Patent Publication Number: US-11649201-B2

Title: Autonomous modular flare gas conversion systems and methods

Description:
This application: (i) claims under 35 U.S.C. § 119(e)(1) the benefit of the filing date of, and claims the benefit of priority to, U.S. provisional application Ser. No. 63/189,756 filed May 18, 2021; (ii) claims under 35 U.S.C. § 119(e)(1) the benefit of the filing date of, and claims the benefit of priority to, U.S. provisional application Ser. No. 63/213,129 filed Jun. 21, 2021; (iii) claims under 35 U.S.C. § 119(e)(1) the benefit of the filing date of, and claims the benefit of priority to, U.S. provisional application Ser. No. 63/197,898 filed Jun. 7, 2021; and (iv) claims under 35 U.S.C. § 119(e)(1) the benefit of the filing date of, and claims the benefit of priority to, U.S. provisional application Ser. No. 63/304,463 filed Jan. 28, 2022, the entire disclosure of each of which are incorporated herein by reference. 
    
    
     BACKGROUND OF THE INVENTION 
     Field of the Invention 
     The present inventions relate to new and improved methods, devices and systems for recovering and converting waste gases, such as flare gas, into useful and economically viable materials. 
     The term “flare gas” and similar such terms should be given their broadest possible meaning, and would include gas generated, created, associated or produced by, or from, oil and gas production, hydrocarbon wells (including shall, conventional and unconventional wells), petrochemical processing, refining, landfills, waste water treatment, dairies, livestock production, and other municipal, chemical and industrial processes. Thus, for example, flare gas would include stranded gas, associated gas, landfill gas, vented gas, biogas, digester gas, small-pocket gas, and remote gas. 
     Typically, the composition of flare gas is a mixture of different gases. The composition can depend upon the source of the flare gas. For instance, gases released during oil-gas production mainly contain natural gas. Natural gas is more than 90% methane (CH 4 ) with ethane and smaller amounts of other hydrocarbons, water, N 2  and CO 2  may also be present. Flare gas from refineries and other chemical or manufacturing operations typically can be a mixture of hydrocarbons and in some cases H 2 . Landfill gas, biogas or digester gas typically can be a mixture of CH 4  and CO 2 , as well as small amounts of other inert gases. In general, flare gas can contain one or more of the following gases: methane, ethane, propane, n-butane, isobutane, n-pentane, isopentane, n-hexane, ethylene, propylene, 1-butene, carbon monoxide, carbon dioxide, hydrogen sulfide, hydrogen, oxygen, nitrogen, and water. 
     The majority of flare gas is produced from smaller, individual point sources, such as a number of oil or gas wells in an oil field, a landfill, or a chemical plant. Prior to the present inventions flare gas, and in particular flare gas generated from hydrocarbon producing wells, and other smaller point sources, was burned to destroy it, in some instances may have been vented directly into the atmosphere. This flare gas could not be economically recovered and used. The burning or venting of fare gas, both from hydrocarbon production and other endeavors, raises serious concerns about pollution and the production greenhouse gases. 
     As used herein unless specified otherwise, the terms “syngas” and “synthesis gas” and similar such terms should be given their broadest possible meaning and would include gases having as their primary components a mixture of H 2  and CO; and may also contain CO 2 , N 2 , and water, as well as, small amounts of other materials. 
     As used herein unless specified otherwise, the term “product gas” and similar such terms should be given their broadest possible meaning and would include gasses having H 2 , CO and other hydrocarbons, and typically significant amounts of other hydrocarbons, such as methane. 
     As used herein unless specified otherwise, the term “reprocessed gas” includes “syngas”, “synthesis gas” and “product gas”. 
     As used herein unless specified otherwise, the terms “partial oxidation”, “partially oxidizing” and similar such terms mean a chemical reaction where a sub-stoichiometric mixture of fuel and air (i.e., fuel rich mixture) is partially reacted (e.g., combusted) to produce a syngas. The term partial oxidation includes both thermal partial oxidation (TPOX), which typically occurs in a non-catalytic reformer, and catalytic partial oxidation (CPOX). The general formula for a partial oxidation reaction is 
     
       
         
           
             
