclosure also relates to the method as described above. Various embodiments and variants disclosed above apply mutatis mutandis to the method. Optionally, in the method, the plurality of heating formats comprises at least one of: -waste heat from internal combustion engines; - solar heat from solar concentrating parabolic troughs; - waste heat from combustion of hydrothermal gasification products; - steam turbine waste heat and / or geothermal heat. Optionally, in the method, the preheater comprises a second plurality of heating formats to increase the temperature of the mixture of waste carbon material and water. Optionally, the method comprises increasing the temperature of the waste flow up to 700 degrees Celsius and pressure thereof up to 400 bars. Optionally, the method comprises increasing temperature of the mixture of waste carbon material and water up to 500-600 degrees Celsius. DETAILED DESCRIPTION OF THE DRAWINGS Figure 1 provides a schematic illustration of a system 100 of the invention. The system comprises a mixing and recirculation tank 10 for receiving waste carbon material and optionally water. The waste carbon material is then transferred to a hydraulic pumping unit 20 where the waste carbon material is mixed with water. The hydraulic pumping unit 20 increases the pressure of the waste carbon material and water mixture before transfer of the mixture to the plug flow reactor 30. The plug flow reactor 30 provides a continuous system through which the waste carbon material and water mixture travels. The plug flow reactor 30 is configured to maintain the pressure of the waste carbon material and water mixture. The pressurised waste carbon material and water mixture travels to the preheater 32 which increases the temperature of the waste carbon material and water mixture to provide waste flow. The waste flow then enters the hydrothermal reactor unit 34 where the mixture is heated further to convert waste flow into syngas and supercritical and / or superheated steam. The plug flow reactor typically comprises a back pressure valve 36 configured to maintain the pressure within the plug flow reactor. Syngas may then enter an interlock where it is separated from superheated / supercritical steam. The syngas then enters a methanol reactor chamber 40 where the syngas is contacted with a catalyst for converting syngas to methanol. The methanol reactor chamber 40 may comprise a back pressure valve 36 at the outlet end to facilitate downstream pressure regulation. Heat generated during methanol production is recirculated from the methanol reactor chamber to the preheater 32 and / or hydrothermal reactor unit 34 by a heat exchanger 50. Referring to Figure 2, illustrated is a flowchart depicting steps of a method for converting waste carbon material into bio-methanol using hydrothermal gasification and catalytic methanol synthesis, in accordance with an embodiment of the present disclosure. At a step 202, waste carbon material is received and is configured to undergo hydrothermal gasification. At a step 204, waste carbon material is mixed with water. Steps 202 and 204 may be consecutive or simultaneous. At a step 206, pressure of a mixture of waste carbon material and water is increased. At a step 208, temperature of the mixture of waste carbon material and water is increased to obtain waste flow. At a step 210, the waste flow is converted into syngas and supercritical and / or superheated steam by hydrothermal gasification. At a step 212, syngas is converted to methanol by catalytic methanol synthesis. At a step 214, methanol is distilled. Heat generated by catalytic methanol synthesis is recirculated to heat the mixture of waste carbon material and water. In addition, heat from downstream of the hydrothermal reactor and / or distillation may be recirculated to heat the mixture of waste carbon material and water.

Claims

1. A system for converting waste carbon material into methanol, the system comprising:(a) a mixing and recirculation tank configured to receive the waste carbon material to undergo hydrothermal gasification;(b) a hydraulic pumping unit configured to mix waste carbon material with water and to increase pressure of the mixture of waste carbon material and water;(c) a plug flow reactor configured to maintain the pressure of the mixture of the waste carbon material and water;wherein the plug flow reactor comprises:(i) a preheater configured to increase temperature of the mixture of waste carbon material and water to obtain waste flow; and(ii) a hydrothermal reactor unit configured to receive the waste flow from the preheater, wherein the hydrothermal reactor unit is configured to convert the waste flow into syngas and steam;(d) a methanol reactor chamber in fluid communication with the plug flow reactor for receiving the syngas therefrom, the methanol reactor chamber housing a catalyst for converting syngas to methanol; and(e) a heat exchanger configured to recirculate excess heat from the methanol reactor chamber to the preheater.

2. A system of claim 1, wherein the methanol reactor chamber comprises a catalyst support and the methanol reactor chamber is configured to pass syngas over and through the catalyst support.

3. A system of claim 1 or claim 2, wherein the system further comprises a distillation unit for distilling methanol from water, optionally wherein the system further comprises a secondary heat exchanger configured to recirculate excess heat from the distillation unit to the preheater.

4. A system of any of the preceding claims, wherein the plug flow reactor is connected to the methanol synthesis chamber via an interlock, optionally wherein the interlock is positioned in an upright position to separate syngas from liquid by density phase separation.

5. A system of any of the preceding claims, wherein the system comprises a heat exchanger configured to recirculate excess heat from downstream of the hydrothermal reactor and / or from the interlock to the preheater and / or the hydrothermal reactor.

6. A system of any of the preceding claims, wherein the catalyst is selected from oxides of zinc, copper, magnesium, aluminium and iron.