               
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     As used herein unless specified otherwise, the term “CO 2 e” is used to define carbon dioxide equivalence of other, more potent greenhouse gases, to carbon dioxide (e.g., methane and nitrous oxide) on a global warming potential basis of 100 years, based on Intergovernmental Panel on Climate Change (IPCC) Fifth Assessment Report (AR5) methodology. The term “carbon intensity” is taken to mean the lifecycle CO 2 e generated per unit mass of a product. 
     As used herein, unless specified otherwise, the terms % and mol % are used interchangeably and refer to the moles of a first component as a percentage of the moles of the total, e.g., formulation, mixture, material or product. 
     As used herein unless specified otherwise, the recitation of ranges of values herein is merely intended to serve as a shorthand method of referring individually to each separate value falling within the range. Unless otherwise indicated herein, each individual value within a range is incorporated into the specification as if it were individually recited herein. 
     Generally, the term “about” as used herein unless stated otherwise is meant to encompass the greater of a variance or range of ±10% or the experimental or instrument error associated with obtaining the stated value. 
     As used herein, unless stated otherwise, room temperature is 25° C., and standard temperature and pressure is 15° C. and 1 atmosphere (1.01325 bar). 
     Unless specifically provided otherwise, all entropy values, including entropy states, entropy points, specific entropy points, and specific entropy values, that are discussed in the specification and shown in the Figures, in particular the T-S diagrams, are based upon, or use as a reference state absolute zero (i.e., 0° K, −273.15° C.) and 1 atmosphere. 
     Related Art and Terminology 
     In the production of natural resources from formations within the earth a well or borehole is drilled into the earth to the location where the natural resource is believed to be located. These natural resources may be a hydrocarbon reservoir, containing natural gas, crude oil and combinations of these; the natural resource may be fresh water; it may be a heat source for geothermal energy; or it may be some other natural resource that is located within the ground. 
     These resource-containing formations may be a few hundred feet, a few thousand feet, or tens of thousands of feet below the surface of the earth, including under the floor of a body of water, e.g., below the sea floor. In addition to being at various depths within the earth, these formations may cover areas of differing sizes, shapes and volumes. 
     Typically, and by way of general illustration, in drilling a well an initial borehole is made into the earth, e.g., the surface of land or seabed, and then subsequent and smaller diameter boreholes are drilled to extend the overall depth of the borehole. In this manner as the overall borehole gets deeper its diameter becomes smaller; resulting in what can be envisioned as a telescoping assembly of holes with the largest diameter hole being at the top of the borehole closest to the surface of the earth. 
     Thus, by way of example, the starting phases of a subsea drill process may be explained in general as follows. Once the drilling rig is positioned on the surface of the water over the area where drilling is to take place, an initial borehole is made by drilling a 36″ hole in the earth to a depth of about 200-300 ft. below the seafloor. A 30″ casing is inserted into this initial borehole. This 30″ casing may also be called a conductor. The 30″ conductor may or may not be cemented into place. During this drilling operation a riser is generally not used and the cuttings from the borehole, e.g., the earth and other material removed from the borehole by the drilling activity are returned to the seafloor. Next, a 26″ diameter borehole is drilled within the 30″ casing, extending the depth of the borehole to about 1,000-1,500 ft. This drilling operation may also be conducted without using a riser. A 20″ casing is then inserted into the 30″ conductor and 26″ borehole. This 20″ casing is cemented into place. The 20″ casing has a wellhead secured to it. (In other operations an additional smaller diameter borehole may be drilled, and a smaller diameter casing inserted into that borehole with the wellhead being secured to that smaller diameter casing.) A BOP (blow out preventer) is then secured to a riser and lowered by the riser to the sea floor; where the BOP is secured to the wellhead. From this point forward all drilling activity in the borehole takes place through the riser and the BOP. 
     It should be noted that riserless subsea drilling operations are also contemplated. 
     For a land-based drill process, the steps are similar, although the large diameter tubulars, 30″-20″ are typically not used. Thus, and generally, there is a surface casing that is typically about 13⅜″ diameter. This may extend from the surface, e.g., wellhead and blow out preventer (BOP), to depths of tens of feet to hundreds of feet. One of the purposes of the surface casing is to meet environmental concerns in protecting ground water. The surface casing should have sufficiently large diameter to allow the drill string, product equipment such as an electronic submersible pump (ESP) and circulation mud to pass through. Below the casing one or more different diameter intermediate casings may be used. (It is understood that sections of a borehole may not be cased, which sections are referred to as open hole.) These can have diameters in the range of about 9″ to about 7″, although larger and smaller sizes may be used, and can extend to depths of thousands and tens of thousands of feet. Inside of the casing and extending from a pay zone, or production zone of the borehole up to and through the wellhead on the surface is the production tubing. There may be a single production tubing or multiple production tubings in a single borehole, with each of the production tubing endings being at different depths. 
     Fluid communication between the formation and the well can be greatly increased by the use of hydraulic fracturing techniques. The first uses of hydraulic fracturing date back to the late 1940s and early 1950s. In general, hydraulic fracturing treatments involve forcing fluids down the well and into the formation, where the fluids enter the formation and crack, e.g., force the layers of rock to break apart or fracture. These fractures create channels or flow paths that may have cross sections of a few micron&#39;s, to a few millimeters, to several millimeters in size, and potentially larger. The fractures may also extend out from the well in all directions for a few feet, several feet and tens of feet or further. It should be remembered that the longitudinal axis of the well in the reservoir may not be vertical: it may be on an angle (either slopping up or down) or it may be horizontal. For example, in the recovery of shale gas and oil the wells are typically essentially horizontal in the reservoir. The section of the well located within the reservoir, i.e., the section of the formation containing the natural resources, can be called the pay zone. 
     As used herein, unless specified otherwise, the terms “hydrocarbon exploration and production”, “exploration and production activities”, “E&amp;P”, and “E&amp;P activities”, and similar such terms are to be given their broadest possible meaning, and include surveying, geological analysis, well planning, reservoir planning, reservoir management, drilling a well, workover and completion activities, hydrocarbon production, flowing of hydrocarbons from a well, collection of hydrocarbons, secondary and tertiary recovery from a well, the management of flowing hydrocarbons from a well, and any other upstream activities. 
     As used herein, unless specified otherwise, the term “earth” should be given its broadest possible meaning, and includes, the ground, all natural materials, such as rocks, and artificial materials, such as concrete, that are or may be found in the ground. 
     As used herein, unless specified otherwise “offshore” and “offshore drilling activities” and similar such terms are used in their broadest sense and would include drilling activities on, or in, any body of water, whether fresh or salt water, whether manmade or naturally occurring, such as for example rivers, lakes, canals, inland seas, oceans, seas, such as the North Sea, bays and gulfs, such as the Gulf of Mexico. As used herein, unless specified otherwise the term “offshore drilling rig” is to be given its broadest possible meaning and would include fixed towers, tenders, platforms, barges, jack-ups, floating platforms, drill ships, dynamically positioned drill ships, semi-submersibles and dynamically positioned semi-submersibles. As used herein, unless specified otherwise the term “seafloor” is to be given its broadest possible meaning and would include any surface of the earth that lies under, or is at the bottom of, any body of water, whether fresh or salt water, whether manmade or naturally occurring. 
     As used herein, unless specified otherwise, the term “borehole” should be given it broadest possible meaning and includes any opening that is created in the earth that is substantially longer than it is wide, such as a well, a well bore, a well hole, a micro hole, a slimhole and other terms commonly used or known in the arts to define these types of narrow long passages. Wells would further include exploratory, production, abandoned, reentered, reworked, and injection wells. They would include both cased and uncased wells, and sections of those wells. Uncased wells, or section of wells, also are called open holes, or open hole sections. Boreholes may further have segments or sections that have different orientations, they may have straight sections and arcuate sections and combinations thereof. Thus, as used herein unless expressly provided otherwise, the “bottom” of a borehole, the “bottom surface” of the borehole and similar terms refer to the end of the borehole, i.e., that portion of the borehole furthest along the path of the borehole from the borehole&#39;s opening, the surface of the earth, or the borehole&#39;s beginning. The terms “side” and “wall” of a borehole should to be given their broadest possible meaning and include the longitudinal surfaces of the borehole, whether or not casing or a liner is present, as such, these terms would include the sides of an open borehole or the sides of the casing that has been positioned within a borehole. Boreholes may be made up of a single passage, multiple passages, connected passages, (e.g., branched configuration, fishboned configuration, or comb configuration), and combinations and variations thereof. 
     Boreholes are generally formed and advanced by using mechanical drilling equipment having a rotating drilling tool, e.g., a bit. For example, and in general, when creating a borehole in the earth, a drilling bit is extending to and into the earth and rotated to create a hole in the earth. To perform the drilling operation the bit must be forced against the material to be removed with a sufficient force to exceed the shear strength, compressive strength or combinations thereof, of that material. The material that is cut from the earth is generally known as cuttings, e.g., waste, which may be chips of rock, dust, rock fibers and other types of materials and structures that may be created by the bit&#39;s interactions with the earth. These cuttings are typically removed from the borehole by the use of fluids, which fluids can be liquids, foams or gases, or other materials know to the art. 
     As used herein, unless specified otherwise, the term “drill pipe” is to be given its broadest possible meaning and includes all forms of pipe used for drilling activities; and refers to a single section or piece of pipe. As used herein the terms “stand of drill pipe,” “drill pipe stand,” “stand of pipe,” “stand” and similar type terms should be given their broadest possible meaning and include two, three or four sections of drill pipe that have been connected, e.g., joined together, typically by joints having threaded connections. As used herein the terms “drill string,” “string,” “string of drill pipe,” string of pipe” and similar type terms should be given their broadest definition and would include a stand or stands joined together for the purpose of being employed in a borehole. Thus, a drill string could include many stands and many hundreds of sections of drill pipe. 
     As used herein, unless specified otherwise, the terms “formation,” “reservoir,” “pay zone,” and similar terms, are to be given their broadest possible meanings and would include all locations, areas, and geological features within the earth that contain, may contain, or are believed to contain, hydrocarbons. 
     As used herein, unless specified otherwise, the terms “field,” “oil field” and similar terms, are to be given their broadest possible meanings, and would include any area of land, sea floor, or water that is loosely or directly associated with a formation, and more particularly with a resource containing formation, thus, a field may have one or more exploratory and producing wells associated with it, a field may have one or more governmental body or private resource leases associated with it, and one or more field(s) may be directly associated with a resource containing formation. 
     As used herein, unless specified otherwise, the terms “conventional gas”, “conventional oil”, “conventional”, “conventional production” and similar such terms are to be given their broadest possible meaning and include hydrocarbons, e.g., gas and oil, that are trapped in structures in the earth. Generally, in these conventional formations the hydrocarbons have migrated in permeable, or semi-permeable formations to a trap, or area where they are accumulated. Typically, in conventional formations a non-porous layer is above, or encompassing the area of accumulated hydrocarbons, in essence trapping the hydrocarbon accumulation. Conventional reservoirs have been historically the sources of the vast majority of hydrocarbons produced. As used herein, unless specified otherwise, the terms “unconventional gas”, “unconventional oil”, “unconventional”, “unconventional production” and similar such terms are to be given their broadest possible meaning and includes hydrocarbons that are held in impermeable rock, and which have not migrated to traps or areas of accumulation. 
     Global Warming and Environmental Concerns 
     The relative harm to the environment by the release of waste gases when compared to CO 2  an established highly problematic gas, are shown  FIG.  22   . 
     The environmental impact in terms of global warming potential of methane slippage from flare gas and venting cannot be overstated. According to a 2019 International Energy Agency (IEA) report, about 200 billion cubic meter (bcm) of waste or flair gas were combusted or vented into the atmosphere in 2018. About 50 bcm of gas were vented, and about 150 bcm were combusted in flares. Combustion is intended to convert hydrocarbons to CO 2 , but their peak efficiency is 98%, and that efficiency drops in the presence of wind. The combination of inefficient combustion and venting results in total CO 2 e emissions of about 1.4 gigatons of CO 2 , which amounts to about 2.7% of all anthropogenic sources of CO 2  per year. 
     This Background of the Invention section is intended to introduce various aspects of the art, which may be associated with embodiments of the present inventions. Thus, the forgoing discussion in this section provides a framework for better understanding the present inventions, and is not to be viewed as an admission of prior art 
     SUMMARY 
     There has been a long-standing, expanding and unmet need, for systems, devices and methods to convert otherwise uneconomic hydrocarbon-based fuel, e.g., flare gas, to value-added, easily transported products (such as methanol, ethanol, mixed alcohols, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals). The present inventions, among other things, solve these needs by providing the articles of manufacture, devices, systems and processes taught, and disclosed herein. 
     Thus, there is provided a system for converting flare gas into an end product, the system having: a reformer stage and a synthesis stage; the reformer stage comprising: an intake for receiving a flow of a flare gas; an intake for receiving a flow of air; a mixer for combining the flow of air and the flow of the flare gas; wherein the mixer is configured to provide a mixture having a rich fuel/air equivalence ratio; an air breathing reformer, configured to operate under rich fuel/air conditions; wherein the reformer is configured to operate in a partial oxidation combustion window; whereby the reformer is configured to convert the mixture into a syngas; a line for flowing the syngas to the synthesis stage; the synthesis stage having: a line for receiving a flow of syngas from the reformer stage; a synthesis unit configured to receive the syngas and convert the syngas into an end product; a control system configured to operate the reformer stage at a predetermined partial oxidation temperature and a predetermined partial oxidation pressure; and the synthesis stage at a predetermined synthesis temperature and a predetermined synthesis pressure. 
     In addition, there is provided a system for converting a flare gas to an end product, the system having: a flare gas source, defining a starting specific entropy; an oxygen source, wherein the oxygen source comprises air; a fuel/air mixture defining a starting specific entropy; a control system; an air-breathing reformer; the reform in conjunction with the control system, configured to partially oxidize a mixture of the oxygen source and the flare gas; thereby providing a reprocessed gas flow comprises a syngas; a synthesis unit in conjunction with the control system configured to provide a first product stream comprising an end product; wherein the end product stream and an exhaust product stream define a final specific entropy; the control system configured to operate the system wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; and, wherein during operation the system is configured to produces less than 2.0 kg of CO 2  per kg of flare gas received. 
     Further, there is provided a continuous method of converting a flare gas to methanol, the method including: receiving a flare gas flow from a source, wherein: the flare gas flow has a rate of about 50,000 scfd to about 30,000,000 scfd; the flare gas flow has a composition, wherein the composition varies over time; compressing the flare gas flow to provide a compressed flare gas flow, wherein the compressed flare gas flow has a pressure of about 8 bar to about 60 bar; mixing the compressed flare gas flow with air to provide a rich fuel/air mixture; partially oxidizing the rich fuel/air mixture at a temperature of from about 700° C. to about 1,200° C. in a reformer to provide a reprocessed gas flow; wherein the reprocessed gas flow having a syngas having a syngas composition; passing the reprocessed gas flow through a deoxygenation reactor, whereby any excess oxygen is removed from the reprocessed gas flow, thereby providing a deoxygenated reprocessed gas flow; removing water from the deoxygenated reprocessed gas flow to thereby provided a syngas flow; controlling the pressure and the temperature of the syngas flow to provide a predetermined synthesis temperature and synthesis pressure of the syngas flow; flowing the syngas flow at the predetermined synthesis temperature and synthesis pressure into a synthesis unit; converting the syngas flow in the synthesis unit to thereby provide a first product stream having methanol; and, removing a material from the first product stream, the material having hydrogen; to thereby provide a second product stream; wherein the second product stream having at least about 80% methanol, and is thereby at least about 80% pure. 
     Yet further, there is provided a continuous method of converting a flare gas to methanol, the method including: receiving a flare gas flow from a source, wherein the flare gas flow has a rate of flow; receiving an air flow from an intake; mixing the flare gas flow with air flow to provide a fuel/air mixture; wherein the fuel/air mixture defines a starting specific entropy; flowing the fuel/air mixture, having a pressure of about 8 bar to 60 bar, into a reformer, partially oxidizing the rich fuel/air mixture at a temperature of from about 700° C. to about 1,200° C. in the reformer to provide a reprocessed gas flow; wherein the reprocessed gas flow having a syngas having a syngas composition; controlling the pressure and the temperature of the reprocessed gas flow to provide a predetermined synthesis temperature and a predetermined synthesis pressure of the syngas flow; converting the reprocessed gas flow in the synthesis unit at the predetermined synthesis temperature and synthesis pressure in a synthesis unit to thereby provide a first product stream having methanol; wherein the first product stream and an exhaust product stream thereby defining a final specific entropy; and, wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other. 
     Additionally, there is provided a system for converting a flare gas to an end product, the system having: a flare gas source, defining a starting specific entropy; an air source; a fuel/air mixture defining a starting specific entropy; a control system; an air-breathing reformer; the reform in conjunction with the control system, configured to partially oxidize a mixture of the air and the flare gas; thereby providing a reprocessed gas flow comprises a syngas; a synthesis unit in conjunction with the control system configured to provide a first product stream comprising an end product; wherein the end product stream and an exhaust product stream define a final specific entropy; the control system configured to operate the system wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; and, wherein during operation, the system is configured to be net carbon-negative, whereby during operation the system produces less than about −20 kg CO 2 e per kg of end product provided. 
     Still in addition, there is provided a system for converting a flare gas to an end product, the system having: a flare gas source, defining a starting specific entropy; an air source, a fuel/air mixture defining a starting specific entropy; a control system; an air-breathing reformer; the reform in conjunction with the control system, configured to partially oxidize a mixture of the air and the flare gas; thereby providing a reprocessed gas flow comprises a syngas; a synthesis unit in conjunction with the control system configured to provide a first product stream comprising an end product; wherein the end product stream and an exhaust product stream define a final specific entropy; the control system configured to operate the system wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; wherein during operation, the system is configured to be net carbon-negative, whereby during operation the system produces less than about −20 kg CO 2 e per kg of end product provided; and, wherein during operation the system is configured to produces less than 2.0 kg of CO 2  per kg of flare gas received. 
     In addition, there is provided a method of converting a flare gas to an end product, the method including: receiving a flare gas from a source; forming a mixture of the flare gas and an oxygen source, wherein the oxygen source having air, thereby defining a fuel/air mixture; wherein the fuel/air mixture defines a starting specific entropy; partially oxidizing the fuel/air mixture at a predetermined reformer temperature; thereby providing a reprocessed gas flow having a syngas having a syngas composition; converting the reprocessed gas flow in a synthesis unit to thereby provide a first product stream having an end product; wherein the first product stream and an exhaust product stream thereby defining a final specific entropy; and, wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other. 
     Still further, there is provided a carbon-neutral method of converting a flare gas to an end product, the method including: (a) receiving a flow of a flare gas from a source; (b) compressing the flare gas; (c) partially oxidizing the flare gas to provide a reprocessed gas; and, (d) converting the reprocessed gas into an end product; wherein steps (a) to (d) produce less than 2.0 kg of CO 2  per kg of flare gas received. 
     Yet additionally, there is provided a net-carbon negative method of capturing and converting flare gas to an end product comprising methanol, the method including: (a) receiving a flow of a flare gas from a source; (b) compressing the flare gas to a predetermined partial oxidation pressure; (c) mixing the flare gas with air, to provide a fuel mixture, where the fuel mixture has a fuel/air equivalence ratio of greater than 1; (d) partially oxidizing the flare gas at a predetermined partial oxidation temperature to provide syngas, wherein the syngas has a ratio of H 2 /CO that is from about 1 to about 3; (e) converting the syngas into an end product at a predetermined synthesis temperature and a predetermined synthesis pressure; wherein the end product comprises methanol; and, wherein steps (a) to (e) are net carbon-negative, whereby these steps produce less than about −20 kg CO 2 e per kg of methanol produced. 
     Additionally, there is provided a carbon-neutral method of making an end product, the method including: (a) partially oxidizing the flare gas to provide a reprocessed gas; (b) converting the reprocessed gas into an end product; wherein steps (a) to (b) produce less than 2.0 kg of CO 2  per kg of flare gas partially oxidized; and, wherein steps (a) to (b) are net carbon-negative, whereby these steps produce less than about −20 kg CO 2 e per kg of end product produced. 
     Still further there is provided, a method of converting a flare gas to an end product, the method including: (a) receiving a flare gas from a source; (b) forming a mixture of the flare gas and an oxygen source, wherein the oxygen source primarily comprises air, thereby defining a fuel/air mixture, wherein the fuel/air mixture defines a starting specific entropy; (c) partially oxidizing the fuel/air mixture at a predetermined reformer temperature; thereby providing a reprocessed gas flow comprises a syngas having a syngas composition; (d) converting the reprocessed gas flow in a synthesis unit to thereby provide a first product stream comprising an end product and an exhaust product stream; thereby defining a final specific entropy; wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; and, wherein steps (a) to (d) produce less than 2.0 kg of CO 2  per kg of flare gas received. 
     Moreover, there is provided a system for converting flare gas into an end product, the system having: a reformer stage and a synthesis stage; the reformer stage including: an intake for receiving a flow of a flare gas; an intake for receiving a flow of air; an air breathing reformer, configured to operate under rich fuel/air conditions; wherein the reformer is configured to operate in a partial oxidation combustion window; whereby the reformer is configured to convert mixture of flare gas and air into a syngas; a line for flowing the syngas to the synthesis stage; the synthesis stage including: a line for receiving a flow of syngas from the reformer stage; a synthesis unit configured to receive the syngas and convert the syngas into an end product; and, a control system configured to operate the reformer stage at a predetermined partial oxidation temperature and a predetermined partial oxidation pressure; and the synthesis stage at a predetermined synthesis temperature and a predetermined synthesis pressure. 
     Moreover, there is provided a method of converting a flare gas to an end product, the method including: (a) receiving a flare gas from a source; (b) forming a mixture of the flare gas and an oxygen source, wherein the oxygen source primarily comprises air, thereby defining a fuel/air mixture, wherein the fuel/air mixture defines a starting specific entropy; (c) partially oxidizing the fuel/air mixture at a predetermined reformer temperature; thereby providing a reprocessed gas flow comprises a syngas having a syngas composition; (d) converting the reprocessed gas flow in a synthesis unit to thereby provide a first product stream comprising an end product and an exhaust product stream; thereby defining a final specific entropy; wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; and, wherein steps a) to d) are net carbon-negative, whereby these steps produce less than about −20 kg CO 2 e per kg of end product provided. 
     Furthermore, there is provided a method of converting a flare gas to an end product, the method comprises: (a) receiving a flare gas from a source; (b) forming a mixture of the flare gas and an oxygen source, wherein the oxygen source primarily comprises air, thereby defining a fuel/air mixture, wherein the fuel/air mixture defines a starting specific entropy; (c) partially oxidizing the fuel/air mixture at a predetermined reformer temperature; thereby providing a reprocessed gas flow comprises a syngas having a syngas composition; (d) converting the reprocessed gas flow in a synthesis unit to thereby provide a first product stream comprising an end product and an exhaust product stream; thereby defining a final specific entropy; wherein the starting specific entropy and the final specific entropy are less than about 1 kJ/kg° C. of each other; wherein steps a) to d) produce less than 2.0 kg of CO 2  per kg of flare gas received; and, wherein steps (a) to (d) are net carbon-negative, whereby these steps produce less than about −20 kg CO 2 e per kg of end product provided. 
     Yet additionally, there is provided these systems, methods and devices having one or more of the following features: wherein the reformer is a reciprocating engine; and the reciprocating engine has one, more than one, or all of: a compression ratio in the range of about 8:1 to about 17:1; an inlet manifold air temperature of ambient temperature to about 300° C.; an inlet manifold air pressure of ambient to about 5 bar; a spark timing between TDC and 50 degrees before TDC; and, an engine speed for from about 8,000 rpm to about 1,500 rpm. 
     Additionally, there is provided these systems, methods and devices having one or more of the following features: wherein the reformer is a reciprocating engine; and the reciprocating engine has at least one of: a compression ratio in the range of about 8:1 to about 17:1; an inlet manifold air temperature of ambient temperature to about 300° C.; an inlet manifold air pressure of ambient to about 5 bar; a spark timing between TDC and 50 degrees before TDC; or, an engine speed for from about 8,000 rpm to about 1,500 rpm; 
     Yet additionally, there is provided these systems, methods and devices having one or more of the following features: wherein the reformer comprises a gas turbine assembly; and the gas turbine assembly has one, more than one, or all of: a first partial oxidation combustor; a two-stage combustion process; a gas turbine combustor; and, a combustion cycle time of from 5 to 50 milliseconds. 
     In addition, there is provided these systems, methods and devices having one or more of the following features: wherein the reformer comprises a gas turbine assembly; and the gas turbine assembly has at least one of: a first partial oxidation combustor; a two-stage combustion process; a gas turbine combustor; or, a combustion cycle time of from 5 to 50 milliseconds. 
     Still further, there is provided these systems, methods and devices having one or more of the following features: has a hydrogen separation unit to provide a stream of a recovered hydrogen to the system; has a hydrogen separation unit to provide a stream of a recovered hydrogen for mixing with the syngas; has a hydrogen separation unit to provide a stream of a recovered hydrogen for mixing with the syngas; and wherein the control system is configured to control the mixing of the recovered hydrogen with the syngas to provide a predetermined H 2  to CO ratio. 
     Additionally, there is provided these systems, methods and devices having one or more of the following features: wherein the air breathing reformer comprises a reciprocating engine having a variable compression ratio; and, further has: a sensor system to detect ignition/combustion behavior over a range from pre-ignition to misfire; and configured to send a detected ignition/combustion behavior information; wherein the control system is in control communication with the sensor system and the engine; wherein the control system is configured to adjust the engine compression ratio based on the detected ignition/combustion behavior information; and, thereby the control system is configured to adjust the compression ratio in response to a variability in a composition of the flare gas. 
     Further, there is provided these systems, methods and devices having one or more of the following features: has a fuel conditioning system to remove liquids and contaminants harmful to a downstream component, thereby providing a conditioned fuel source; has a separation assembly associated with the synthesis unit, wherein a byproduct is selectively removed from the synthesis unit in situ; has a separation assembly associated with the synthesis unit, wherein a byproduct is selectively removed from the synthesis unit by a liquid or gaseous sweep; wherein the byproduct is water; wherein the separation assembly comprises at least one of a device for membrane separation, a device for absorption, a device for adsorption, or a device for distillation; has a separation assembly associated with the synthesis unit, wherein the end product is selectively removed from the synthesis unit in situ; has a separation assembly associated with the synthesis unit, wherein the end product is selectively removed from the synthesis unit by a liquid or gaseous sweep; wherein the end product is methanol; wherein the separation assembly comprises at least one of a device for membrane separation, a device for absorption, a device for adsorption, or a device for distillation. 
     Yet additionally, there is provided these systems, methods and devices having one or more of the following features: wherein the engine is a compression ignition engine; wherein the engine is a spark ignition engine; wherein the engine is an opposed-piston free-piston linear internal combustion engine; wherein the engine is a crankshaft-driven opposed-piston internal combustion engine with a crankshaft phaser to rotate a phasing of one piston relative to the other thereby modifying overall compression ratio; wherein the engine is a conventional spark-ignited reciprocating engine, wherein the engine is configured for a variable effective compression ratio utilizing camshaft phasers to rotate intake and exhaust camshafts to thereby affect a valve opening and closing; wherein the engine is configured for a variable effective compression ratio utilizing a variable lift, a duration valvetrain, or both to affect a valve opening and closing; and, wherein the engine comprises a multi-link system configured to rotate a crankshaft, and comprising an actuator motor configured to change an endpoint of the multi-link system. 
     Moreover, there is provided these systems, methods and devices having one or more of the following features: including passing the flare gas flow through a first heat exchanger, wherein the first heat exchanger is receiving the reprocessed gas flow from the reformer; whereby the flare gas flow is heated; including controlling the partial oxidation in the reformer; whereby the composition of the syngas in the reprocessed gas flow does not change with the varying composition of the flare gas flow; wherein the predetermined synthesis temperature is from about 200° C. to about 300° C.; wherein the predetermined synthesis pressure is from about 30 bar to about 100 bar; wherein the predetermined synthesis temperature is from about 200° C. to about 300° C. and the predetermined synthesis pressure is from about 30 bar to about 100 bar; wherein second product stream having at least 93% methanol and is thereby at least 93% pure; wherein second product stream having from 90% to 95% methanol and is thereby from 90% to 95% pure; wherein the reformer having an air-breathing reformer; wherein the reformer having one or more of a gas turbine engine, a combustion box, an internal combustion engine, an otto cycle reciprocating engine, a diesel cycle reciprocating engine; wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from 1.1 to about 4; wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from about 1.5 to about 3.0; wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from about 1.5 to about 2.5; wherein a ratio of H 2  to CO in the syngas is from about 1.0 to about 2.0; wherein a ratio of H 2  to CO in the syngas is from 0.8 to 2.5; wherein a ratio of H 2  to CO in the syngas is from about 2 to about 3; wherein a ratio of H 2  to CO in the syngas is from 1.1-2.5; wherein a ratio of H 2  to CO is less than 3; wherein a ratio of H 2  to CO is less than 2.5; wherein the reformer is a reciprocating engine; and the reciprocating engine has one, more than one, or all of: a compression ratio in the range of about 8:1 to about 17:1; an inlet manifold air temperature of ambient temperature to about 300° C.; an inlet manifold air pressure of ambient to about 5 bar; and, a spark timing between TDC and 50 degrees before TDC; an engine speed from about 1,500 rpm to about 8,000 rpm; wherein the reformer is selected from the group consisting of a two-stroke reciprocating engine and a four-stroke reciprocating engine; wherein the reformer is a gas turbine assembly; and the gas turbine assembly has one, more than one, or all of: a first partial oxidation combustor; a two-stage combustion process; a gas turbine combustor; and, a combustion cycle time of from 5 to 50 milliseconds; comprising capturing and using heat generated from the partial oxidation of the rich fuel/air mixture, wherein the heat is used in the continuous method of converting a flare gas to methanol; wherein the flare gas flow has a rate of about 50,000 scfd to about 30,000,000 scfd; wherein the flare gas flow has a rate of greater than about 200,000 scfd; wherein the flare gas flow has a rate of greater than about 200,000 scfd; wherein the flare gas flow has a composition, where in the composition varies over time; wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 7.1 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 7.5 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 8.0 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of about 7.1 kJ/kg° C. to about 8.6 kJ/kg, wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; including providing the fuel/air mixture at a predetermined reformer pressure, to a reformer, wherein the partial oxidation is conducted in the reformer at the predetermined reformer temperature; including controlling the pressure and the temperature of the reprocessed gas flow to provide a predetermined synthesis temperature and a predetermined synthesis pressure of the reprocessed gas flow; wherein the end product is selected from the group consisting of methanol, ethanol, ammonia, mixed alcohols, dimethyl-ether, and F-T liquids; wherein the end product consist of methanol; wherein the end product consists essentially of methanol; wherein the predetermined temperatures and pressures comprises one, more than one, or all of: (i) the predetermined partial oxidation temperature is from about 700° C. to about 1,200° C.; (ii) the predetermined partial oxidation pressure is from about 1 bar to about 70 bar; (iii) the predetermined synthesis temperature is from about 200° C. to about 300° C.; and, (iv) the predetermined synthesis pressure is from about 30 bar to about 100 bar; wherein a variation in a composition of the flare gas does not change a composition of the end product; and wherein the variation in the composition of the flare gas does not require a change in one or more than one, of the predetermined synthesis temperature, the predetermined synthesis pressure, and the predetermined reformer temperature, and the predetermined reformer temperature; wherein a byproduct is selectively removed from the synthesis unit in situ; wherein a byproduct is selectively removed from the synthesis unit by a liquid or gaseous sweep; wherein the byproduct is water; wherein the selected removal is by at least one of membrane separation, absorption, adsorption, or distillation; wherein the end product is selectively removed from the synthesis unit in situ; wherein the end product is selectively removed from the synthesis unit by a liquid or gaseous sweep; wherein the end product is methanol; wherein the selected removal is by at least one of membrane separation, absorption, adsorption, or distillation; wherein the source of the flare has a composition as set out in Tables 1 and 2; and wherein the source of the flare has a varying composition, wherein the varying composition is within the range of compositions set out in Tables 1 and 2. 
     Still further, there is provided these systems, methods and devices having one or more of the following features: wherein the step of partially oxidizing the flare gas, comprises combusting a mixture of the flare gas and a source of oxygen; wherein the oxygen source comprises air, and the mixture has a fuel/air equivalence ratio of greater than 1; wherein the oxygen source comprises air, and the mixture has a fuel/air equivalence ratio of from 1.1 to about 4; wherein the oxygen source comprises air, and the mixture has a fuel/air equivalence ratio of from about 1.5 to about 3.0; using, water, steam, or both in the step of partially oxidizing the flare gas; wherein the step of partially oxidizing the flare gas occurs in an air-breathing reformer; wherein the step of partially oxidizing the flare gas takes place in a reformer stage of a liquid-to-gas system; and wherein, the reformer stage comprises one or more of a gas turbine engine, a combustion box, and a reciprocating engine; wherein the step of converting the reprocessed gas into an end product takes place under a predetermined synthesis temperature and a predetermined synthesis pressure; wherein the predetermined synthesis temperature is from about 200° C. to about 300° C.; wherein the predetermined synthesis pressure is from about 30 bar to about 100 bar; wherein the predetermined synthesis temperature is from about 200° C. to about 300° C. and the predetermined synthesis pressure is from about 30 bar to about 100 bar; wherein the step of partially oxidizing the flare gas takes place under a predetermined reformer temperature and a predetermined reformer pressure; wherein the predetermined reformer temperature is from about 700° C. to about 1,200° C.; wherein the predetermined reformer pressure is from about 1 bar to about 70 bar; wherein the predetermined reformer temperature is from about 700° C. to about 1,200° C.; and the predetermined reformer pressure is from about 1 bar to about 70 bar; wherein the step of converting the reprocessed gas into an end product takes place under a predetermined synthesis temperature and a predetermined synthesis pressure; and the predetermined synthesis temperature is from about 200° C. to about 300° C. and the predetermined synthesis pressure is from about 30 bar to about 100 bar; the step of removing an excess of oxygen from the reprocessed gas; wherein the reprocessed gas contains a synthesis gas; wherein the reprocessed gas consists of a synthesis gas; wherein a variation in a composition of the flare gas does not change a composition of the end product; wherein the step of converting the reprocessed gas into an end product takes place under a predetermined synthesis temperature and a predetermined synthesis pressure; wherein the step of partially oxidizing the flare takes place under a predetermined reformer temperature and a predetermined reformer pressure; wherein a variation in a composition of the flare gas does not change a composition of the end product; and wherein the variation in the composition of the flare gas does not require a change in one or more than one, of the predetermined synthesis temperature and the predetermined synthesis pressure; wherein the step of converting the reprocessed gas into an end product takes place under a predetermined synthesis temperature and a predetermined synthesis pressure; wherein the step of partially oxidizing the flare takes place under a predetermined reformer temperature and a predetermined reformer pressure; wherein a variation in a composition of the flare gas does not change a composition of the end product; and wherein the variation in the composition of the flare gas does not require a change in one or more than one, of the predetermined synthesis temperature, the predetermined synthesis pressure, and the predetermined reformer temperature; wherein less than 1.0 kg of CO 2  per kg of flare gas processed is produced; wherein less than 0.5 kg of CO 2  per kg of flare gas is produced; wherein less than 0.1 kg of CO 2  per kg of flare gas processed is produced; wherein less than 0.05 kg of CO 2  per kg of flare gas processed is produced; wherein the reprocessed gas comprises a syngas; wherein the reprocessed gas consists essentially of a syngas; wherein the reprocessed gas consists of a syngas; where the end product is a liquid; wherein the end product is selected from the group consisting of methanol, ethanol, mixed alcohols, ammonia, dimethyl-ether, and F-T liquids; wherein the end product contains methanol; wherein the end product consists essentially of methanol; wherein steps (a) to (d) or (a) to (e) are net carbon-negative, whereby these steps produce less than about −20 kg CO 2 e per kg of end product produced; wherein steps (a) to (d) or (a) to (e) are net carbon-negative, whereby these steps produce less than about −40 kg CO 2 e per kg of end product produced; wherein steps (a) to (d) or (a) to (e) are net carbon-negative, whereby these steps produce less than about −100 kg CO 2 e per kg of end product produced; wherein steps (a) to (d) or (a) to (e) are net carbon-negative, whereby these steps produce from about −20 kg CO 2 e to about −150 kg CO 2 e, per kg of methanol produced; wherein steps (a) to (d) or (a) to (e) are net carbon-negative, whereby these steps produce from about −40 kg CO 2 e to about −130 kg CO 2 e, per kg of methanol produced; and, wherein the predetermined temperatures and predetermined pressures includes one, more than one, or all of: (i) the predetermined partial oxidation temperature is from about 900° C. to about 1,150° C.; (ii) the predetermined partial oxidation pressure is from about 1 bar to about 70 bar; (iii) the predetermined synthesis temperature is from about 200° C. to about 300° C.; and, (iv) the predetermined synthesis pressure is from about 30 bar to about 100 bar. 
     Yet additionally, there is provided these systems, methods and devices having one or more of the following features: wherein less than about −40 kg CO 2 e per kg of end product produced; wherein less than about −100 kg CO 2 e per kg of end product produced; wherein from about −20 kg CO 2 e to about −150 kg CO 2 e, per kg of methanol produced; wherein from about −40 kg CO 2 e to about −130 kg CO 2 e, per kg of methanol produced; wherein less than 1.0 kg of CO 2  per kg of flare gas is produced; wherein less than 0.5 kg of CO 2  per kg of flare gas is produced; wherein less than 0.1 kg of CO 2  per kg of flare gas is produced; wherein less than 0.05 kg of CO 2  per kg of flare gas is produced; The method of any of claims  73  to  78 , wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 7.1 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 7.5 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of greater than about 8.0 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere; wherein the partial oxidation of the flare gas is conducted at a specific entropy of about 7.1 kJ/kg° C. to about 8.6 kJ/kg° C., wherein a reference state for the specific entropy is based upon −273.15° C. and 1 atmosphere. 
     Moreover, there is provided these systems, methods and devices having one or more of the following features: wherein the starting specific entropy and the final specific entropy are less than about 0.5 kJ/kg° C. of each other; wherein the starting specific entropy and the final specific entropy are less than 0.3 kJ/kg° C. of each other; and, wherein the starting specific entropy and the final specific entropy are less than 0.2 kJ/kg° C. of each other. 
     Moreover, there is provided these systems, methods and devices having one or more of the following features: wherein the reformer is a reciprocating engine; and the reciprocating engine has one, more than one, or all of: a compression ratio in the range of about 8:1 to about 17:1; an inlet manifold air temperature of ambient temperature to about 300° C.; an inlet manifold air pressure of ambient to about 5 bar; to about 300° C.; a spark timing that is between TDC and 50 degrees before TDC; and, an engine speed for from about 8,000 rpm to about 1,800 rpm; wherein the reformer is selected from the group consisting of a two-stroke reciprocating engine and a four-stroke reciprocating engine; wherein the reformer is a gas turbine assembly; and the gas turbine assembly has one, more than one, or all of: a first partial oxidation combustor; a two-stage combustion; a gas turbine combustor; and, a combustion cycle time of from 5 to 50 milliseconds. 
     Still further there is provided these systems, methods and devices having one or more of the following features: wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from 1.1 to about 4; wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from about 1.5 to about 3.0; wherein the rich fuel/air mixture has a fuel/air equivalence ratio of from about 1.5 to about 2.5; wherein the ratio of H 2  to CO in the syngas is from about 1.0 to about 2.0; wherein the ratio of H 2  to CO in the syngas is from 0.8 to 2.5; wherein the ratio of H 2  to CO in the syngas is from about 2 to about 3; wherein the ratio of H 2  to CO in the syngas is from 1.1-2.5; wherein the ratio of H 2  to CO is less than 3; wherein the ratio of H 2  to CO is less than 2.5. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG.  1    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  2    is a T-S diagram of embodiments of the thermodynamic state points for converting waste, e.g., flare gas to syngas to value added products using an embodiment of an air-breathing process in accordance with the present inventions. 
         FIG.  3    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  4    is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flag gas to syngas to methanol, using the system of  FIG.  3    in accordance with the present inventions. 
         FIG.  5    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  6    is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flag gas to syngas to methanol, using the system of  FIG.  5    in accordance with the present inventions. 
         FIG.  7    is a partial cutaway perspective view of an embodiment of a gas turbine for use in an embodiment of a reformer stage in accordance with the present inventions. 
         FIG.  7 A  is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flaRE gas to syngas to methanol, using an embodiment of the present system in accordance with the present inventions. 
         FIG.  8    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  9    is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flag gas to syngas to methanol, using the system of  FIG.  8    having a spark ignition reciprocating engine in accordance with the present inventions. 
         FIG.  9 A  is a table setting out an embodiment of operating conditions for the system of  FIG.  8    having a spark ignition reciprocating engine, and the operating conditions of  FIG.  9    in accordance with the present inventions. 
         FIG.  10 A  is a cross section view of embodiments of engine reformer s accordance with the present inventions. 
         FIG.  10 B  is a cross sectional view of an embodiment of a variable compression engine reformer, showing the piston heights, in accordance with the present inventions. 
         FIG.  11    is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flag gas to syngas to methanol, using the system of  FIG.  8    having a compression ignition reciprocating engine in accordance with the present inventions. 
         FIG.  12    is a cross sectional view of an opposed-piston internal combustion reciprocating reformer engine in accordance with the present inventions. 
         FIG.  13    is a graph comparing the displaced volumes of an opposed piston engine reformer in accordance with the present inventions. 
         FIG.  14    is a schematic flow diagram of an embodiment of a system and process of a modular reformer stage in accordance with the present inventions. 
         FIG.  15    is a schematic flow diagram of an embodiment of a system and process of a modular synthesis stage in accordance with the present inventions. 
         FIG.  16    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  17    is a T-S diagram showing an embodiment of a process, operating conditions and thermodynamic state points for converting flag gas to syngas to methanol, using the system of  FIG.  16    in accordance with the present inventions. 
         FIG.  17 A  is a chart showing compressor power as function of engine backpressure for embodiments of the present systems in accordance with the present invention. 
         FIG.  18    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  19    is a schematic flow diagram of an embodiment of a system and process in accordance with the present inventions. 
         FIG.  20 A  is a pie chart showing the composition of an embodiment of a lean flare gas that can be processed by the present systems and methods in accordance with the present inventions. 
         FIG.  20 B  is a pie chart showing the composition of an embodiment of a rich flare gas that can be processed by the present systems and methods in accordance with the present inventions. 
         FIG.  21    is a graph showing the Wobbe number versus fuel heating value for various components and variations of flare gas that can be processed by embodiments of the present systems and methods in accordance with the present inventions. 
         FIG.  22    is a table showing global warming potential values. 
         FIG.  23    is a chart comparing the CO2e for embodiments of methanol in accordance with the present inventions compared to methanol obtained from convention methods. 
         FIG.  24    is a schematic diagram of an embodiment of a control system for use with embodiments of the present systems and methods in accordance with the present inventions. 
         FIG.  25    is a detailed schematic diagram of an embodiment of a control system for use with embodiments of the present systems and methods in accordance with the present inventions. 
     
    
    
     The T-S diagrams of these Figures, are all plotted and depicted on graphs having the same axes. The Specific Entropy axis (x axis) is in units of kJ/kg° C., and describes the entropy per unit mass of air. The Temperature axis (y axis) is in ° C. and describes the fluid temperature, assumed to have properties similar to air. The relationship between temperature and lines of constant pressure are governed by the physical properties of the fluid. 
     DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     The present inventions generally relate to systems, devices and methods to recover in an economical fashion usable materials from waste gas, e.g., flare gas. In general, embodiments of the present inventions relate to systems, devices and methods, to achieve such recovery at smaller, isolated or remote locations or point sources for the waste gas. 
     In general, embodiments of the present inventions relate to methods, devices and systems for utilizing flare gas to produce a reprocessed gas and then utilizing that reprocessed gas to provide useful and economically viable materials. In particular, embodiments of the present inventions relate to methods, devices and system for producing, recovering and processing reprocessed gas to provide useful and economically viable materials. 
     Embodiments of the present inventions have a reciprocating engine, a gas turbine engine or both, to produce reprocessed gas, preferably syngas. These embodiments can be modular and can easily and readily be positioned at difficult to access locations, locations with limited area for placement of the systems, and combinations and variations of these, where flare gas typically is generated. 
     Systems and Processes—Generally 
     Generally, embodiments of the present systems and methods can be associated with a source of hydrocarbon fuel. The hydrocarbon fuel can be a solid, a liquid, a gas, a slurry and combinations and variations of these. Preferably, the hydrocarbon fuel is a waste gas, and in particular a flare gas. The system is in fluid communication with the hydrocarbon fuel source, by way of for example, pipes, conduits tubulars, hoses and the like, and in this manner the hydrocarbon fuel is provided to the system. The hydrocarbon source can be an active source, in that the hydrocarbons are actively flowing, e.g., flowing from a borehole in the earth, a producing hydrocarbon well, a refinery, or a chemical plant. The hydrocarbon source can be a static source, in that the hydrocarbons are contained in, and obtained from, a holding or collected source, e.g., a holding tank, a tank farm, a tank truck, a rail car, a barge, a container and the like. The source of hydrocarbon fuel can be combinations and variations of active sources, and static sources 
     Generally, the hydrocarbon fuel source, e.g., flare gas, and an oxygen source, e.g., air, are feed to a reformer unit, where the hydrocarbon fuel source is converted through preferably a controlled and predetermined combustion into reprocessed gas, e.g., syngas. This reformer stage of the general system and method, can also have equipment for handling and processing the incoming hydrocarbon fuel source, e.g., flare gas and oxygen source, e.g., air, as well as, equipment to process the reprocessed gas, e.g., syngas, such as for example, valves, controllers, compressors, sensors and monitors, temperature control systems, mixers, filters and screens, separators, equipment to remove water, guard beds, guard bed reactors, deoxo reactors, and other handling and processing equipment and methods. It being understood that some or all of the reprocessed gas, e.g., syngas, processing equipment and methods can be in stages, or located in the general system places other than the reformer stage. 
     Generally, the reformer, and the reformer stage, are preferably operating in a predetermined manner to optimize the composition of reprocessed gas, e.g., syngas, that is obtained, such that the reprocessed gas, e.g., syngas, has a predetermined composition that is determined for optimum performance in its conversion to a value-add product, e.g., methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals, and combination and variations of these. 
     Generally, the reprocessed gas, e.g., syngas, from the reformer is provided to a synthesis unit, e.g., a methanol unit, where the reprocessed gas, e.g., syngas, is converted to a value-add product, e.g., methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals, and combination and variations of these. Preferably, the value-add product is collected and stored as a liquid. It being understood that the value-add product can be gaseous, or in some other state. This synthesis stage, e.g., methanol synthesis stage, can have other equipment and methods for processing and handling the incoming reprocessed gas, e.g., syngas, as well as, for handling and processing the value-add product, e.g., methanol, including for example, valves, controllers, compressors, sensors and monitors, mixers, filters and screens, temperature control systems, separators, equipment to remove water and other handling and processing equipment and methods. The pressure of the reprocessed gas, e.g., syngas, can be, and preferably is controlled, e.g., compressed, prior to being provided to the synthesis unit, e.g., methanol unit, when forming the value-add product, e.g., methanol. 
     Generally, the systems and methods may have additional separation and processing equipment, for example, to remove hydrogen from the value-add product, e.g., methanol. In these embodiments, preferably the hydrogen can be used to generate electricity to operate the system, as well as, potentially other devices, e.g., excess electricity is produced by the system. 
     The stages can be in a single system, in a single integrated system, in separate systems, in two or more modular systems and combinations and variations of these. 
     Generally, the systems and methods have control systems. The control systems can include computers having possessors, memory and data storage. The control systems further can include controllers, e.g., program logic controllers (“PLC”), input/output (“I/O”), sensors, graphic user interface (GUI) and communication protocols and capabilities, e.g., web servers, cellular, satellite. In embodiments, the control system includes a blockchain for authenticating the operation of the system and method, e.g., mass balance of method and operation, and to validate, encrypt and authentic data related to carbon capture, reduction of greenhouse gases, carbon credits, and the like. 
     Thus, the preferred embodiments of the present systems relate to liquid-to-gas systems and methods, e.g., flare gas to methanol. 
     In general, the reformer can be one or more devices or assembly of devices that combusts the waste gas, e.g., flare gas, under controlled and predetermined conditions to provide a reprocessed gas. Preferably one or more of the temperature, pressure, and composition for the reprocessed gas is optimized for use in the synthesis stage, and the controlled and predetermined conditions for operation of the reformer are optimized to provide this optimized temperature, pressure, and composition of the reprocessed gas. Thus, and in general, the reformer can have one or more combustion device, a combustion box, engine, internal combustion engine, reciprocating engine, rotary engine, gasoline engine (i.e., spart ignition), diesel engine (i.e., compression ignition), jet engine, turbine engine, gas turbine engine, air-breathing engine, air breathing combustion device and combinations and variations of these, as well as other peripheral or ancillary devices and equipment. 
     Embodiments of the present inventions can be used to take uneconomic hydrocarbon-based fuels at a well-head and remote locations that are primarily gaseous hydrocarbons and convert them to a more valuable easily condensable or liquid compounds, such as methanol. One source of fuel could be associated gas or flare gas, which is produced as a byproduct at oil wells. Another source is flare gas produced by industrial processes, such as refinery flare gas. Another source could be biogas from landfill or anaerobic digesters. 
     In general, the embodiments of the present systems and methods use waste gas that is preferably flare gas. Examples of the composition of flare gas that any of the reformers of the present systems and methods can process into reprocessed gas, which is then processed by the synthesis units into a value-added product (e.g., methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) are set forth in Table 1 and Table 2. The flare gasses can have one or more, and all of the constituents or components in one or more of the various amounts set forth in these tables. 
     
       
         
           
               
             
               
                 TABLE 1 
               
             
            
               
                   
               
               
                 Examples of flare glass compositions 
               
            
           
           
               
               
               
            
               
                   
                 Gas Constituent 
                 % of Constituent 
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 Name 
                 Formula 
                 Min. 
                 Max 
                 Average 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 Methane 
                 CH 4   
                 7.17 
                 82.0 
                 43.6 
               
               
                   
                 Ethane 
                 C 2 H 6   
                 0.55 
                 13.1 
                 3.66 
               
               
                   
                 Propane 
                 C 3 H 8   
                 2.04 
                 64.2 
                 20.3 
               
               
                   
                 n-Butane 
                 C 4 H 10   
                 0.199 
                 28.3 
                 2.78 
               
               
                   
                 Isobutane 
                 C 4 H 10   
                 1.33 
                 57.6 
                 14.3 
               
               
                   
                 n-Pentane 
                 C5H12 
                 0.008 
                 3.39 
                 0.266 
               
               
                   
                 Isopentane 
                 C5H1; 
                 0.096 
                 4.71 
                 0.530 
               
               
                   
                 neo-Pentane 
                 CSH 12   
                 0.000 
                 0.342 
                 0.017 
               
               
                   
                 n-Hexane 
                 C 6 H 14   
                 0.026 
                 3.53 
                 0.635 
               
               
                   
                 Ethylene 
                 C 2 H 4   
                 0.081 
                 3.20 
                 1.05 
               
               
                   
                 Propylene 
                 C 3 H 6   
                 0.000 
                 42.5 
                 2.73 
               
               
                   
                 1-Butene 
                 C 4 H 8   
                 0.000 
                 14.7 
                 0.696 
               
               
                   
                 Carbon monoxide 
                 CO 
                 0.000 
                 0.932 
                 0.186 
               
               
                   
                 Carbon dioxide 
                 CO 2   
                 0.023 
                 2.85 
                 0.713 
               
               
                   
                 Hydrogen sulfide 
                 H 2 S 
                 0.000 
                 3.80 
                 0.256 
               
               
                   
                 Hydrogen 
                 H 2   
                 0.000 
                 37.6 
                 5.54 
               
               
                   
                 Oxygen 
                 O 2   
                 0.019 
                 5.43 
                 0.357 
               
               
                   
                 Nitrogen 
                 N 2   
                 0.073 
                 32.2 
                 1.30 
               
               
                   
                 Water 
                 H 2 O 
                 0.000 
                 14.7 
                 1.14 
               
               
                   
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 2 
               
             
            
               
                   
               
               
                 Examples of biogas types of flare gas compositions 
               
            
           
           
               
               
            
               
                   
                 Source of biogas type flare gas 
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 Municipal 
                   
                 Agricultural/ 
                 Waste from 
                   
               
               
                 Constituent 
                 waste 
                 Wastewater 
                 Animal waste 
                 food industry 
                 Landfill 
               
               
                   
               
               
                 CH 4  (vol %) 
                 50-60 
                 55-77 
                 50-75 
                 68-75     
                 35-70 
               
               
                 C0 2  (vol %) 
                 34-38 
                 36-38 
                 37-38 
                 26 
                 15-60 
               
               
                   
                   
                 19-33 
                 19-33 
               
               
                   
                   
                 30-45 
                 30-50 
               
               
                   
                   
                 35-45 
                 30-40 
               
               
                 N 2  (vol %) 
                 0-5 
                   
                 &lt;1   
                   
                 &lt;1-40 
               
               
                   
                   
                 &lt;2 
                 &lt;1-2  
               
               
                   
                   
                 &lt;1 
                 &lt;3   
               
               
                 0 2  (vol %) 
                 0-1 
                   &lt;0.5 
                 &lt;0.5 
                   
                 &lt;0.2-5       
               
               
                 H 2 (vol %) 
                   
                   
                   
                   
                 0-5 
               
               
                 CO (vol %) 
                   
                   
                   
                   
                 0-3 
               
               
                 H 2 S (ppm) 
                  70-650 
                   63-3,000 
                    3-7,000 
                 280-&lt;21,500 
                    0-20,000 
               
               
                 Aromatic 
                  0-200 
                   
                   
                   
                   30-1,900 
               
               
                 (mg/m 3 ) 
               
               
                 Ammonia 
                   
                   
                     50-100 mg/m 3   
                   
                 5 ppm 
               
               
                 Halogenated 
                 100-800 
                   
                   
                   
                    1-2,900 
               
               
                 compounds 
               
               
                 (mg/m 3 ) 
               
               
                 Benzene 
                   
                 0.1-0.3 
                 0.7-1.3 
                   
                 0.6-2.3 
               
               
                 (mg/m 3 ) 
               
               
                 Toluene 
                   
                  2.8-11.8 
                 0.2-0.7 
                   
                 1.7-5.1 
               
               
                 (mg/m 3 ) 
               
               
                 Siloxanes 
                   
                 1.5-15  
                 &lt;0.4 
                   
                 0.1-4     
               
               
                 (ppmv) 
               
               
                 Non- 
                   
                   
                   
                   
                   0-0.25 
               
               
                 methane 
               
               
                 organics (% 
               
               
                 dry weight) 
               
               
                 Volatile 
                   
                   
                   
                   
                     0-0.1 
               
               
                 organics (% 
               
               
                 dry weight) 
               
               
                   
               
            
           
         
       
     
       FIGS.  20 A and  20 B  also provide the compositions of flare gas that can occur and are processed by embodiments of the present inventions.  FIG.  20 A  shows a typical composition of a lean flare gas, and  FIG.  20 B  shows a typical composition of a rich flare gas. The lean and rich flare gases can have methane  2001 , ethane  2002 , propane  2003 , butanes  2004 , impurities  2005 , the rich flare gas can also include pentanes  2006  and hexanes and heavier hydrocarbons  2007 .  FIG.  21    is a graph showing the Wobbe number vs fuel heating value for various components and variations of flare gases that can occur and are processed by embodiments of the present inventions. 
     These compositions (e.g., Table 1, Table 2,  FIG.  20 A,  20 B,  21   ) represent compositions, and variations in compositions that the present systems and methods can utilize for gas-to-liquids synthesis (e.g., fare gas to liquid methanol) in embodiments of the present systems and methods in general, as well as embodiments of small modular systems. 
     The present inventions, including the embodiments of the Examples, can use and reprocess flare gases falling within any of the ranges of compositions and constituents set forth in Table 1, Table 2 and combinations of the compositions and ranges in these tables, as well as, other compositions and ranges of components. One of the reasons that these gases are non-economic is that the flare gas, composition is highly variable. Thus, the composition of the flare gas can change from source-to-source, from day-to-day at the same source (transients), from season-to-season (e.g., bio-gases), and over time as the source (e.g., well) ages. These variations have effects on combustion properties such as: heating value, cetane number (delay in time of ignition of fuel), and octane number (resistance to pre-ignition due to compression). Embodiments of the present reformers address these changes and provide the ability to operate in a consistent and efficient manner to process these varying flare gas compositions at a source site to provide a reprocessed gas, e.g., syngas, and preferably provide a consistent, predetermined and both syngas, with respect to the composition and temperature of the syngas. 
     Turning to  FIG.  1    there is shown a generalized embodiment of a system and method for the conversion of a waste gas, e.g., flare gas, into a value-added product, e.g., methanol. The system  100  has a reformer stage  101  and a synthesis stage  102 . The system  100  has an air intake  110 , that feeds air through into a compressor  111 , which compresses the air. The compressed air is feed through heat exchanger  120   a  into a mixer  113 . The system has a waste gas, e.g., flare gas, intake  114 . The waste gas flows through a heat exchanger  120   b  into the mixer  113 . The mixer  113 , provides a predetermined mix of air and waste gas, as taught and disclosed in this specification, to a reformer  114 . 
     The fuel-air mixture that is formed in mixer  113  is preferably rich, more preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     It being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing” reformers, and air breathing engines as used herein are understood to also include engines using air modified with the addition of water, oxygen or both. 
     The reformer  114  combusts the predetermined mixture of waste gas and air (e.g., flare gas and air) to form a reprocessed gas (e.g., syngas). The syngas flows through heat exchangers  120   a ,  120   b  and into a filter  115 , e.g., a particulate filter. 
     After passing through the filter  115 , the reprocessed gas (e.g., syngas) flows to a guard bed reactor assembly  116 , having two guard bed reactors  116   a ,  116   b . The guard bed reactor  116  has materials, e.g., catalysts, that remove contaminates and other materials from the syngas that would harm, inhibit or foul later apparatus and processes in the system. For example, the guard bed reactor  116  may contain catalyst or other materials to remove sulfur (e.g., iron sponge, zinc oxide or similar) and halogenated compounds. 
     After leaving the guard bed reactor  116 , the reprocessed gas (e.g., syngas) flows to a deoxo reactor  117 . The deoxo reactor  117  removes excess oxygen from the reprocessed gas (e.g., syngas) by oxidizing combustible compounds in the mixture such as methane, CO, and H 2 , where the oxygen is converted to water. Catalyst for the deoxo reaction are platinum, palladium, and other active materials supported on alumina or other catalyst support materials. 
     The system  100  has a cooling system  150 , which uses a cooling fluid, e.g., cooling water, that is flow through cooling lines, e.g.,  151 . 
     After leaving the deoxo reactor  117 , the reprocessed gas (e.g., syngas) flows to heat exchanger  120   c . The reprocessed gas (e.g., syngas) then flows from heat exchanger  120   c  to a water removal unit  118 , e.g., a water knockout drum, demister, dryer, membrane, cyclone, desiccant or similar devices, where water is removed from the reprocessed gas (e.g., syngas). In general, the reprocessed gas (e.g., syngas) upon leaving unit  118  should have less than about 5% water by weight, less than about 2%, less than about 1% and less than about 0.1% water. 
     The overall (general) reaction for a rich fuel/air mixture to syngas is given by the equation:
 
ØCH 4 +2[O 2 +3.76 N 2 ]→ a CO+ b H 2   +c CO 2   +d H 2 O+7.52 N 2  
 
Where stoichiometric coefficients a, b, c and are determined by the chemical kinetics, conservation of atomic species, and the reaction conditions.
 