7. A system of any of claims 2-6, wherein the catalyst support is a ceramic porous matrix providing a high surface area to volume ratio, optionally wherein the catalyst support is a zeolite clinoptilolite ceramic porous matrix providing a high surface area to volume ratio.

8. A system of any of the preceding claims, wherein the plug flow reactor is configured to enable continuous flow of the mixture of waste carbon material and water to the preheater and the hydrothermal reactor unit.

9. A system of any of the preceding claims, wherein the plug flow reactor comprises a back pressure valve positioned downstream of the hydrothermal reactor unit.

10. A system of any of the preceding claims, wherein the hydrothermal reactor unit comprises a heater for increasing the temperature of the waste flow using a plurality of heating formats.

11. A system of any of the preceding claims, wherein the hydrothermal reactor unit comprises a conduit configured to partially recirculate waste heat into the hydrothermal reactor unit.

12. A system of any of the preceding claims, further comprising a processing electronics module configured to regulate and control flowrates, temperatures and pressures in the system.

13. A system of any of claims 10-12, wherein the plurality of heating formats in the hydrothermal reactor unit comprises at least one of:(i) steam turbine waste heat;(ii) geothermal heat;(iii) waste heat from internal combustion engines;(iv) solar heat from solar concentrating parabolic troughs; and(v) waste heat from combustion of waste material produced from hydrothermal gasification.

14. A system of any of the preceding claims, wherein the preheater comprises a second plurality of heating formats to increase the temperature of the mixture of waste carbon material and water.

15. A system of any of the preceding claims, wherein the plug flow reactor is tubular in structure.

16. A system of any of the preceding claims, wherein the hydraulic pumping unit comprises a double acting piston.

17. A system of any of the preceding claims, wherein the hydraulic pumping unit comprises a plurality of hydraulic pumps.

18. A system of any of the preceding claims, wherein a temperature capacity of the hydrothermal reactor unit is 700 degrees Celsius, a pressure capacity of the hydrothermal reactor unit is 400 bars and flow rate capacity thereof is 100 kilograms per hour.

19. A system of any of the preceding claims, wherein the preheater is configured to increase temperature of the mixture of waste carbon material and water up to 500-600 degrees Celsius.

20. A method for converting waste carbon material into methanol, the method comprising(a) receiving the waste carbon material configured to undergo hydrothermal gasification;(b) mixing waste carbon material with water;(c) increasing pressure of the mixture of waste carbon material and water using a hydraulic pumping unit to provide a pressurised mixture of waste carbon material and water;(d) transferring the pressurised mixture of waste carbon material and water to a plug flow reactor comprising a preheater and a hydrothermal reactor unit, wherein the plug flow reactor is configured to maintain the pressure of the mixture of waste carbon material and water;(e) increasing temperature of the mixture of waste carbon material and water in the preheater to obtain waste flow;(f) converting the waste flow into syngas steam in the hydrothermal reactor unit by increasing the temperature of the waste flow;(g) transferring the syngas to a methanol reactor chamber housing a catalyst for converting syngas to methanol and contacting the syngas with the catalyst under conditions suitable for the production of methanol; and(h) recirculating excess heat from the methanol reactor chamber to the preheater via a heat exchanger.

21. A method of claim 20, further comprising distilling methanol from water in a distillation unit.

22. A method of claim 20 or 21, further comprising recirculating excess heat from the distillation unit to the preheater.

23. A method of any of claims 20-22, wherein the method comprises adding an alkali catalyst to the waste carbon material.

24. A method of any of claims 20-23, wherein the method comprises transferring the syngas to a methanol reactor chamber via an interlock configured to separate syngas from liquid.

25. A method of any of claims 20-24, wherein the method comprises recirculating heat from downstream of the hydrothermal reactor and / or the interlock to the preheater and / or the hydrothermal reactor via a heat exchanger.

26. A method of any of claims 20-25, wherein increasing the temperature of the waste flow comprises using a plurality of heating formats.

27. A method of any of claims 20-26, wherein the method comprises configuring a conduit to partially recirculate waste heat from the hydrothermal reactor unit into the waste flow.

28. A method of any of claims 20-27, further comprising decreasing temperature and pressure of the syngas and / or methanol.

29. A method of any of claims 20-28, wherein the plurality of heating formats comprise at least one of:(i) steam turbine waste heat;(ii) geothermal heat;(iii) waste heat from internal combustion engines;(iv) solar heat from solar concentrating parabolic troughs; and(v) waste heat from combustion of waste material produced from hydrothermal gasification.

30. A method of any of claims 20-29, wherein the preheater comprises a second plurality of heating formats to increase the temperature of the mixture of waste carbon material and water.

31. A method of any of claims 20-30, wherein the method comprises increasing the temperature of the waste flow up to 700 degrees Celsius and pressure thereof up to 400 bars.

32. A method of any of claims 20-31, wherein the method comprises increasing temperature of the mixture of waste carbon material and water up to 500-600 degrees Celsius.

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