     In addition to syngas minor constituents in the gas exiting the reformer can include water vapor, CO 2 , and various unburned hydrocarbons. 
     After leaving unit  118 , the now dry reprocessed gas (e.g., syngas) is in the synthesis stage  102 . In stage  102  the now dry reprocessed gas (e.g., syngas) flows to an assembly  130 . Assembly  130  provides for the controlled addition of hydrogen from line  131  into the now dry reprocessed gas (e.g., syngas). In this manner the ratio of the syngas components can be adjusted and controlled to a predetermined ratio. The hydrogen is provided from hydrogen separate  139 . The ratio adjusted dry reprocessed gas (e.g., syngas) leaves assembly  130  and flow to compressor  132 . Compressor  132  compresses the reprocessed gas (e.g., syngas) to an optimum pressure as taught and disclosed in this specification, for use the synthesis unit  133 . Preferably, the synthesis unit  133  is a two-stage unit with a first reactor unit  133   a  and a second reactor unit  133   b . Each reactor is a pressure vessel where process gas flows through a catalyst bed in an exothermic reaction. The catalyst bed tubes are typically emersed in a pool of cooling water at a controlled temperature and pressure. Synthesis unit  133  also has heat exchanger  120   e.    
     The synthesis unit  133  converts the ratio adjusted dry reprocessed gas (e.g., syngas) into a value-added product (e.g., methanol, ethanol, mixed alcohols, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals). The value-added product (e.g, methanol, etc.) flows into to heat exchanger  120   d . The value-added product (e.g, methanol, etc.) flows to a collection unit  140 . The collection unit  140  collects the value-added product (e.g, methanol, etc.) and flows it through line  141  for sale, holding, or further processing. 
     Generally, the syngas is compressed to a pressure of about 15 to about 100 bar and preferably 30-50 bar, and about 25 to about 80 bar, at least about 10 bar, at least about 25 bar and at least about 50 bar, and greater and lower pressures. The temperature of the pressurized syngas is adjusted to a temperature of about 150° C. to about 350° C. and preferably 250° C., about 200° C. to about 300° C., about 250° C. to about 375° C., greater than 125° C., greater than 150° C., greater than 200° C., greater than 250° C., greater than 350° C., and less than 400° C., and higher and lower temperatures. The pressure and temperature-controlled syngas is then feed to reactors for transforming the syngas into a more useful, more easily transportable, and economically viable product such as methanol, ethanol, mixed alcohols, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals. In a preferred embodiment methanol is produced using the reaction of syngas to methanol, reactions for hydrogenation of CO, hydrogenation of CO 2 , and reverse water-gas shift using actively cooled reactors, such as a heat-exchanged reactor or boiling water reactor, and a copper containing catalyst such as Cu/ZnO/Al 2 O 3  or the like. In general embodiments of the synthesis state can use the following reactions:
 
CO+2H 2 →CH 3 OH(CO hydrogenation)
 
CO 2 +3H 2 →CH 3 OH+H 2 O(CO 2  hydrogenation)
 
CO+H 2 O→CO 2 +H 2 (reverse water-gas shift)
 
     Generally, and in preferred embodiments, the characteristic length scale of the reactors used in this system are sufficiently small (e.g., micro-channel or mini-channels) that they can be shaped into unconventional shapes and topologies using new 3D printing techniques for metals and other high-temperature materials, thus allowing compact packaging and tight control over reaction conditions. Other strategies for intensification of the downstream synthesis reactions can also be considered, such as selectively removing the product from the reactor in-situ, or in a closely coupled fashion, to shift the equilibrium-limited reaction to higher conversion. This process intensification may minimize the need for large recycle streams or allow the reaction to proceed at milder conditions (e.g., lower pressure) thereby increasing process safety margins. 
     Typically, in reacting the syngas to form the higher value product, unreacted H 2  is also produced. The H 2  can be collected and sold, or used to power the gas turbine or a second generator to produce additional electric power. 
     In general, the ratio of H 2 /CO in the syngas produced by the engine can be tailored to the downstream conversion process. For example, for methanol synthesis or Fischer-Tropsch (F-T) synthesis the ideal H 2 /CO ratio is 2-3. For ammonia synthesis or for hydrogen production, the maximum possible H 2 /CO ratio is desirable and can be enhanced by, for example, steam addition to promote the water-gas shift reaction. For ammonia and hydrogen production, the CO is not required by the downstream synthesis. As such, CO and CO 2  byproducts can be collected, sequestered, stored or utilized for other purposes. 
     The collection unit  140  also has a line that flows gas separated from the value-added product (e.g, methanol, etc.) to valve  135 , where it is sent to hydrogen separate  139 , to a recycle loop  136  or both. Recycle loop has compressor  134  and valve  138  to feed the value-added product (e.g, methanol, etc.) back into the synthesis unit  133 . Hydrogen separation can be achieved by via membrane separation or pressure swing absorption (PSA) or the like in the hydrogen separation unit  139 . 
     Turning to  FIG.  2    there is shown a temperature-entropy (T-S) diagram for the general operation and thermodynamics for the operation of systems of the type shown in  FIG.  1   . The overall conversion process from waste gas, e.g., flare gas, to useful product, e.g., methanol, is described using the T-S diagram of  FIG.  2   . This diagram uses the properties of air, in an air standard approximation of the process.  FIG.  2    outlines the general solutions and operation of systems such as shown in  FIG.  1    from the point of thermodynamics, temperature and pressure. The diagram shows the starting point of the process at ambient conditions, the high temperature and the pressure conditions for rich, partial oxidation, in the reformer, and for high pressure lower temperature reactions for the synthesis of methanol. Thus, there is shown temperature vs entropy dashed line  201  for 60 bar pressure, dashed line  202  for 30 bar pressure, dashed line  203  for 8 bar pressure, and dashed line  204  for 1 bar pressure. (1 atmosphere is equivalent to 1.013 bar.) The temperature and pressure for the incoming air (e.g.,  FIG.  1 ,  110   ) and the waste gas (e.g., flare gas) is at point  206  ( FIG.  2   ). The operating conditions for the reformer stage (e.g.,  FIG.  1 ,  101   ) is shown in zone  210  ( FIG.  2   ). Zone  210  has temperatures above at and above 900° C. Zone  210  has two sub-zones,  210   a ,  210   b . Sub-zone  210   a  is a lower pressure zone (from less than 1 bar to about 25 bar). Sub-zone  210   b  is a higher-pressure zone (from about 20 bar to about 100 bar), and in particular, a high pressure zone for rich, partial oxidation conditions in the reformer (e.g.,  FIG.  1 ,  114   ), which are the preferred condictiones for the embodiments of the present inventions. The optimum operation for the synthesis stage (e.g.,  FIG.  1 ,  131   ) is shown in zone  211  for methanal synthesis. The zone  211  is in a temperature of 200-300° C. and a pressure of about 20 bar to 100 bar. A preferred zone for methanol production is 200-300° C. and a pressure of 30-100 bar. 
     Thus,  FIG.  2    is a graphic representation of conditions that may generally be used in a system to provide for the conversion of flare gas to an end product, in this case methanol, and to preferably do so with a neutral (i.e., provides all energy needed to operate the system and process, or positive, provides excess energy) energy balance. The Specific Entropy axis (x axis) is in units of kJ/kg C, and describes the entropy per unit mass of air. This type of diagram is a convenient way to show physical processes, such as compression and expansion (nearly vertical lines between pressure levels, and heat exchange (usually at near constant pressure). Ideal compression or expansion is isentropic, meaning no change in entropy, between two pressure levels. Compression with real equipment is non-isentropic as indicated by non-vertical lines. The Temperature axis (y axis) is in degrees C. and describes the fluid temperature, assumed to have properties similar to air. The relationship between temperature and lines of constant pressure are governed by the physical properties of the fluid. One of the benefits of the T-S diagram is that is allows a visual representation of the physical processes and the relationship between components. 
     The partial oxidation window  210  defines a region of temperature and pressure where the key partial-oxidation (POX) reactions take place to produce syngas. The region defines the reaction conditions that lead to reaction timescales that are commensurate with the combustion residence in reformers (e.g., a gas turbine, typically 5-50 ms). In general the POX reaction happens at much higher temperatures than that downstream synthesis (e.g., methanol) reactions, which means that the temperature needs to be reduced in a heat exchanger prior to the methanol reactor. 
     The methanol synthesis window  211  defines the region of temperature and pressure where the methanol synthesis reactions take place. The region defines the reaction conditions that lead to reasonable equilibrium conversion for this equilibrium-limited reaction. For this exothermic process, lower temperatures are favored for equilibrium conversion but are constrained on the low end by ensuring sufficient catalyst activity. Higher pressures yield higher equilibrium concentrations due to the net decrease in moles in the reaction but require the cost of compression and design for high pressure. While figure specifically shows a methanol synthesis window, it is understood that other possible downstream synthesis reactions, e.g. Fischer-Tropsch synthesis, require similar conditions. 
     In embodiments, the present systems, can be a mobile system that is contained in a shipping container frame that would fit on a single semi-truck trailer, length about 40 feet to about 60 feet, width about 6 feet to about 10 feet, and height of about 7 feet to about 15 feet. The system may also be in one, two or more separate shipping containers or open skid frames, which are then assembled into a flare gas recovery system at the location of the flare gas, e.g., an oil field, an oil well, an off-shore platform, or a floating production storage and offloading (FPSO) vessel. 
     In embodiments these mobile systems they are sized and configure to processes from flare gas flows of from about 250,000 scfd (standard cubic feet per day) to 30,000,000 scfd, from about 400,000 scfd to 30,000,000 scfd, from about 500,000 scfd to about 20,000,000 scfd, from about 600,000 scfd to about 15,000,000 scfd, from about 700,000 scfd to about 10,000,000 scfd, from about 1,000,000 scfd to about 25,000,000 scfd, greater than about 250,000 scfd, greater than about 500,000 scfd, greater than about 750,000 scfd, less than 10,000,000 scfd, less than 5,000,000 scfd, and less than 1,000,000 scfd, and larger and smaller flows. It further is contemplated that one, two or more of these mobile systems can be placed at a location associated with flare gas, such as an oil field, having a large number of wells, and the flare gas can be piped from several wells to these mobile systems. Thus, providing complete coverage, i.e., capture and recycling of all of the flare gas produced from the oil field. 
     Embodiments of the present inventions are useful in small-scale plants, using one or a plurality of syngas engines, targeting 600,000 scfd (standard cubic feet per day) of inlet gas. The size of such a plant could vary from 80,000 scfd to 3,000,000 scfd, or 20,000 scfd to 100,000 scfd. 
     Embodiments of the present inventions can be incorporated into one or more modular, interconnected skids or containers that are built at a central fabricator shop location and then installed at a field location. A small number of modules comprise the system and when connected at site they form an integrated system. The modular nature of the assembly enables application to remote locations under a range of inlet gas feed volumes, with a minimum of field labor. 
     In general, embodiments of these present systems and processes provide low carbon reprocessing of flare gas, and are preferably carbon neutral-to-negative and energy positive. In this manner embodiments of the present systems and processes capture the flare gas and convert the flare gas to an end product (e.g., methanol, ethanol, etc.) while generating sufficient energy (mechanical, electrical and both) to operate the system. In making the end product, the system is essentially carbon neutral-to-negative due to the combination of two effects: (1) Instead of being released as CO 2  and methane slippage, carbon from the flare gas is sequestered in the methanol thus displacing the flare gas emissions, and (2) instead of producing methanol by conventional means from natural gas or coal, that methanol is displaced by methanol produced from flare gas. 
     Thus, in embodiments the system and the process to produce an end product (e.g., methanol) provide a net negative CO2e for the process and the making of the end product. (As used in this specification CO2e and CO 2 e are synonymous.) Thus, in preferred embodiments the process and resultant end product (e.g., methanol) has from about −40 kg CO2e to −130 kg CO2e, less than −20 kg CO2e, less than −40 kg CO2e, less than −60 kg CO2e, less than −100 kg CO2e and less than −130 kg CO2e per kg of downstream product (e.g, liquid methanol). It should be noted that the typical CO2e for methanol produced from natural gas is 2.1 kg CO2e per kg methanol (based on 45 kg CO2e per MMBTU methanol, 1,040 btu/scf natural gas, and 0.8 kg natural gas per m 3 ). CO2e (carbon dioxide equivalent) is based on a 20-year time horizon global warming potential for methane, based on the IPCC AR5 estimate for methane, and is 85× the global warming potential of CO 2 . 
     Thus, turning to  FIG.  23    there is shown a graph showing the significant improvement, from among other things, an CO2e (and GWP) perspective, compared to conventional sources for methanol (coal, natural gas or CO 2 +H 2  or black liquor).  FIG.  23    shows the significant reduction in CO2e for the present inventions  2300 , which methanol is obtained using the present systems and processes to convert flare gas into syngas into methanol. 
     More preferably, these reformers, the synthesis units and both can also produce sufficient energy to have excess energy available to operate other devices or for other purposes, e.g., oil field operations, computers having high electrical needs for processing complex algorithms, charging electric vehicles, battery storage, etc. 
     More preferably the control system (and sub-systems if any) operate the entire mobile system and processes. The mobile systems are configured for real time or near real time monitoring and control from a remote location, or on site. 
     In embodiments, these systems also have monitory and metering devices to monitor and control and memory devices to record the amount of flare gas processed, the amount of product produced and the amount, if any, of CO 2  produced. This information will be recorded in a secure manner for use or transmission to support carbon capture credits, or other regulatory or private equity or exchange transaction relating to CO 2 . 
     More preferably the control system (and sub-systems if any) operate the entire mobile system and processes. The mobile systems are configured for real time or near real time monitoring and control from a remote location, or on site. 
     A block-chain based record of the carbon captured or carbon offset measurement will improve the quality of the measurement system through networked, secure record keeping. A blockchain-based carbon credit may then be sold as part of a cryptocurrency or other verifiable token in a voluntary carbon market as a carbon offset. 
     Reciprocating Engine Based Reformers—Generally 
     Embodiments of the present inventions have a reciprocating engine and methods of operating those engines to handle the variable combustion properties of the waste gas, e.g., flare gas, sources. Thus, and generally, in some embodiments the reformer  114  of  FIG.  1    is a reciprocating engine. One of the reasons that these gases are non-economic is that the waste gas, e.g., flare gas, composition is highly variable. A consequence of composition variation is the resulting effect on combustion properties such as: heating value, cetane number (delay in time of ignition of fuel), and octane number (resistance to pre-ignition due to compression). These variations can occur from source-to-source, from day-to-day at the same source (transients), from season-to-season (particularly bio-gases), and over time as the source ages. 
     Conventional air-breathing reciprocating engines typically are designed to operate using fuels with a narrow fuel specification. For example, the compression ratio of automotive gasoline engines is selected for the quality of fuel used. The “regular’ gasoline in the United States has an octane rating of 86-87. A higher performance (e.g., higher compression ratio) engine may require premium gasoline with octane rating of 91-94. 
     Embodiment of the present inventions use a commercial reciprocating engine (e.g., off the shelf engine) as the reformer to produce a reprocessed gas, e.g., syngas, by operating the reciprocating engine at rich conditions with high fuel-to-air ratio (equivalence ratio in the range 1.5 to 2.5). To allow the engine to operate off-design from its intended design point, and to operate satisfactorily using fuel that varies over a wide range of octane and cetane numbers, embodiments modify the operating engine parameters including compression ratio, inlet manifold air temperature, inlet manifold air pressure, and engine speed. These modifications apply to both compression ignition engines (diesel cycle) and spark ignition engines (otto cycle). For spark ignition engines, the spark timing can also be used to adapt the engine operation to fuel variation. 
     In embodiment of a modular system, the system and method utilize a nominally air-breathing engine that is operated under rich conditions to produce a reprocessed gas, e.g., syngas, from a waste gas, e.g., flare gas, source. Variation in composition of the fuel results in variation in combustion properties that effect engine operability. In particular, impacted operability parameters include, for example:
         Engine mis-fire—inability to transition from spark discharge to propagating flame, in one or more cylinders of an engine.   Pre-ignition—Premature combustion of the fuel-air mixture in one or more of the cylinders in an engine.   Auto-ignition (knock)—Spontaneous ignition of the fuel-air mixture ahead of the propagating flame.   Low combustion efficiency—high levels of unburned fuel in the exhaust, due to exhaust valve opening before combustion propagation across the cylinder volume is complete, or unburned fuel in crevice volumes and quenching on cold surfaces, or can be related to mis-fire.       

       FIGS.  20 A,  20 B, and  21   , as well as, Tables 1 and 2, show the range of compositions for the flare gas that can be processed by embodiments of the reciprocating engine reformers, including the embodiments of the Examples, into reprocessed gas, e.g., syngas. 
     These mixtures and their individual constituents represent wide range of octanes, with the heavier hydrocarbons having lower octane and hence a greater tendency to pre-ignite or auto-ignite. Specific values of octane number, a key measure of mixture reactivity, are shown in Table 3. Estimated values of octane number for the lean and rich gas in  FIGS.  20 A and  20 B  are shown in Table 3. 
       FIG.  21    shows how the fuel energy per unit volume varies with gas composition. This variation affects, and is address by the sizing and control of the fuel delivery system. 
     
       
         
           
               
             
               
                 TABLE 3  
               
             
            
               
                   
               
               
                 (Octane numbers of individual constituents (Octane 
               
               
                 Number (research octane number = RON)) 
               
            
           
           
               
               
               
               
            
               
                   
                 Octane 
                 Octane 
                 AKI 
               
               
                 Constituent 
                 (research/RON) 
                 (motor/MON) 
                 (R + M)/2 
               
               
                   
               
            
           
           
               
               
               
               
            
               
                 Methane 
                 135 
                 122 
                 128.5 
               
               
                 Ethane 
                 108 
               
               
                 Propane 
                 112 
                 97 
                 104.5 
               
               
                 Butane 
                 93 
                 90 
                 91.5 
               
               
                 Pentane 
                 61.7 
                 61.9 
                 61.8 
               
               
                 Lean Associated 
                 126 (est) 
               
               
                 Gas (table 1) 
               
               
                 Rich Associated 
                 117 (est) 
               
               
                 Gas (table 1) 
               
               
                   
               
            
           
         
       
     
     Turning to  FIG.  21    it is shown that for gaseous fuels, changes in fuel composition also influence the energy content of the fuel, as quantified by fuel heating value per unit volume (Wobbe number). This figure shows typical ranges of Wobbe number vs fuel heating value for a range of fuel compositions. 
     Variation in fuel properties sets up a fundamental tension in the design of a reciprocating engine system, which embodiments of the present inventions address. On one hand, high compression ratio and high inlet air temperature are beneficial for the combustion characteristics to produce syngas with desired H 2 /CO ratio (typical range about 1.0 to about 2.0, preferably 1.5 to 2.0) with low emission of unburned fuel. On the other hand, high compression ratio and high inlet air temperature can result in pre-ignition, or autoignition of the fuel-air mixture if the fuel becomes more reactive. Conversely, if the fuel becomes less reactive, increased compression ratio or inlet air heating would be beneficial. Thus, setting a specific design point for the engine is not compatible with smooth engine operation with fuel, e.g., flare gas, that has variable combustion properties. 
     In embodiments, the solution to this problem is modify the engine operating properties while the engine is operating. In embodiments, a combination of modified critical operating engine parameters including:
         compression ratio (effective compression ratio or geometric compression ratio)   range 8:1 to 17:1   inlet manifold air temperature, range of ambient temperature to 300 C.   inlet manifold air pressure, ambient to 5 bar.   spark timing, TDC (top dead center, e.g. zero degrees) to MBT (minimum spark advance for best torque, e.g. 30 degrees typical, 15-45 degree range)   and engine speed, 800 rpm to engine max (eg. 1800 rpm)   the range of conditions above can be applied to a two-stroke or four-stroke reciprocating engine.       

     In embodiments, to detect if the engine is operating correctly, in a controller, and preferably an autonomous control system, a set of sensors can be used. This autonomous control system is preferable a part of, or in control communication with, the control system for the overall system (e.g., system  100  of  FIG.  1   ), and can be for example a sub-system, a separate controller, and preferably is also in control communication with the general control system for the overall system. These sensors can include:
         Knock detection (vibration-based sensors) mounted to the block or head   Lambda sensor (sensor that infers air to fuel ratio from exhaust gas composition, typically mounted downstream of exhaust valves)   Exhaust temperature (typically thermistor or thermocouple) mounted downstream of the exhaust valves.   Intake manifold temperature or pressure.   Fuel sensors including mass flow, dew point temperature, and heating value (e.g., calorimeter).       

     In an embodiment, of the reciprocating engine, the fuel-air mixture is rich, preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     In embodiments of the reciprocating engine reformer, it being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing engines” defined herein are understood to also include engines using air modified with the addition of water or oxygen. 
     The reciprocating engine produces, a reprocessed gas, e.g, syngas, (as well as heat and mechanical energy, which can be used to power and operate the entire process) which is then filtered and heat from the syngas is recovered by a heat exchanger. 
     The overall (general) reaction for rich fuel/air mixture to syngas in a reciprocating engine is given by the equation:
 
ØCH 4 +2[O 2 +3.76 N 2 ]→ a CO+ b H 2   +c CO 2   +d H 2 O+7.52 N 2  
 
Where stoichiometric coefficients a, b, c and are determined by the chemical kinetics, conservation of atomic species, and the reaction conditions.
 
     In addition to syngas minor constituents in the gas exiting the reciprocating engine include water vapor, CO 2 , and various unburned hydrocarbons. 
     Gas Turbine Engine Based Reformers—Generally 
     Embodiments of the present systems and methods, utilizing gas turbine reformers, generally relate to systems, devices and methods to convert otherwise uneconomic hydrocarbon-based fuel, e.g., flare gas to a to value-added, easily transported products (such as, methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals, and combination and variations of these). These embodiments in general have a flare gas (i.e., fuel) conditioning system, an air-breathing gas engine, and a conditioning assembly that conditions the syngas for storage, shipping, later processing and combinations and variations of these. The flare gas is conditioned to remove impurities and materials that could be detrimental to later processing steps. The flare gas (e.g., fuel gas for the system) is then mixed with air and ignited in an engine. 
     Embodiments of the present inventions have a turbine engine, e.g., air breathing gas turbine engine, as the reformer to produce reprocessed gas, preferably syngas. Thus, and generally, in some embodiments the reformer  114  of  FIG.  1    is a gas turbine engine. In some embodiments gas turbines are preferred under certain circumstances (such as larger magnitudes of wellhead flows), as they provide advantages over embodiments using reciprocating engines to produce syngas. The gas turbine-based systems are suitable for larger scale gas-to liquid (e.g., flare gas to methanol) applications where there are packaging limitations, e.g., on-site footprint limitations. Embodiments of the present systems are modular and can easily and readily be positioned at difficult to access locations, locations with limited area for placement of the systems, and combinations and variations of these, where for example flare gas is generated. 
     Further, the gas turbine-based system has the capability to handle, e.g., receive and process to an end product, flare gases having a wide and varying ranges of composition, which in some embodiments can provide an advantage over a reciprocating engine. Changes in flare gas (i.e., fuel) composition can change ignition characteristics and burning times. For a reciprocating engine with fixed compression ratio, such changes should be addressed to avoid the potential of damaging engine knocking or misfires and exhaust value over-heating, as well as other problems. 
     Gas turbine combustion systems can burn a wide variety of liquid and gaseous fuels, preferably provided they are suitably free of contaminants that would lead to corrosion or deposits. Also, the flame is continuously burning in a gas turbine, unlike reciprocating engines where ignition must occur in each cylinder during each power stroke. Moreover, gas turbines can operate continuously for about 8,000 hrs (up to 24,000 hrs for some models, and potentially longer), without shutdown, and extended intervals greater than 24,000 hrs for major overhaul. With more moving parts and more wear surfaces, reciprocating engines must typically be shutdown to replace lubricating fluids at about 2,000 to about 4,000 hours intervals, and major overhaul at about 8,000-12,000 hours. 
     One of the many advantages that a gas turbine system may have over a reciprocating engine system, in some embodiments, is that the flare gas components can vary and gas turbine performance is not affected. In general, flare gasses having compositions as set out in  FIGS.  20 A,  20 B,  21   , as well as, Tables 1 and 2, can be processed by the embodiments of gas turbine systems of the present inventions, including the Examples. However, some factors that still may play a part in performance of gas turbine system include: 1) margin to the dew point, i.e., superheat, of the flare gas of 10° C., ensuring gaseous inlet fuel, 2) keeping the heating value of the overall fuel is &gt;400 BTU/scf., and 3) corrosive elements, such as Vanadium, are filtered out prior to combustion. 
     Embodiments of the present systems and methods, utilizing gas turbine reformers, generally relate to systems, devices and methods to convert otherwise uneconomic hydrocarbon-based fuel, e.g., flare gas to a to value-added, easily transported products (such as, methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals, and combination and variations of these). These embodiments in general have a flare gas (i.e., fuel) conditioning system, an air-breathing gas turbine, and a conditioning assembly that conditions the syngas for storage, shipping, later processing and combinations and variations of these. The flare gas is conditioned to remove impurities and materials that could be detrimental to later processing steps. The flare gas is then compressed to a pressure of about 8 to about 35 bar (typically corresponding to about 1.2× the pressure ratio of the gas turbine air compressor), about 5 to about 40 bar, at least about 10 bar, at least about 20 bar and at least about 1.1× the pressure ratio of the gas turbine air compressor, from about 1.05× to about 1.8× the pressure ratio of the gas turbine air compressor and greater and smaller values. The compressed flare gas (i.e., fuel for the system) is then mixed with air and ignited in a gas turbine. The pressure of the air when mixed with the compressed fuel gas, preferably will be the same as the fuel gas. The temperature of the compressor discharge air is a known function of the inlet air temperature, the compression ratio, and the compressor efficiency, and the temperature of the compressed discharge air should be about 150° C. to about 600° C., about 150° C. to about 500° C., about 200° C. to about 400° C., greater than about 150° C., greater than about 300° C., and greater than about 500° C. The temperature of the compressed waste gas, e.g., flare gas, should be about 100° C. to about 300° C., about 150° C. to about 300° C., about 125° C. to about 200° C., greater than about 150° C., greater than about 200° C., and greater than about 250° C., and less than 350° C. and higher and lower values. 
     Generally, for embodiments of the gas turbine reformers, the fuel-air mixture is rich, preferably having an overall fuel/air equivalence ratio (ϕ or ER) 0.98 or greater, greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     In embodiments of the gas turbine reformers, it is understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing engines” defined herein are understood to also include engines using air modified with the addition of water or oxygen. 
     Preferably the gas turbines are smaller sized units, from about 200 kW to about 5000 kW, from about 200 kW to about 2000 kW, and less than 6000 kW, less than 5000 kW, less than 3000 kW and less than 2000 kW, although larger and smaller sizes may be used. 
     The gas turbine produces syngas, (as well as heat and mechanical energy, which can be used to power and operate the entire process) which is then filtered and heat from the syngas is recovered by a heat exchanger. 
     The overall (general) reaction for rich fuel/air mixture to syngas in a gas turbine is given by the equation:
 
ØCH 4 +2[O 2 +3.76 N 2 ]→ a CO+ b H 2   +c CO 2   +d H 2 O+7.52 N 2  
 
Where stoichiometric coefficients a, b, c and are determined by the chemical kinetics, conservation of atomic species, and the reaction conditions.
 
     In embodiments of the systems initiation of combustion occurs at near ambient conditions in the combustion chamber of gas turbine when the shaft of the turbine is turned at low cranking speed. 
     An additional feature, for an embodiment of the combustion chamber is to stage the fuel addition to extend the rich limit of combustion. For example, in a forward part of the combustion chamber part of the fuel is mixed with air to produce a flame with very stable combustion (for example near stochiometric conditions). Downstream of that stable flame zone additional fuel is added to meet the overall equivalence ratio required to achieve the H 2 /CO ratio of the downstream process. 
     In addition to syngas minor constituents in the gas exiting the gas turbine include water vapor, CO 2 , and various unburned hydrocarbons. 
     In general, embodiments of a partial-oxidation gas turbine comprise a compressor, combustor, and turbine. The compressor takes ambient air and raises the pressure. The compressor discharge air is mixed with excess fuel and partially oxidized in the combustor. The discharge of the combustor is expanded through the turbine to ambient conditions. The work produced by the turbine typically exceeds the work required to drive the compressor. A conceptual drawing of one embodiment of the partial-is shown in  FIG.  7   . 
     Thus, turning to  FIG.  7    the reformer gas turbine assembly  700 . The gas turbine  700  has a gas turbine engine  710 , (e.g., air breathing turbine engine) that has an air intake  711 , a compressor  712 , a turbine  713 , and an exhaust flow  714 . The gas turbine  710  has a shaft configured for rotation with the turbine and compressor that is connected to a motor or generator  715 . The gas turbine  700  has two part or two stage combustor  740 , that provides for partial oxidation combustion of the flare gas. The two stage combustor  740  has a first stage, which is a rich partial oxidation combustor  741  and a second stage, which is the gas turbine  710 . The flare gas is injected at  742  and is partially combusted in reaction zone  743  of first stage combustor  741 . The product of this partial combustion is directed into the gas turbine  710  where further combustion, with the incoming air from intake  711  occurs to provide syngas. Syngas is produced in  743  (inside the combustion chamber), flows up and through heat exchanger  760  and out line  733  to the synthesis stage. The post-reaction synthesis gas returns through line  732  from the synthesis unit. This flow is heated by the syngas produced in  743 , and expanded through the turbine in  713 . A portion of the flow of line  732  is unheated and flows through bypass line  731 . This gas may have a high N 2  gas flow for use on seals and secondary cavities. 
     The numbers in circles in  FIG.  7    relate to a location for a process condition, e.g., state points, discussed with respect to T-S diagrams relating to specific Examples and as discussed in the Examples. 
     EXAMPLES 
     The following examples are provided to illustrate various embodiments of the present waste gas conversion processes and systems. These examples are provided to illustrate various embodiments of the present gas-to-liquid conversion processes and systems. These examples are for illustrative purposes, may be prophetic, and should not be viewed as, and do not otherwise limit the scope of the present inventions. 
     The embodiments of these Examples 1 to 54 can have or utilize one or more of the embodiments, processes, methods, features, functions, parameters, components, or systems disclose and taught in the “Systems and Processes—Generally”, “Reciprocating Engine Based Reformers—Generally”, and “Gas Turbine Engine Based Reformers—Generally” sections of this specification, and combinations and variations of each of these; as well as, one or more of the embodiments, processes, methods, features, functions, parameters, components, or systems provided in one or more of the other Examples and other embodiments taught and disclosed in this specification. 
     Example 1 
     A system and process to convert otherwise uneconomic hydrocarbon-based fuel such as flare gas to value-added, easily transported products (such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) using an autonomous, modular system comprising the following elements: (1) a fuel conditioning system to meet requirements of downstream components; (2) an air-breathing gas turbine, modified to operate a rich, partial-oxidation reformer, to produce a syngas mixture with a H 2 /CO ratio suitable for synthesis of liquids; (3) a combination of integrated heat exchangers, compression system components, and heat exchangers to prepare the syngas for the downstream synthesis reactors; and (4) a downstream synthesis reactor system to produce useful liquid hydrocarbon products. 
     Example 2 
     A system and process to convert otherwise uneconomic hydrocarbon-based fuel such as flare gas to value-added, easily transported products (such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) using an autonomous, modular system comprising the following elements: (1) a fuel conditioning system to meet requirements of downstream components; (2) an air-breathing gas turbine, modified to operate a rich, partial-oxidation reformer, to produce a syngas mixture with a H 2 /CO ratio suitable for synthesis of liquids; (3) a combination of integrated heat exchangers, compression system components, and heat exchangers to prepare the syngas for the downstream synthesis reactors; (4) a downstream synthesis reactor system to produce useful liquid hydrocarbon products; and, (5) a hydrogen recycle loop to improve overall system process performance. 
     Example 3 
     The systems and process of Examples 1 and 2 can also have one, or more, or all of the following additional features: (6) optional substantially oxygen-free gas recirculation loop to cool and protect downstream components of the combustor, such as seals, bearings, and secondary cavities; (7) optional O 2  enrichment of the inlet stream to the gas turbine via membrane separation or partial air separation unit; (8) a recuperator heat exchanger (from (3)) and a turbo expander to recover energy from the high pressure exhaust gas from the downstream synthesis reactor; (9) integration of a closed-loop operating system with custom instrumentation; (10) a cloud-based remote monitoring system, including AI-trained anomaly detection for dynamic preventative maintenance and operations control; (11) optional offtake pathways to utilize byproducts, such as nitrogen, water, and CO 2  for reinjection, well recompletions, or other purposes; (12) optional water (or steam) injection into the rich combustor to improve H 2 /CO ratio and reduce carbon build-up on surfaces within the combustor and turbine. 
     Example 4 
     A gas-to-liquid system takes uneconomic hydrocarbon-based fuels, e.g., flare gas, at a well-head and remote locations that are primarily gaseous hydrocarbons and convert them to a more valuable easily condensable or liquid compounds, such as methanol. One source of source fuel could be associated gas or flare gas, which is produced as a byproduct at oil wells. Another source could be biogas from landfill or anaerobic digesters. 
     A small-scale plant, targeting 3,000,000 scfd (standard cubic feet per day) of inlet gas. The size of such a plant could vary from 300,000 scfd to 15,000,000 scfd. The plant is incorporated into one or more modular, interconnected skids or containers that are built at a central fabricator shop location and then installed at a field location. A small number of modules comprise the system and when connected at site they form an integrated system. The modular nature of the assembly enables application to remote locations under a range of inlet gas feed volumes, with a minimum of field labor. The modular nature further improves flexibility to deploy or redeploy these assets, reduces initial capital outlay and project financial risks, allows matching of the process throughput to the flare gas supply, and reduces time-to-market by allowing module fabrication and site preparation to occur in parallel. 
     Example 5 
     Turning to  FIG.  3    there is shown a schematic of a system and method, and preferably a modular plant and processes, for the recovery and conversion of flare gas into methane.  FIG.  4    is a T-S graph showing a preferred operating conditions and thermodynamic state points of the process that can be used for the operation of the embodiment of  FIG.  3   . The reference points (numbers— 31 ,  32 ,  33 ,  34 ,  35 ,  36 ,  37 ,  37 . 5 ,  38 ,  39 , in  FIG.  3   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  3   , and those process conditions are shown by corresponding reference points in  FIG.  4   . The prime reference points in  FIG.  4    (e.g.,  35 ′,  36 ′) indicate expected cycle points considering efficiency of the components. Reference point  7 . 5  indicates the discharge of the downstream synthesis process. And, reference points  33   s  and  35   s  indicates idealized isentropic processes (vertical process lines) conditions. The starting specific entropy for this process is at points  31 ,  32  (6.9 kJ/kg° C.) and the final specific entropy point for this process is  39  (7.04 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.14 kJ/kg° C.). 
     Turning to  FIG.  3    there is shown a combustion chamber system  300  for converting flared gas from a flare gas source (e.g., oil well, gas well, land fill, agriculture plant, waste water treatment plant, etc.) into methanol. The system  300  has a reformer section or stage  350  and a synthesis section or stage  351 . 
     The system  300  has an air intake  301  that flows the air to a filter  302 , where dust, sand, particulates, etc., are removed from the air, after which the air flows to compressor  303 , where it is compressed. The compressed air leaves compressor  303  and flows to an air breathing combustion box  304 , where the flare gas is partially oxidized. The combustion box  304  can be a single stage, two stages, or more. 
     Flare gas (e.g., raw flare gas) from a flare gas source (e.g., an oil or gas well or field) enters system  300  through line  311  and flows to a separator  313 , where liquids and gas are separated. The separated liquids, including liquid hydrocarbons having 3 or more carbon atoms, and flow from the separator  313  through line  314 . These liquids can flow through line  315  to a storage tank  316 . The separated liquids can flow through line  317 , and are pumped, by pump  318  into the combustion box  304 . 
     The gases components of the flare gas exit the separator  313  via line  312  and flow to a gas conditioning unit  310 . Gas conditioning unit  310  can remove harmful materials to the process, including H 2 S (hydrogen sulfide), as well as, any materials that would harm or poison any catalysts that are used in the system. The conditioned flare gas leaves conditioning unit  310  and flows to gas filter  309 , where further harmful or detrimental materials are removed, e.g., iron sulfides, sulfur, as well as any materials that would harm or poison any catalysts that are used in the system. The conditioned and filtered flare gas leaves filter  309  and flows into gas compressor  306 , which is driven by motor  307 . The compressor  306 , compresses the flare gas to a predetermined pressure and temperature as taught and disclosed in this specification and for example shown in  FIG.  4   , and flows this flare gas into combustion box  304 . Water, steam, or oxygen may also be added to the combustion box  304  via line  305 . 
     The compressed flare gas can be at a pressure of about 3 to about 60 bar, about 8 to about 35 bar (typically corresponding to about 1.2× the pressure ratio of the gas turbine air compressor), about 5 to about 40 bar, at least about 10 bar, at least about 20 bar, and at least about 1.1× the pressure ratio of the air compressor, from about 1.05× to about 1.8× the pressure ratio of the gas air compressor and greater and smaller values. The compressed flare gas (i.e., fuel for the system  300 ) is then mixed with the compressed air and ignited in the combustion box  304 , where it is partially oxidized. The pressure of the air when mixed with the compressed flare gas, can be any of the above ranges of pressure for the flare gas; and preferably will be the same pressure as the flare gas. In the embodiment of the operation of the process as shown in  FIG.  4   , the pressure of the flare gas and air is 8 bar, when they are introduced into the combustion box  304  for partial oxidation to form syngas. 
     The syngas exits the combustion box  304  and flows into turbine  320 , where its pressure is reduced (see, e.g., state points  34  (preferred 8 bar) and  35  (preferred 1 bar)). The turbine  320  is connect to compressor  303  by rotation shaft  329 , where it turns compressor  303 . The turbine  320  is connect to motor or generator  336  by rotating shaft  319   a . Rotating shaft  319   b  contexts turbine  337  with motor or generator  336 . 
     The syngas leaves turbine  320  via line  321  and flows into filter  322  where particulates, e.g., soot, are removed. The syngas then flows into heat exchange  323  where the temperature is lowered to the methanol synthesis window, preferably 200° C.-300° C. (see, e.g.,  FIG.  4   ). The heat exchanger  323  is part of a heat exchanger loop  324 . The syngas then flows from heater exchanger  323  to a water separation unit  325 . Water is removed from the water separation unit  325  via line  326 . The syngas leaves unit  325  and flows via line  321   a  into compressor  327 , which is driven by motor  328 . The compressor compresses the syngas to about 30-100 bar. For the preferred operation shown in  FIGS.  3  and  4   , by state points  36  (1 bar) and  37  (30 bar). 
     The syngas leaves compressor  327  and flows to a heat exchanger  329 , where the temperature is maintained for the methanol synthesis window, and flows from the heat exchanger  329  via line  321   b  to the synthesis unit  329 . The synthesis unit has two reactors  329   a  and  329   b . It is noted that a single stage or reactor can be used, and that more than two stages or reactors can be used. The synthesis unit  329  has a line  335  for discharging water, methanol or both. The synthesis unit  329  converts the syngas to methanol, which then flows to hold and separation unit  330 . Unit  330  separates the liquid methanol from any remaining gas. The methanol is discharged through line  331  for storage, further processing, use, shipping, etc. The gases flow through line  332  to hydrogen separator unit  333 . Hydrogen leaves separation unit  333  via line  334  and flows back to the synthesis unit  329 , where it is used to adjust the H 2 /CO ratio of the syngas. The remaining gases, e.g., low H 2  concentration stream, from the unit  333 , flow through line  339   b  for injection into the turbine  320 ; and flow through line  339   a  to turbine  337  and then to exhaust line  338 . 
     This arrangement of components in this example is an efficient way to achieve the particular state points of the process that produce methanol in an economic and effective manner. These state points include: 1) starting at ambient conditions, 2) raising temperature and pressure to achieve rich partial oxidation, and 3) cooling and pressurizing to achieve downstream synthesis. The carbon intensity and energy intensity of the process can be managed by tuning the cycle points to just match the POX and synthesis windows. Furthermore, the cycle points can be tuned to minimize the energy requirements for midstream and downstream separations processes. 
     The operation of the system of  FIG.  3    under the embodiment of the state conditions of  FIG.  4    revolves around a rich-burn reformer and a synthesis reactor. Unlike a traditional gas turbines and reciprocating engines, the combustor  304  runs at rich conditions, up to equivalence ratio of about 4 so the fuel, i.e., flare gas, experiences rich partial oxidation (POX). The system  300  has fuel, i.e., flare gas, conditioning system, heat exchangers, compressors, and turbines. The fuel conditioning system separates liquids from gases in the feed stream and removes compounds that can damage the gas turbine or synthesis reactor. The heat exchangers and compressors take the syngas mixture at the exit of the gas turbine and adjust the temperature and pressure to deliver the target conditions for the synthesis reactor. Within the synthesis sub-system is an optional H 2  recycle loop. The gas at the exit of the synthesis reactor is heated in a recuperating (e.g., counter-flow) heat exchanger to an elevated temperature and then expanded to ambient conditions. 
     Example 6 
     The system of  FIG.  3   , and other embodiments of the present systems, can be operated and configured in a manner that limits expansion of the gas through the turbine  337 , such that the work from the compressor  303  and turbine sections  320  is matched. In this way, the exhaust gas from line  338  is pressurized above ambient pressure and less compression work, with compressors  303 , and in particular  329 , is required to meet the pressure required by the downstream synthesis reactor  329 , thus reducing the compression stages and equipment complexity. For example, compressor  329  can be reduced in size, work required, and even eliminated. 
     Example 7 
     Turning to  FIG.  5    there is shown a schematic of a system and method, and preferably a modular plant and processes, for the recovery and conversion of flare gas into methane.  FIG.  6    is a T-S graph showing a preferred operating conditions and thermodynamic state points of the process that can be used for the operation of the embodiment of  FIG.  5   . The reference points (numbers— 51 ,  52 ,  53 ,  54 ,  55 ,  56 ,  57 ,  58 ,  59 , in  FIG.  5   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  5   , and those processes conditions are shown by corresponding reference points in  FIG.  6   . And, reference points  53   s  indicates idealized isentropic processes (vertical process lines) conditions. The starting specific entropy for this process is at points  51 ,  52  (6.9 kJ/kg° C.) and the final specific entropy point for this process is  58  (7.2 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.3 kJ/kg° C. 
     Turning to  FIG.  5    there is shown a combustion chamber system  500  for converting flared gas from a flare gas source (e.g., oil well, gas well, land fill, agriculture plant, waste water treatment plant, etc.) into methanol. The system  500  has a reformer section or stage  550  and a synthesis section or stage  551 . 
     The system  500  has an air intake  501  that flows the air to a filter  502 , where dust, sand, particulates, etc., are removed from the air, after which the air flows to compressor  503 , where it is compressed. The compressed air leaves compressor  503  and flows to an air breathing combustion box  504 , where the flare gas is partially oxidized. The combustion box  504  can be a single stage, two stages, or more. 
     Flare gas (e.g., raw flare gas) from a flare gas source (e.g., an oil or gas well or field) enters system  500  through line  511  and flows to a separator  513 , where liquids and gas are separated. The separated liquids, including liquid hydrocarbons having 3 or more carbon atoms, and flow from the separator  513  through line  514 . The separated liquids can flow through line  514 , and are pumped, by pump  518  into the combustion box  504 . 
     The gases components of the flare gas exit the separator  513  via line  512  and flow to a gas conditioning unit  510 . Gas conditioning unit  510  can remove harmful materials to the process, including H 2 S, as well as, any materials that would harm or poison any catalysts that are used in the system. The conditioned flare gas leases conditioning unit  510  and flows to gas filter  509 , where further harmful or detrimental materials are removed, e.g., iron sulfides, sulfur, as well as any materials that would harm or poison any catalysts that are used in the system. The conditioned and filtered flare gas leaves filter  509  and flows into gas compressor  506 . The compressor  506 , compresses the flare gas to a predetermined pressure and temperature as disclosed and taught in this specification and for example shown in  FIG.  6   , and flows this flare gas into combustion box  504 . Water, steam, or oxygen may also be added to the combustion box. 
     The compressed flare gas can be at a pressure of about 3 to about 60 bar, about 8 to about 35 bar (typically corresponding to about 1.2× the pressure ratio of the gas turbine air compressor), about 5 to about 40 bar, at least about 10 bar, at least about 20 bar, and at least about 1.1× the pressure ratio of the air compressor, from about 1.05× to about 1.8× the pressure ratio of the gas air compressor and greater and smaller values. The compressed flare gas (i.e., fuel for the system  500 ) is then mixed with the compressed air and ignited in the combustion box  504 , where it is partially oxidized. The pressure of the air when mixed with the compressed flare gas, can be any of the above ranges of pressure for the flare gas; and preferably will be the same pressure as the flare gas. In the embodiment of the operation of the process as shown in  FIG.  6   , the pressure of the flare gas and air is 8 bar, when they are introduced into the combustion box  504  for partial oxidation to form syngas. 
     The compressor  503  is connected by rotation shaft  529 , to motor or generator  536 . Rotating shaft  519   b  contexts turbine  537  with motor or generator  536 . 
     The syngas exits the combustion box  504  via line  521  and flows into filter  522  where particulates, e.g., soot, are removed. The syngas then flows into heat exchange  523  where the temperature is lowered to the methanol synthesis window, preferably 200° C.-500° C. (see, e.g.,  FIG.  6   ). The heat exchanger  523  is part of a heat exchanger loop  524 . The syngas then flows from heater exchanger  523  to the synthesis unit  529 . The synthesis unit has two reactors  529   a  and  529   b . It is noted that a single stage or reactor can be used, and that more than two stages or reactors can be used. The synthesis unit  529  converts the syngas to methanol, which then flows to hold and separation unit  530 . Unit  530  separates the liquid methanol from any remaining gas. The methanol is discharged through line  531  for storage, further processing, use, shipping, etc. The gases flow through line  532  to hydrogen separator unit  533 . Hydrogen leaves separation unit  533  via line  534  and flows back to the synthesis unit  529 , where it is used to adjust the H 2 /CO ratio of the syngas. The remaining gases, e.g., low H 2  concentration exhaust products stream, from the unit  533 , flow into the turbine  537  and then to exhaust line  538 . 
     The operation of the system of  FIG.  5    under the state conditions of  FIG.  6    revolves around the integration of the synthesis reactor within the gas turbine cycle. The fuel system, compressor, and rich combustor are similar to the systems of Example 5. However, instead of delivering combustion products into the turbine, in this Example 7 the syngas at the exit of the combustor  504  flows through a recuperating heat exchanger  523  until the syngas temperature is acceptable for the synthesis reactor  529 . At the exit of the synthesis reactor  529 , the spent gas is returned through the recuperating heat exchanger system  524 , and delivered to the turbine  537  to expand back to ambient pressure. An advantage of this embodiment is fewer components, but it requires a high-temperature recuperating heat exchanger and more sophisticated controls, than the embodiment of Example 5. 
     Example 8 
     An embodiment of these systems and methods includes the use of water in the waste gas, e.g., flare gas, or added directly into the POX combustor to raise the H 2 /CO ratio to enhance the efficiency and effectiveness of the downstream synthesis reactor. This embodiment can be used with any of the present systems, including the Examples. 
     Example 9 
     An embodiment of these systems and methods includes the addition of substantially oxygen-free gas, to the reformer, e.g., the turbine, including such as that at the exit of the high pressure side of hydrogen separator, to pressurize seals and ensure that no air is entrained into the secondary passages of the turbine. This embodiment can be used with any of the present systems, including the Examples. 
     Example 10 
     A hybrid system, consisting of reciprocating engine(s) and gas turbine(s), whereby the reciprocating engine(s) may be used for auxiliary power generation, or to supply additional synthesis gas is also contemplated. The hybrid system may contain reciprocating engines and gas turbines at scales sized to match the inlet gas feed. 
     Example 11 
     In an embodiment of the system of  FIG.  1   , the reformer is the gas jet turbine of  FIG.  7   . This system can be preferably operated as set forth in the T-S diagram of  FIG.  7 A . The reference points (numbers— 3 ,  4 ,  5 ,  6 ,  7 ,  8 , in  FIG.  7   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  7   , and those process conditions are shown by corresponding reference points in  FIG.  7 A . The state point  1  (not shown in  FIG.  7   ), is the conditions of the flare gas as it is injected at  742 . The starting specific entropy for this process is at points  1 ,  2  (6.9 kJ/kg° C.) and the final specific entropy point for this process is 8 (7.2 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.3 kJ/kg° C. 
     Example 12 
     Turning to  FIG.  8    there is shown an embodiment of a system and method for the conversion of flare gas into a value-added product. The system  800  has a reformer stage  801  and a synthesis stage  802 . The system  800  has an air intake  810 , that feeds air through into a compressor  811 , which compresses the air. The compressed air is feed through heat exchanger  820   a  into a mixer  813 . The system has a flare gas intake  884 . The flare gas flows through a heat exchanger  820   b  into the mixer  813 . The mixer  813 , provides a predetermined mix of air and flare gas, as disclosed and taught in greater detail in this specification, to a reformer  814 , which is a reciprocating engine. 
     The fuel-air mixture that is formed in mixer  813  is preferably rich, more preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     It being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing” reformers, and air breathing engines as used herein are understood to also include engines using air modified with the addition of water, oxygen or both. 
     The reciprocating engine  814  combusts the predetermined mixture of flare gas and air to form syngas. The syngas flows through heat exchangers  820   a ,  820   b  and into a filter  815 , e.g., a particulate filter. 
     After passing through the filter  815 , the syngas flows to a guard bed reactor assembly  816 , having two guard bed reactors  816   a ,  816   b . The guard bed reactor  816  has materials, e.g., catalysts, that remove contaminates and other materials from the syngas that would harm, inhibit or foul later apparatus and processes in the system. For example, the guard bed reactor  816  may contain catalyst or other materials to remove sulfur (e.g., iron sponge, zinc oxide or similar) and halogenated compounds. 
     After leaving the guard bed reactor  816 , the syngas flows to a deoxo reactor  817 . The deoxo reactor  817  removes excess oxygen from the reprocessed gas (e.g., syngas) by oxidizing combustible compounds in the mixture such as methane, CO, and H 2 , where the oxygen is converted to water. Catalyst for the deoxo reaction are platinum, palladium, and other active materials supported on alumina or other catalyst support materials. 
     The system  800  has a cooling system  850 , which uses a cooling fluid, e.g., cooling water, that is flow through cooling lines, e.g.,  851 . 
     After leaving the deoxo reactor  817 , the syngas flows to heat exchanger  820   c . The reprocessed gas (e.g., syngas) then flows from heat exchanger  820   f  and  820   c  to a water removal unit  818 , e.g., a water knockout drum, demister, dryer, membrane, cyclone, desiccant or similar, where water is removed from the syngas. In general, the syngas upon leaving unit  818  should have less than about 5% water by weight, less than about 2%, less than about 1% and less than about 0.1% water. 
     After leaving unit  818 , the now dry syngas is in the synthesis stage  802 . In stage  802  the now dry syngas flows to an assembly  830 . Assembly  830  provides for the controlled addition of hydrogen from line  831  into the now dry syngas. In this manner the ratio of the syngas components can be adjusted and controlled to a predetermined ratio. The hydrogen is provided from hydrogen separate  839 . The ratio adjusted dry syngas leaves assembly  830  and flow to compressor  832 . Compressor  832  compresses the syngas to an optimum pressure as taught and disclosed in this specification, for use the synthesis unit  833 . Preferably, the synthesis unit  833  is a two-stage unit with a first reactor unit  833   a  and a second reactor unit  833   b . Synthesis unit  833  also has heat exchanger  820   e.    
     The synthesis unit  833  converts the ratio adjusted dry syngas into a value-added product, methanol. The methanol flows into to heat exchanger  820   d . The methanol flows to a collection unit  840 . The collection unit  840  collects the methanol and flows it through line  841  for sale, holding, or further processing. 
     Generally, the syngas is compressed to a pressure of about 15 to about 100 bar and preferably 30-50 bar, and about 25 to about 80 bar, at least about 10 bar, at least about 25 bar and at least about 50 bar, and greater and lower pressures. The temperature of the pressurized syngas is adjusted to a temperature of about 150° C. to about 350° C. and preferably 250° C., about 200° C. to about 300° C., about 250° C. to about 375° C., greater than 125° C., greater than 150° C., greater than 200° C., greater than 250° C., greater than 350° C., and less than 400° C., and higher and lower temperatures. The pressure and temperature-controlled syngas is then feed to reactors for transforming the syngas into a more useful, more easily transportable, and economically viable product such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals. In a preferred embodiment methanol is produced using the reaction of syngas to methanol, reactions for hydrogenation of CO, hydrogenation of CO 2 , and reverse water-gas shift using actively cooled reactors, such as a heat-exchanged reactor or boiling water reactor, and a copper containing catalyst such as Cu/ZnO/Al 2 O 3  or the like. 
     Generally, and in preferred embodiments, the characteristic length scale of the reactors used in this system are sufficiently small (e.g., micro-channel or mini-channels) that they can be shaped into unconventional shapes and topologies using new 3D printing techniques for metals and other high-temperature materials, thus allowing compact packaging and tight control over reaction conditions. Other strategies for intensification of the downstream synthesis reactions can also be considered, such as selectively removing the product from the reactor in-situ, or in a closely coupled fashion, to shift the equilibrium-limited reaction to higher conversion. This process intensification may minimize the need for large recycle streams or allow the reaction to proceed at milder conditions (e.g., lower pressure) thereby increasing process safety margins. 
     In general, the ratio of H 2 /CO in the syngas produced by the engine can be tailored to the downstream conversion process. For example, for methanol synthesis or Fischer-Tropsch (F-T) synthesis the ideal H 2 /CO ratio is 2-3. For ammonia synthesis or for hydrogen production, the maximum possible H 2 /CO ratio is desirable and can be enhanced by, for example, steam addition to promote the water-gas shift reaction. For ammonia and hydrogen production, the CO is not required by the downstream synthesis. As such, CO and CO 2  byproducts can be collected, sequestered, stored or utilized for other purposes. 
     The collection unit  840  also has a line that flows gas separated from the methanol to tee-connector  835 , where it is sent to hydrogen separate  839 , to a recycle loop or both. Recycle loop has compressor  834  and valve  838  to feed the methanol back into the synthesis unit  833 . Hydrogen separation can be achieved by via membrane separation or pressure swing absorption (PSA) or the like in the hydrogen separation unit  839 . 
     The remaining gas after hydrogen separation is sent through loop  890  and through heat exchanger  820   f  to turbine expander  891 , where the gas is then sent to exhaust. 
     Example 13 
     In an embodiment of the system of  FIG.  8   , the reformer  814  is a spark ignition (otto cycle) reciprocating engine. This system can be preferably operated as set forth in the T-S diagram of  FIG.  9   . The reference points (numbers— 81 ,  82 ,  83 ,  84 ,  85 ,  86 ,  87 ,  88 ,  89  in  FIG.  8   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  8   , and those process conditions are shown by corresponding reference points in  FIG.  9   . The line from state point  84   a ′ to  84   b ′ represents a reduction in compression ratio that occurs in response to a more reactive flare gas fuel. State point  85   b  relates to the syngas exiting the syngas reformer after the expansion of the turbocharger. The expansion from  85  to  85   b  occurs within the turbocharger. The starting specific entropy for this process is at points  81 ,  82  (6.9 kJ/kg° C.) and the final specific entropy point for this process is  89  (6.95 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.05 kJ/kg° C. 
       FIG.  9 A  is a table set out further operating conditions for the system of this Example.  FIG.  9 A  shows the compression power (gross and net) for flare gas to methanol process using the turbo expander  891  under the conditions of a 3 bar backpressure and a 50 bar methanol synthesis pressure. 
     Example 14 
     In an embodiment of the system of  FIG.  8   , the reformer  814  is a compression ignition (diesel cycle) reciprocating engine. This system can be preferably operated as set forth in the T-S diagram of  FIG.  11   . The reference points (numbers— 81 ,  82 ,  83 ,  84 ,  85 ,  86 ,  87 ,  88 ,  89  in  FIG.  8   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  8   , and those process conditions are shown by corresponding reference points in  FIG.  11   . The line from state point  84   a ′ to  84   b ′ represents a reduction in compression ratio that occurs in response to a more reactive flare gas fuel. State point  85   b  relates to the syngas exiting the syngas reformer after the expansion of the turbocharger. The expansion from  85  to  85   b  occurs within the turbocharger. The starting specific entropy for this process is at points  81 ,  82  (6.9 kJ/kg° C.) and the final specific entropy point for this process is  89  (6.95 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.05 kJ/kg° C. 
     Example 15 
     Turning to  FIGS.  10 A and  10 B  there is shown an embodiment of a variable compression ratio engine that can be used as a reformer in embodiments of the present systems, including the Examples. The variable compression ration engine,  1002  can be one such as the Nissan VC-turbo engine, that uses a multi-link system in place of a traditional connecting rod to rotate the crankshaft, and an actuator motor changes the multi-link system endpoint in order to vary the pistons&#39; reach to transform the compression ratio. 
       FIG.  10 A  is a cutaway view of a conventional engine  1001  compared to a partial cutaway view of a variable compression engine  1002 . The piston  1010  are the crank  1011  are the same. The conventional engine  1001  has a connection rod  1020 , and a 2 nd  balancer  1021 . The variable compression engine  1002  has a U-link  1030 , an L-link  1031 , a C-link  1032 , a control shaft  1033 , an A-link  1034  and an actuator Motor  1035 . 
     The components of the variable compression engine  1002  make it possible to vary the compression ratio continuously as needed within the range of about 8:1 (for high load) to about 14:1 (for low load). For an automobile engine made by Nissan, the optimal compression ratio can be continuously set to match the operation of the accelerator pedal by the driver. A schematic of this linkage is shown on  FIGS.  10 A and  10 B . The effects of this linkage on on piston height is shown on  FIG.  10 B . This approach can be applied to a two-stroke or four-stroke reciprocating engine, although an engine as described here is preferably operated as a four-stroke. Thus, using the variable compression engine as a reformer, the optimal compression ratio for producing syngas can be continuously set to accommodate combustion properties from variation in the flare gas with variable compression ratio. In this manner, in embodiments, an engine with a linkage to rotate the crankshafts to vary the compression ratio to run rich with variable flare gas compositions is utilized to produce synthetic gas. 
     Thus, and for illustration, turning to  FIG.  10 B , the relative adjustments for the variable compression reciprocating engine reformer  1002  are shown. Piston height  1010   a  is for 14:1 compression ratio. Piston height  1010   b  is for 8:1 compression ratio. The adjustment of the linkages are shown by arrows  1031   a  and  1033   a.    
     Example 16 
     Turning to  FIG.  12   , there is shown an embodiment on an engine for production of syngas from compression-ignition of rich fuel-air mixtures is preferred due to simplicity (lower part count) and better performance (high compression ratio yielding faster burn times). This engine reformer can be used in embodiments of the present systems, including the Examples. An example architecture is the opposed-piston free-piston linear internal combustion engine with integrated linear motor/generator, such as that produced by MainSpring Energy (aka Etagen). U.S. Pat. No. 2,362,151 discloses a basic engine configuration for modification in accordance with the teachings of the present specification, the entire disclosure of which is incorporated herein by reference. 
     Thus, turning to  FIG.  12   , the a free piston engine “A” is connected to two single phase generators “B” and “B”, which can be operated by the engine. When used as a reformer the generators may not be present, or can be used to power components in the system. 
     The free piston engine A has a cylinder  61  in which the pistons  62 - 62   a  reciprocate, and which is surrounded by a second cylinder  63  having the annular water chamber  65  therein encompassing the explosion chamber  64  of the engine. Annular air chambers  66  are formed in the end portions of cylinder  63  as shown and are connected by a passage  67  whereby the air pressure in the two chambers is equalized. Intake passages  68  lead from chamber  66   a  to the interior of cylinder  61 , and discharge passages  69  lead from the opposite end portion of the cylinder  61  to discharge into manifold  10 . 
     Inasmuch as the two ends of the device are duplicates one end only will be described in detail and similar parts on the other end will be indicated by similar characters followed by the character “a”. 
     Through the outer end of chamber  66  are formed passages  11  fitted with inwardly opening check valves  12 , the said passages leading to an annular cylinder  13  axially disposed relative to cylinder  61  and somewhat larger In diameter than said cylinder-and mounted end wise thereon as at  14 . This cylinder  13  is provided with an air intake passage at  15  fitted with an inwardly operating check valve as at  18  and disposed adjacent the inner end of said cylinder. 
     The piston  12  has an enlarged head  17  thereon to reciprocate in chamber  13 , and a stem  18  projects axially outwardly from said head and through the bearing  19  in the outer end of the chamber  13  and has a shoulder  20  formed therein as shown, exteriorly of chamber  13  to form a seat for the magnet  21 . 
     The magnet  21  is a field magnet, and in the present instance comprises a part  22 , circular in form, seated on the shoulder  20 , a second member  24  of smaller diameter seated on the member  22 , and a winding of wire on the second member as indicated at  23  and grounded to said second part. This second member  24  is also provided with a flange  25  extending outwardly from its outer end at right anglers to its axis, and then turned backwardly in parallel relation with the axis and with a diameter slightly greater than the chamber  13  to encompass the magnet parts  22  and  24  as shown. The winding  23  is energized by means of a battery at  26  grounded to the engine at  21  and connected to a bar  28  mounted upon the engine at  29  and extending forwardly thereof as indicated, in parallel relation with its axis. A shoe  630  slidably engages the bar  28  and is in fixed contact with the coil  23  so that the magnet is energized at all times regardless of its position with relation to the fixed end of the device. 
     The armature comprises a coil of wire as  631  within a supporting cylinder  632  mounted upon the outer end of chamber  11  to encompass the magnet parts  22  and  24 . Wires as  633  connect the armatures  631  and  631   a , and electricity is taken off of these wires as at  34 . 
     When the device is in operation the outward movement or the piston heads  17 - 17   a  draw air into the chambers  13 - 13   a  through valves  16 - 16   a , and on their inward movement push the air through valves  12  into chamber  66 - 66   a . The air in chamber  68   a  is sufficiently compressed to flow forcibly into the cylinder  61  when the piston  62   a  uncovers the passages  68 . The exhaust passages  69  are uncovered at substantially the same time as the passages  68  so that the air entering the cylinder  61  at  68  will scavenge the same and carry out all of the burnt gases at  69  leaving the cylinder filled with fresh air. 
     But in the movement of pistons  12 - 12   a  just described the piston heads  17 - 17   a  compress the air entrapped in the chamber  13 - 13   a , which form cushions which forcibly drive the said pistons back in cylinder  61  compressing the air therein. As the pistons approach each other the compressed air trapped between them, or at least a small portion thereof, is discharged through passage  635  and pipe  637  to actuate a plunger  638  in injector  639  in which the fuel oil is admitted at  49  and discharged through valve  41  into combustion chamber  64 . These parts are proportioned and arranged to form a combustible mixture at the moment when the pistons  62 - 62   a  approach each other most closely, the resulting explosion diving the pistons outwardly again to repeat the cycle. The valves at  47 - 47   a  are inserted in chambers  13 - 13   a  to permit the drawing of air into said chambers to compensate for such air as may leak out of the same past the heads  17 - 17   a  or paste bearings  19 - 19   a.    
     In an engine of this kind the pistons  62 - 62   a  are reciprocated at high speed, upwards of some ten thousand times a minute, and the magnets  21 - 21   a  are, or course, reciprocated at the same high speed. In this manner the mechanical energy of the engine is converted into electrical energy, since the rapid reciprocation of the magnetic fields about the magnets  21 - 21   a  through the induction cons  631 - 631   a  will rapidly after the number of lines or force passing through the coils. 
     This engine is modified with digital electronic controls (sensor and control system) to achieve a practical and high efficiency engine for small-scale power generation. This approach can be applied to a two-stroke or four-stroke reciprocating engine, although a linear engine with fixed ports in the side walls is generally operated as a two-stroke. Thus, this linear engine operating under rich conditions can be a reformer in any of the Examples of systems to produce syngas. Preferably this linear engine reformer is a free-piston configuration with an electronically-control linear motor/generator that allows the compression ratio to be varied according the properties of the incoming fuel. This linear engine reformer may also have a free-piston configuration with sensors to detect the in-cylinder combustion behavior under rich conditions and automatically adjust the compression ratio. 
     Example 17 
     An embodiment of a variable compression ratio engine reformer, for use in embodiments of the present systems, including the Examples, is through a crankshaft-driven opposed-piston engine utilizing a variable phaser on the crankshafts. Combustion chamber volume in such an engine is dictated by the relative positions of the pistons. Offsetting motion of one piston to the other increases minimum volume, thereby reducing compression ratio. Turning to  FIG.  8    there is shown a comparison of displaced volume when the opposed pistons are synchronized (left) vs offset by 40 degrees (right). The compression ratio is higher when the pistons are synchronized, and reduces when the pistons are offset. An example of an opposed-piston linear engine with crank shafts is an engine developed by Achates Engines. 
     In an embodiment the opposed piston engine reformer has a variable phaser on the crankshafts to run rich with variable fuel to produce synthetic gas is novel. 
     This approach can be applied to a two-stroke or four-stroke reciprocating engine, although a linear engine with fixed ports in the side walls is generally operated as a two-stroke. 
     Example 18 
     Turning to  FIG.  14    there is shown a modular reformer system and process that is a portion of a liquid-to-gas system  1400 . This system  1400  has a reformer stage  1401 , that is placed on a transport system  1490  (e.g. skid, truck bed, rail car, ship deck, barge, drilling platform, drill ship, container, or other platform, base or container), that can be readily moved by rail, air, truck or ship. The stage  1401  has a compressor  1411  and an engine reformer  1414 , as well as other components as labeled on the drawing as taught and disclosed in this specification. It being understood that any of the engine reformers of the present systems and Examples could be used in the stage  1401 . The stage  1401  provides clean syngas. 
     This stage can be used, or positioned with any unit that can further process the syngas into move valuable products. For example, this stage  1401  can be used with the modular methanol synthesis unit of the present inventions, such as the unit of Example 19. 
     Example 19 
     Turning to  FIG.  15    there is shown a modular methanol synthesis system and process that is a portion of a liquid-to-gas system  1400 . This system  1400 , has a synthesis stage  1402 , that can be placed on a transport system  1491  (e.g., skid, truck bed, rail car, ship deck, barge, drilling platform, drill ship, container, or other platform, base or container), that can be readily moved by rail, air, truck or ship. This stage  1402  is configured to receive clean, syngas. This stage  1402  can be used with the reformer stage  1401  of Example 18, as well as with other reformer stages as taught and disclosed in this specification, including the Examples. The stage  1402  produces an end product, e.g., methanol, from syngas. 
     The stage  1402  has a synthesis unit  1433 , which is a two-stage unit with a first reactor unit  1433   a  and a second reactor unit  1433   b . The stage has a hydrogen separator  1439 , a collection unit  1440 , as well as, other components as labeled on the drawing and as taught and disclosed in this specification. It being understood that any of the configurations of synthesis stages of the present systems and Examples could be used in stage  1402 . 
     This stage  1402  can be positioned near a tank, storage container, or source of syngas and process that syngas into methanol. 
     Example 20 
     Turning to  FIGS.  16 ,  17  and  17 A .  FIG.  16    shows an embodiment of a system and method for the conversion of flare gas into a value-added product, e.g., methanol. The system  1600  has a reformer stage  1601  and a synthesis stage  1602 . The system  1600  has an air intake, that feeds air through into a compressor  1611 , which compresses the air. The compressed air is feed through a heat exchanger into a mixer. The system has a flare gas intake. The flare gas flows through a heat exchanger into the mixer. The mixer provides a predetermined mix of air and waste gas, as taught and disclosed in this specification, to a reformer  1614 , which is a reciprocating engine. 
     The fuel-air mixture that is formed in mixer is preferably rich, more preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     It being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing” reformers, and air breathing engines as used herein are understood to also include engines using air modified with the addition of water, oxygen or both. 
     The reciprocating engine  1614  combusts the predetermined mixture of flare gas and air to form syngas. The syngas flows through heat exchangers and into a filter, e.g., a particulate filter. 
     After passing through the filter, the syngas flows to a guard bed reactor assembly, having two guard bed reactors. After leaving the guard bed reactor, the syngas flows to a deoxo reactor. The deoxo reactor removes excess oxygen from the reprocessed gas (e.g., syngas). 
     The system has a cooling system, which uses a cooling fluid, e.g., cooling water, that is flow through cooling lines. 
     After leaving the deoxo reactor, the syngas flows to heat exchanger. The reprocessed gas (e.g., syngas) then flows from the heat exchanger to a water removal unit, e.g., a water knockout drum, demister, dryer, membrane, cyclone, desiccant or similar, where water is removed from the syngas. In general, the syngas upon leaving unit the water removal unit should have less than about 5% water by weight, less than about 2%, less than about 1% and less than about 0.1% water. 
     After leaving the water removal unit, the now dry syngas flows into in the synthesis stage  1602 . In stage  1602  the now dry syngas flows to an assembly that provides for the controlled addition of hydrogen from line into the now dry syngas. In this manner the ratio of the syngas components can be adjusted and controlled to a predetermined ratio. The hydrogen is provided from hydrogen separate  1639 . The ratio adjusted dry syngas leaves the assembly and flows to compressor  1632 . Compressor  1632  compresses the syngas to an optimum pressure as taught and disclosed in this specification, for use the synthesis unit  1633 , which is a two-stage unit with a first reactor unit  1633   a  and a second reactor unit  1633   b . Synthesis unit  1633  also has heat exchanger. 
     The synthesis unit  1633  converts the ratio adjusted dry syngas into a value-added product, e.g., methanol. The methanol flows into to heat exchanger and then to a collection unit  1640 . The collection unit  1640  collects the methanol and flows it through a line for sale, holding, or further processing. 
     The collection unit  1640  also has a line that flows gas separated from the methanol to tee-connector, where it is sent to hydrogen separate  1639 , to a recycle loop or both. Recycle loop has a compressor and a valve to feed the methanol back into the synthesis unit  1633 . 
     The system  1600  can be preferably operated as set forth in the T-S diagram of  FIG.  17   . The reference points (numbers— 161 ,  162 ,  163 ,  164 ,  165 ,  166 ,  167 ,  168 ,  169  in  FIG.  17   ) correspond to process conditions, i.e., state points, at those locations in the system of  FIG.  16   , and those process conditions are shown by corresponding reference points in  FIG.  17   . The starting specific entropy for this process is at points  161 , (6.9 kJ/kg° C.) and the final specific entropy point for this process is  169  (6.95 kJ/kg° C.). Thus, the difference between the start and final specific entropy is 0.05 kJ/kg° C. 
     Further, turning to  FIG.  17 A  there is shown the predicted compressor work (total and for syngas compression only), as a function of the engine exhaust backpressure for a 50 bar downstream synthesis pressure. These data are generated using a chemical process simulation that performed the mass and energy balances for the embodiment of a liquid-to-gas system and method of the type shown in  FIG.  16   . The syngas compressor is treated as a three-stage compressor with interstage cooling. The isentropic efficiency of the compressor is assumed to be 75%, representative of industrial centrifugal and reciprocating compressors. The syngas ratio adjustment recycle stream enters the compressor at the inlet to the second stage. Increasing the engine exhaust backpressure from 2 bar up to 3 bar decreases the compression work by 20.4%. Further increasing the backpressure from 2 bar to 4 bar decreases the compression work by 28.0%. This trend suggests a diminishing return and therefore optimal value of engine exhaust backpressure for the embodiment of  FIG.  16    would be in the 2-5 bar range to balance reduction in compression work with reduction in engine reformer breathing and performance. 
     Example 21 
     Turning to  FIG.  18    there is shown an embodiment of a system and method for the conversion of flare gas into a value-added product, e.g., methanol. The system  1800  is configured to reduce the compression work required by raising the back pressure of the engine above ambient, to about 5 bar. 
     The system  1800  has a reformer stage  1801  and a synthesis stage  1802 . The system  1800  has an air intake, that feeds air through into a compressor  1811 , which compresses the air. The compressed air is fed through heat exchanger in to a mixer. The system has a flare gas intake. The flare gas flows through a heat exchanger  1820   b  into the mixer  1813 . The mixer  1813 , provides a predetermined mix of air and waste gas, as taught and disclosed in this specification, to a reformer  1814 , which is a reciprocating engine. 
     The fuel-air mixture that is formed in mixer is preferably rich, more preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     It being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing” reformers, and air breathing engines as used herein are understood to also include engines using air modified with the addition of water, oxygen or both. 
     The reciprocating engine  1814  combusts the predetermined mixture of flare gas and air to form syngas. The syngas flows through heat exchangers and into a filter, e.g., a particulate filter. 
     After passing through the filter, the syngas flows to a guard bed reactor assembly, having two guard bed reactors. After leaving the guard bed reactor, the syngas flows to a deoxo reactor. The deoxo reactor removes excess oxygen from the reprocessed gas (e.g., syngas). 
     The system has a cooling system, which uses a cooling fluid, e.g., cooling water, that is flow through cooling lines. 
     After leaving the deoxo reactor, the syngas flows to heat exchanger. The reprocessed gas (e.g., syngas) then flows from the heat exchanger to a water removal unit, e.g., a water knockout drum, demister, dryer, membrane, cyclone, desiccant or similar, where water is removed from the syngas. In general, the syngas upon leaving unit the water removal unit should have less than about 5% water by weight, less than about 2%, less than about 1% and less than about 0.1% water. 
     After leaving the water removal unit, the now dry syngas is in the synthesis stage  1802 . In stage  1802  the now dry syngas flows to an assembly that provides for the controlled addition of hydrogen from line into the now dry syngas. In this manner the ratio of the syngas components can be adjusted and controlled to a predetermined ratio. The hydrogen is provided from hydrogen separate  1839 . The ratio adjusted dry syngas leaves the assembly and flows to compressor  1832 . Compressor  1832  compresses the syngas to an optimum pressure as taught and disclosed in this specification, for use the synthesis unit  1833 , which is a two-stage unit with a first reactor unit  1833   a  and a second reactor unit  1833   b . Synthesis unit  1833  also has heat exchanger. 
     The synthesis unit  1833  converts the ratio adjusted dry syngas into a value-added product, e.g., methanol. The methanol flows into to heat exchanger and then to a collection unit  1840 . The collection unit  1840  collects the methanol and flows it through a line for sale, holding, or further processing. 
     The collection unit  1840  also has a line that flows gas separated from the methanol to tee-connector, where it is sent to hydrogen separate  1839 , to a recycle loop or both. Recycle loop has a compressor and a valve to feed the methanol back into the synthesis unit  1833 . 
     Stage  1802  has a line  1883  for taking depleted methanol from unit  1833   b  and sending it through heat exchanger  1820   d . The stage  1802  has a methanol desorber  1880  that has pump  1881 . Line  1882  for desorber  1880  flows methanol rich product to heat exchanger  1820   g.    
     In the operation of system  1800  the preferred process uses a two-stage methanol synthesis reactor with reactive separation in the second stage (Rxtr  2 )  1833   b  only. The first stage (Rxtr  1 )  1833   a  is generally far from equilibrium and does not warrant reactive separation. The example shown in this figure is reactive absorption or membrane separation with a liquid sweep. Methanol is selectively removed from the reactor in situ resulting in a methanol-depleted gaseous stream containing primarily unreacted syngas and a methanol-rich absorbent stream. Compared to other embodiments, the primary recycle loop is not used because of the improved single-pass conversion. The methane-rich absorbent stream passes through a valve to reduce the pressure and desorb the methanol which is then condensed and sent the product stream. The absorbent, now in a regenerated state, is pumped back to the synthesis pressure and recirculated to the reactor. The pumping work for the absorbent is minimal compared to the syngas compressor work because the liquid absorbent is nearly incompressible. The reactor could be a trickle bed or a membrane reactor with the liquid absorbent (sweep) on the permeate side of the membrane. Any methanol that does not partition into the absorbent is condensed out of the gas phase in a downstream separation step and combined with the methanol product stream 
     Example 22 
     Turning to  FIG.  19    there is shown an embodiment of a system and method for the conversion of flare gas into a value-added product, e.g., methanol. The system  1900  has a reformer stage  1901  and a synthesis stage  1902 . The system  1900  has an air intake, that feeds air through into a compressor  1911 , which compresses the air. The compressed air is feed through heat exchanger into a mixer. The system has a flare gas intake. The flare gas flows through a heat exchanger  1920   b  into the mixer  1913 . The mixer  1913 , provides a predetermined mix of air and waste gas, as taught and disclosed in this specification, to a reformer  1914 , which is a reciprocating engine. 
     The fuel-air mixture that is formed in mixer is preferably rich, more preferably having an overall fuel/air equivalence ratio (ϕ or ER) greater than 1, greater than 1.5, greater than 2, greater than 3, from about 1.5 to about 4.0, about 1.1 to about 3.5, about 2 to about 4.5, and about 1.1 to about 3, and greater values. 
     It being understood that oxygen can be added to the air. And that water or steam may also be injected into the mixture of air and fuel, or to air or fuel individually. From about 1 to about 20% (molar) water can be injected, from about 10 to about 15% (molar water), from about 5 to about 17% (molar) water, more than 5% (molar) water, more than 10% (molar) water, more than 15% (molar) water, and less than 25% (molar) water, water can be injected. Following oxygen enrichment, the combustion air can have from about 21% to about 90% oxygen. “Air-breathing” reformers, and air breathing engines as used herein are understood to also include engines using air modified with the addition of water, oxygen or both. 
     The reciprocating engine  1914  combusts the predetermined mixture of flare gas and air to form syngas. The syngas flows through heat exchangers and into a filter, e.g., a particulate filter. 
     After passing through the filter, the syngas flows to a guard bed reactor assembly, having two guard bed reactors. After leaving the guard bed reactor, the syngas flows to a deoxo reactor. The deoxo reactor removes excess oxygen from the reprocessed gas (e.g., syngas). 
     The system has a cooling system, which uses a cooling fluid, e.g., cooling water, that is flow through cooling lines. 
     After leaving the deoxo reactor, the syngas flows to heat exchanger. The reprocessed gas (e.g., syngas) then flows from the heat exchanger to a water removal unit, e.g., a water knockout drum, demister, dryer, membrane, cyclone, desiccant or similar, where water is removed from the syngas. In general, the syngas upon leaving unit the water removal unit should have less than about 5% water by weight, less than about 2%, less than about 1% and less than about 0.1% water. 
     After leaving the water removal unit, the now dry syngas is in the synthesis stage  1902 . In stage  1902  the now dry syngas flows to an assembly that provides for the controlled addition of hydrogen from line into the now dry syngas. In this manner the ratio of the syngas components can be adjusted and controlled to a predetermined ratio. The hydrogen is provided from hydrogen separate  1939 . The ratio adjusted dry syngas leaves the assembly and flows to compressor  1932 . Compressor  1932  compresses the syngas to an optimum pressure as taught and disclosed in this specification, for use the synthesis unit  1933 , which is a two-stage unit with a first reactor unit  1933   a  and a second reactor unit  1933   b . Synthesis unit  1933  also has heat exchanger  1920   e.    
     The synthesis unit  1933  converts the ratio adjusted dry syngas into a value-added product, e.g., methanol. The methanol flows into to heat exchanger and then to a collection unit  1940 . The collection unit  1940  collects the methanol and flows it through a line for sale, holding, or further processing. 
     The collection unit  1940  also has a line that flows gas separated from the methanol to tee-connector, where it is sent to hydrogen separate  1939 , to a recycle loop or both. Recycle loop has a compressor and a valve to feed the methanol back into the synthesis unit  1933 . 
     Stage  1902  has a line  1983  for taking water depleted methanol from unit  1933   b  and sending it through heat exchanger  1920   d . The stage  1902  has a line  1987  from unit  1833   b  that removes water rich product. 
     The system  1900  is for the gas-to-liquids process with reactive separation of byproducts. The process uses a two-stage methanol synthesis reactor with reactive separation in the second stage (Rxtr  2 )  1933   b  only. The first stage (Rxtr  1 )  1833   a  is generally far from equilibrium and does not warrant reactive separation. The example shown in this figure is membrane separation with a gaseous sweep. Water (a byproduct of CO 2  hydrogenation to methanol) is selectively removed from the reactor  1833   b  (via line  1987 ) in situ resulting in a water-depleted gaseous stream containing primarily unreacted syngas and a water-rich sweep gas. In this embodiment a primary recycle loop is not use because of the improved single-pass conversion. Further, in this embodiment, regeneration of the sweep stream (e.g., air in this embodiment) is not performed. The membrane reactor could use a polymeric or ceramic membrane material that is perm-selective to water and a sweep gas (e.g., air) on the permeate side of the membrane. Removing the water shifts the equilibrium towards the products. The reverse water-gas shift reaction converts CO 2  to CO, and so this approach also helps convert CO 2  to more reactive CO. As such, this approach is especially attractive for CO 2 -rich syngas streams such as those produced from partial oxidation. Methanol is condensed out of the gas phase in a downstream separation step and combined with the methanol product stream. 
     Example 23 
     An embodiment of a methanol synthesis unit, for use with any of the present systems including the systems of the Examples, is a quench style methanol reactor. A cool reactor feed gas is injected between catalyst beds to quench the gas exiting each catalyst bed and control the feed temperature of reactants to each catalyst bed. The following parameters set the basis for the sizing of the Methanol Reactor.
         4 catalyst beds.   225° C. inlet temperature to each bed, consistent with expected catalyst supplier end of life feed temperature. This sets the required quench gas flowrates.   Average gas velocity within the reactor&lt;=1 ft/s. This parameter sets the minimum required reactor diameter.   Average gas residence time per catalyst bed&gt;=2.5 seconds. This parameter sets the minimum average catalyst bed depth, which in turns sets the minimum tangent-to-tangent length of the reactor.       

     A parameter for methanol synthesis is the ratio of hydrogen to carbon oxides in the feed to the methanol reactor. The gas stoichiometry is defined using the S ratio as follows. 
     
       
         
           
             S 
             = 
             
               
                 
                   H 
                   ⁢ 
                   2 
                 
                 - 
                 
                   CO 
                   ⁢ 
                   2 
                 
               
               
                 CO 
                 + 
                 
                   CO 
                   ⁢ 
                   2 
                 
               
             
           
         
       
     
     The preferred S ratio is between 2-2.3. Typical steam methane reformers produce a syngas with an S ratio of approximately 3. However, the engine reformers of the present systems can produce a syngas with an S ratio closer to 1. The target S ratio, for the embodiment of this Example, is 2.1. To achieve this S ratio at the feed to the methanol reactor it is required that a portion of the recycled loop gas is sent through a hydrogen purification step. Therefore, the target S ratio defines the sizing basis for the Hydrogen Recovery Package. 
     Example 23 
     An embodiment of a control system for the operation and monitoring of the present systems and processes, including the Examples. This control system also has components for calculation, obtaining and storing data and information about the operation of the system and process, e.g. process information and data. This process data and information can, among other things, include: mass balance data and information (e.g., kg of flare gas into system, kg of methanel produced, kg of exhaust produced, etc.), carbon capture data and information, CO 2 e related data and information, and combinations and variations thereof and well as other types of data and information. This data and information among other things can be used to validate or obtain carbon credits on for example a carbon exchange, or to meet environmental regulatory reporting or monitoring requirements. 
     A control has a control panel located on site at the system (e.g., on a skid, on one or both stages in a modular system). The control panel will house control equipment such as controllers, marshalling panels, power supplies, network switches, etc. The control panel will include the basic process control and the safety shutdown system. Preferably all information will be available for monitoring and control from the control panel. 
     The process information and data on the on-site control panel will preferably be available for remote monitoring and limited remote control from a remote-control room via cellular (4G/5G) network, satellite, or other hardwired or wireless communication mode. 
     Preferably, the level of automation provided by the control panel shall be such that under normal plant operating conditions, manual intervention of the operators is minimized. Manual intervention can be required for abnormal events and conditions that occur during module start up and shutdown. Preferably the control panel shall always be active and provide full control, monitoring, and safeguarding of the module at all times. 
     Preferably, the control systems shall be designed to be fail-safe such that upon the loss of power, instrument air supply, or control signal to/from instrument device shall cause the plant to move to a predetermined safe operating state. 
     Preferably, the control systems shall support a level of redundancy and fault tolerance such that the failure of any single component of the system shall have no significant adverse effect on the processes being controlled. 
     Preferably, the control panel serves as the Integrated Control &amp; Safety System (ICSS) and thus provides basic process control and basic safety functions for the system, and preferably includes one, more than one and all of the following functions:
         Basic Process Control System (BPCS),   Safety Instrumented System (SIS), if determined required in future phases of the project,   Corresponding Human-Machine Interfaces (HMI) displays,   Communications systems,   Mechanical vendor system interfaces (such as Anti-Surge Control systems (ASC)).       

     Preferably, all field instruments shall be “smart” type device in which, for example, the HART protocol is available for instrument diagnostic. Instrument designs and selections shall follow industrial standards such as ISA (International Society of Automation) and PIP (Process Industry Practices). IEC61508 certified instruments shall be used for SIFs that are SIL 1 or above. 
     Example 24 
     Turning to  FIG.  24    there is provided a control and communication system network  2300  for the use with the present systems and processes, including the Examples. Network  2300  includes and is control communication with a flare gas to syngas to methanol system  2301 , generally of the type disclosed and taught in the specification, including the Examples. 
     The system  2300  has a local, e.g., on-site control system  2320 . The components of the on-site control system  2320  can be in a box or housing located on or attached to the system  2301 . The components of system  2320  may be located in separate housings and enclosures or in a single enclosure. The system  2320  has a controller  2321 , having a processor and memory, a storage device  2322 , a HMI (human machine interface)  2323 , and an input/output (I/O)  2324 , and a communication module  2325 . 
     The system  2300  has numerous on-site communication pathways, e.g.,  2341  that make up local, or on-site sub-network  2340 . The Sub-network  2340  can also communicate with other sub-networks via pathway  2342 . These on-site communication pathways. e.g.  2341 , transmit communications, including control communication, data and information, to and from one, more than one, and preferably all the devices and components of the system  2301 . Additionally, these on-site-pathways, e.g.,  2341 , transmit communications, including control communications, data and information, to and from one, more than one, and preferably all of the sensors and monitoring devices and instruments in system  2301 . In this manner on-site sub-network  2340  can send and receive control communications, as well as, sensor data and information from system  2301  to the control system  2320 . In this manner the on-site control system  2320  is in control communications with the flare gas to syngas to methanol system  2301 . In this manner the on-site control system  2320  can operation and control the system  2301 , and receive data and information about the processes and operations of the system  2301 . The on-site control system  2320  can be, for example, configured along the lines of the control system in Example 23. 
     The on-site control system is in control communication with a remote-control system  2350 . In this manner, the remote-control system  2350  can configure, control, change, monitor the on-site control system  2320 , the system  2300 , and both. The remote-control system has The system  2320  has a controller, having a processor and memory, a storage device, a HMI, and a communication module. 
     The remote-control system  2350 , the control system  2320  and both are configured to monitor, calculate, record, store and transmit, information about any and all aspects of the operation of system  2301 , e.g., flow rates, mass flow, density, temperature, settings of equipment, exhaust conditions, etc. Among of things, these operation aspects would include: mass balance data and information (e.g., kg of flare gas into system, kg of methanal produced, kg of exhaust produced, etc.). This information and data can be and processed to determine and record, preferably real time, GWP information and data, carbon capture information and data, CO2e information and data, for the operation of system  2301 , and preferably for the real time operation of system  2301 . This data and information among other things can be used to validate or obtain carbon credits on for example a carbon exchange, or to meet environmental regulatory reporting or monitoring requirements. Preferably this GWP type information is encrypted using block chain, or some other encryption methodology, to insure its validity. 
     Thus, the control system  2320 , the remote-control system  2350  and both can be in control communication with another entity  2360 . For example, entity  2360  can be a carbon exchange, it can be a government regulatory agency, it can be a trade regulatory agency, or other entities, such as a class room. It should be noted that while the communications pathways between entity  2360  and the control can be two-way communication, these pathways do not send or receive any control communication. In this manner the entity  2360  has no capability to control the system  2301 . Further, the other information about system  2301  can be provided to entity  2360 , as may be needed or required. 
     Example 25 
     Turning to  FIG.  25    there is shown a schematic of the architecture of a control communication network for use with the present systems and processes, including the Examples. 
     Example 26 
     In situations where the flare gas contains H 2 S, is preferably is removed prior to processing the flare gas into syngas. Batch And cyclic process technology can be used to remove the H 2 S, which would include a packed bed with solid adsorbent/scavenger material. Liquid solvents can be used, most commonly an amine like methyl diethanolamine (MDEA) to remove the H 2 S and CO 2  from flare gas streams. A typical configuration is to flow the amine solution through an absorption tower countercurrent to the flare gas. The amine stays in a closed loop and is regenerated with heat. 
     Example 27 
     The present systems and processes, including the Examples are operated to convert flare gas into methanol having a purity of about 80% and greater, at least about 85%, at least about 90%, at least about 93%, at least 95%, from about 80% to 95%, and from about 85% to about 90%. 
     Example 28 
     A system and process to convert otherwise uneconomic hydrocarbon-based fuel such as flare gas to value-added, easily transported products (such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) using an autonomous, modular system comprising the following elements: (1) a fuel conditioning system to meet requirements of downstream components; (2) an air-breathing gas turbine, modified to operate a rich, partial-oxidation reformer, to produce a syngas mixture with a H 2 /CO ratio suitable for synthesis of liquids; (3) a combination of integrated heat exchangers, compression system components, and heat exchangers to prepare the syngas for the downstream synthesis reactors; and (4) a downstream synthesis reactor system to produce useful liquid hydrocarbon products. 
     Example 29 
     A system and process to convert otherwise uneconomic hydrocarbon-based fuel such as flare gas to value-added, easily transported products (such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) using an autonomous, modular system comprising the following elements: (1) a fuel conditioning system to meet requirements of downstream components; (2) an air-breathing gas turbine, modified to operate a rich, partial-oxidation reformer, to produce a syngas mixture with a H2/CO ratio suitable for synthesis of liquids; (3) a combination of integrated heat exchangers, compression system components, and heat exchangers to prepare the syngas for the downstream synthesis reactors; (4) a downstream synthesis reactor system to produce useful liquid hydrocarbon products; and, (5) a hydrogen recycle loop to improve overall system process performance. 
     Example 30 
     The systems and process of Examples 28 and 29, can also have one, or more, or all of the following additional features: (6) optional substantially oxygen-free gas recirculation loop to cool and protect downstream components of the combustor, such as seals, bearings, and secondary cavities; (7) optional O 2  enrichment of the inlet stream to the gas turbine via membrane separation or partial air separation unit; (8) a recuperator heat exchanger (from (3)) and a turbo expander to recover energy from the high pressure exhaust gas from the downstream synthesis reactor; (9) integration of a closed-loop operating system with custom instrumentation; (10) a cloud-based remote monitoring system, including AI-trained anomaly detection for dynamic preventative maintenance and operations control; (11) optional offtake pathways to utilize byproducts, such as nitrogen, water, and CO 2  for reinjection, well recompletions, or other purposes; (12) optional water (or steam) injection into the rich combustor to improve H 2 /CO ratio and reduce carbon build-up on surfaces within the combustor and turbine. 
     Example 31 
     Embodiments of these inventions, provide modular systems that can be positioned near sources of uneconomical hydrocarbons (e.g., flare gas), syngas, product gas, and reprocessed gas to convert these materials into higher value products. These inventions will be used to take uneconomic hydrocarbon-based fuels at a well-head (e.g, flare gas) and remote locations that are primarily gaseous hydrocarbons and convert them to a more valuable easily condensable or liquid compounds, such as methanol. One source of source fuel could be associated gas or flare gas, which is produced as a byproduct at oil wells. Another source could be biogas from landfill or anaerobic digesters. 
     A small-scale plant, targeting 3,000,000 scfd (standard cubic feet per day) of inlet gas. The size of such a plant could vary from 300,000 scfd to 15,000,000 scfd. The plant is incorporated into one or more modular, interconnected skids or containers that are built at a central fabricator shop location and then installed at a field location. A small number of modules comprise the system and when connected at site they form an integrated system. The modular nature of the assembly enables application to remote locations under a range of inlet gas feed volumes, with a minimum of field labor. The modular nature further improves flexibility to deploy or redeploy these assets, reduces initial capital outlay and project financial risks, allows matching of the process throughput to the flare gas supply, and reduces time-to-market by allowing module fabrication and site preparation to occur in parallel. 
     Example 32 
     A modular unit having a collection of unit-scale engine reformers and unit-scale MeOH synthesis systems, with no common BOP (balance of plant). 
     Example 33 
     A modular unit having a collection of unit-scale engine reformers and unit-scale MeOH synthesis systems, with common BOP. 
     Example 34 
     A modular unit having a collection of unit-scale engine reformers that supply a common, unitary MeOH synthesis system. 
     Example 35 
     A modular unit having 900 scfd (standard cubic feet per day) of feed gas, (e.g., flare gas). 
     Example 36 
     A modular unit having 75,000 scfd of feed gas (e.g., flare gas), scale right-sized for a single engine reformer. 
     Example 37 
     A modular reformer stage having 2 or more, 3 or more, at least 5, at least 6, or 2 to 10 reformers. The reformers can be one or more of a gas turbine engine, a combustion box, an internal combustion engine, an otto cycle reciprocating engine, a diesel cycle reciprocating engine and combinations of these. This modular reformer stage can be skid mounted, truck mounted, etc. 
     Example 38 
     In an embodiment of the present inventions have a rich-burn reciprocating engine and a synthesis reactor. Unlike a traditional reciprocating engine, the engine runs at rich conditions, up to equivalence ratio of 2.5, so the fuel experiences rich partial oxidation (POX). Additional components include the fuel conditioning system, heat exchangers, compressors, and turbines. The fuel conditioning system separates liquids from gases in the feed stream and removes compounds that can damage the reciprocating engine or synthesis reactor. The heat exchangers and compressors take the syngas mixture at the exit of the reciprocating engine and adjust the temperature and pressure to deliver the target conditions for the synthesis reactor. Within the synthesis sub-system is an optional H 2  recycle loop. The gas at the exit of the synthesis reactor is heated in a recuperating (e.g., counter-flow) heat exchanger to an elevated temperature and then expanded to ambient conditions. 
     Example 39 
     In this embodiment it is preferrable that in configuring and operating a syngas engine for achieving preferred engine operation under conditions sufficiently rich to produce a syngas with the desired H 2 /CO ratio near 2. Even if acceptable operability is achieved with one fixed fuel composition, changes to the fuel composition, which will arise during operation in the field, for example at an oil well, will change the combustion properties and lead to poor engine operation. Thus, the engine has sensors and control systems that detect changes in the combustion properties of the fuel and adapt its parameters to achieve desired engine operation. An engine with a combination of sensing and variable compression ratio can overcome these challenges. A variable compression ratio engine adjusts the compression ratio of an internal combustion engine while the engine is in operation. Variable compression engines allow the volume above the piston at top dead center to be changed. 
     Example 40 
     An embodiment of a variable compression ratio engine reformer is through the use of variable valve timing, such as cam phasers. Twin Independent Variable Camshaft Timing (Ti-VCT) is the name given by Ford to engines with the ability to advance or retard the timing of both the intake and exhaust camshafts independently, unlike the original versions of VCT, which only operated on a single camshaft. This allows for improved power and torque, particularly at lower engine RPM, as well as improved fuel economy and reduced emissions 
     A “cam phaser” is an adjustable camshaft sprocket that can be turned by means of a computer-controlled servo. Rather than operating with a fixed amount of advance or retard, the computer can advance or retard the cam or cams continuously. An embodiment of this application is to enhance drivability at light load and low engine speed (by reducing overlap of the intake and exhaust events to minimize residual dilution), and generate more power at high engine speed (by retarding the intake valve event to increase volumetric efficiency). 
     For rich combustion operation to produce syngas, when the fuel composition is richer (greater fraction of low-octane constituents) the purpose of retarding the timing of the intake valve event is to retard valve closing sufficiently to shorten the effective compression stroke and thus reduce the effective compression ratio. 
     When the fuel composition is leaner (greater fraction of high-octane constituents) the purpose of advancing the timing of the intake valves is to advance intake valve opening sufficiently to extend the effective compression strokes and thus increase the effective compression ratio. Operating at a higher effective compression ratio increases pressure and temperature in the combustion chamber and thus extends the rich combustion limit with lean gas. 
     Example 41 
     An VVT/cam (variable valve timing/cam) phaser engine that allows, among other things, the compression ratio to be varied according the properties of the incoming fuel for rich combustion to produce syngas. 
     Example 42 
     A VVT/cam phaser engine with sensors to detect the in-cylinder combustion behavior under rich conditions and automatically adjust the compression. 
     This approach can be applied to a two-stroke or four-stroke reciprocating engine. 
     Example 43 
     A system and process to convert otherwise uneconomic hydrocarbon-based fuel such as flare gas to value-added, easily transported products (such as methanol, ethanol, ammonia, dimethyl-ether, F-T liquids, and other fuels or chemicals) using an autonomous, modular system comprising the following elements: (1) a fuel conditioning system to meet requirements of downstream components; (2) an air-breathing gas engine, modified to operate a rich, partial-oxidation reformer, to produce a syngas mixture with a H2/CO ratio suitable for synthesis of liquids; (3) a combination of integrated heat exchangers, compression system components, and heat exchangers to prepare the syngas for the downstream synthesis reactors; (4) a downstream synthesis reactor system to produce useful liquid hydrocarbon products; and, (5) a hydrogen recycle loop to improve overall system process performance. 
     Example 44 
     A embodiment of a variable compression ratio engine is through an opposed-piston free-piston linear internal combustion engine. A free-piston engine is linear, ‘crankless’ internal combustion engine. The power delivered by the engine is not delivered via a crankshaft, but instead through exhaust gases driving a turbine or a linear motor/generator directly coupled to the pistons to produce electric power. 
     Example 45 
     A rich-burn reciprocating engine and a synthesis reactor. Unlike a traditional reciprocating engine, the engine runs at fuel-rich conditions, up to equivalence ratio of 2.5 so the fuel experiences rich partial oxidation (POX). Additional components include the fuel conditioning system, heat exchangers, compressors, and synthesis reactor. The fuel conditioning system separates liquids from gases in the feed stream and removes compounds that can damage the reciprocating engine or synthesis reactor. The heat exchangers and compressors take the syngas mixture at the exit of the reciprocating engine and adjust the temperature and pressure to deliver the target conditions for the synthesis reactor. Within the synthesis sub-system is an H 2  recycle loop or CO 2  scrubber for syngas ratio adjustment. Optionally, the gas at the exit of the synthesis processes is heated in a recuperating (e.g., counter-flow) heat exchanger to an elevated temperature and then expanded to ambient pressure, thus providing shaft work for compression of the synthesis gas. 
     Example 46 
     The embodiments of the systems of the above Examples are operated in a carbon neutral-to-negative manner, producing and releasing less than or equal to zero CO 2 e from a lifecycle perspective. 
     Example 47 
     One or more of the systems of the above Examples are placed at an oil field having a large number of oil wells. The flare gas from these oil wells is captured at the wellhead of each of the oil wells and flows in a piping and manifold system to the units where it is processed into an end product, such as methanol. 
     Example 48 
     One or more of the systems of the above Examples are placed at a livestock production farm, handling or production facility. The methane-rich biogas from anaerobic digestion of the livestock manure is collected and processed by the systems into an end product, such as methanol. 
     Example 49 
     One or more of the systems of the above Examples are placed at municipal waste-water treatment facilities where anaerobic digesters produce fuel for the syngas unit, and methanol produced by the process is consumed by the denitrification process as part of the treatment process. This approach results in a local and circular process for waste water treatment. 
     Example 50 
     In an oil filed have several oil, gas or both wells, (e.g., 5 wells, 10 wells, 20 wells or more) piping and distribution headers are used to collect and transfer the flare gas from each of the wells, to one or of the present waste gas, e.g., flare gas, processing units, such as one or more of systems of the above Examples. 
     Example 51 
     Hydrocarbon production activity, e.g., exploration, drilling, workover and completion of a hydrocarbon well, e.g., an oil or gas well, can including the planning for, and use of, the present systems and methods, including the systems of the above Examples. In this manner the overall effect of the hydrocarbon production activity on global warming, e.g., GWP, can be mitigated or reduced. Thus, the use of the present systems and methods, including the Examples, can be included in the planning hydrocarbon activity, as well as, in the obtaining of regulatory approval for such activity. 
     Example 52 
     The present systems and methods, including the systems and methods of the Examples, where the source of the flare gas is one, or more than one, of a hydrocarbon well, an oil well, an unconventional oil well, a conventional oil well, an off-shore well, or an on-shore well. 
     Example 53 
     The present systems and methods, including the systems and methods of the Examples, where the source of the flare gas is selected from the group consisting of petrochemical processing, refining, landfills, waste water treatment, and livestock. 
     Example 54 
     The embodiments of the systems of the above Examples are operated in an energy positive manner, producing more power, in the form of electricity, than is required to operate the system. 
     Headings and Embodiments 
     It should be understood that the use of headings in this specification is for the purpose of clarity, reference, and is not limiting in any way. Thus, the processes compositions, and disclosures described under a heading should be read in context with the entirely of this specification, including the various Examples. The use of headings in this specification should not limit the scope of protection afforded the present inventions. 
     It is noted that there is no requirement to provide or address the theory underlying the novel and groundbreaking production rates, performance or other beneficial features and properties that are the subject of, or associated with, embodiments of the present inventions. Nevertheless, various theories are provided in this specification to further advance the art in this important area, and in particular in the important area of hydrocarbon exploration and production. These theories put forth in this specification, and unless expressly stated otherwise, in no way limit, restrict or narrow the scope of protection to be afforded the claimed inventions. These theories many not be required or practiced to utilize the present inventions. It is further understood that the present inventions may lead to new, and heretofore unknown theories to explain the conductivities, fractures, drainages, resource production, and function-features of embodiments of the methods, articles, materials, devices and system of the present inventions; and such later developed theories shall not limit the scope of protection afforded the present inventions. 
     The various embodiments of devices, systems, activities, methods and operations set forth in this specification may be used with, in or by, various processes, industries and operations, in addition to those embodiments of the Figures and disclosed in this specification. The various embodiments of devices, systems, methods, activities, and operations set forth in this specification may be used with: other processes industries and operations that may be developed in the future: with existing processes industries and operations, which may be modified, in-part, based on the teachings of this specification; and with other types of gas recovery systems and methods. Further, the various embodiments of devices, systems, activities, methods and operations set forth in this specification may be used with each other in different and various combinations. Thus, for example, the configurations provided in the various embodiments of this specification may be used with each other. For example, the components of an embodiment having A, A′ and B and the components of an embodiment having A″, C and D can be used with each other in various combination, e.g., A, C, D, and A. A″ C and D, etc., in accordance with the teaching of this specification. Thus, the scope of protection afforded the present inventions should not be limited to a particular embodiment, configuration or arrangement that is set forth in a particular embodiment, example, or in an embodiment in a particular Figure. 
     The invention may be embodied in other forms than those specifically disclosed herein without departing from its spirit or essential characteristics. The described embodiments are to be considered in all respects only as illustrative and not restrictive.