Patent Publication Number: US-2022212158-A1

Title: Systems For Producing Chemicals And Fuels Having An Optimized Carbon Footprint

Description:
CLAIM OF PRIORITY 
     This disclosure claims priority to U.S. Provisional Application No. 62/847,986, filed May 15, 2019, the disclosure of which is incorporated by reference in its entirety. 
    
    
     STATEMENT OF GOVERNMENT-SPONSORED RESEARCH 
     This invention was made with government support under grant number DE-SC0019791, awarded by the United States Department of Energy, Small Business Innovation Research. The government has certain rights in the invention. 
    
    
     FIELD OF INVENTION 
     The present invention relates generally to the creation of chemical producing systems which allow for an optimized carbon footprint. Example systems for the production of synthesis gas (syngas), hydrogen, hydrocarbon fuels, ammonia, and urea are presented. Reducing the carbon footprint of chemicals such as these is of vital importance to reducing the environmental impact of industries such as transportation and agriculture. In many of the embodiments a secondary product is produced, the sale of this secondary product may make the primary low-carbon footprint chemical more economical. In many cases the secondary product is carbon, methods of sequestering this carbon via enhanced oil and gas recovery are presented. 
     BACKGROUND OF THE INVENTION 
     Chemical and fuel production and use are major sources of greenhouse gases in the earth&#39;s atmosphere and are contributing to climate change. Additionally, fossil-fuel sources are becoming scarcer and more difficult to recover. In order to reduce the emission of greenhouse gases, slow climate change, and maintain lifestyle standards in transportation and agriculture, new greener systems for chemical production are of vital importance. 
     The synthesis of many fuels and chemicals starts with the formation of hydrogen or syngas (a mixture of hydrogen and carbon monoxide). The production of these gases is currently dominated by steam-methane reforming, where water (H2O) and methane (CH4) are converted with catalytic assistance into hydrogen (H2) and carbon monoxide (CO) where there are about three hydrogen molecules for every carbon monoxide molecule (H2O+CH4→CO+3*H2). This reaction is highly endothermic, requiring 225.4 kJ/mol from room temperature, the thermal energy required is typically provided by combusting natural gas (primarily CH4), which produces carbon dioxide. 
     For chemical processes requiring hydrogen, the carbon monoxide molecule is generally “shifted” to additional hydrogen using the water-gas shift reaction. Water is added to the carbon monoxide-rich gas and carbon dioxide and hydrogen gas form (CO+H2O→CO2+H2). This reaction is slightly exothermic releasing 41.0 kJ/mol. Thus, the production of hydrogen gas produces additional carbon dioxide. 
     Green alternatives for producing hydrogen exist, such as electrolysis. However, since all of the energy for electrolysis must be provided by electricity the operational costs may be prohibitive for such systems alone. 
     SUMMARY OF THE INVENTION 
     Plasma-based reforming systems may provide a viable alternative to the standard steam-methane reforming methods which produce greenhouse gases, and electrolysis only methods which uses only electrical energy sources. 
     Plasma-based reforming systems can be used to do the aforementioned steam reforming where water and methane are used to make syngas, however instead of combusting methane or other hydrocarbons to provide the energy to drive the reaction the energy is provided by an electrically driven plasma. If the electricity source does not produce greenhouse gases, the carbon footprint of plasma-based syngas production is reduced. 
     Plasma-based reforming can also be applied to other reforming reactions, such as, dry reforming and pyrolysis. In dry reforming carbon dioxide (CO2) and methane (CH4) are converted into hydrogen (H2) and carbon monoxide (CO) where there are about one hydrogen molecules for every carbon monoxide molecule (CO2+CH4→2*C0+2*H2). Like steam reforming, this reaction is highly endothermic, requiring 260.5 kJ/mol from room temperature. To consume additional CO2 reverse water-gas shift reactions (CO2+H2 CO+H2O) can be encourage by running CO2-rich, ideally in this case three molecules of CO2 could be reformed with every CH4 molecule (CH4+3*CO2 4*CO+2*H2O). 
     In methane pyrolysis the methane (CH4) is converted into hydrogen (H2) and carbon (C) where there are about two hydrogen molecules for every carbon atom (CH4→2*H2+C). Methane pyrolysis is also endothermic requiring 74.9 kJ/mol from room temperature. Larger hydrocarbon materials can also be pyrolyzed, the ratio of hydrogen molecules to carbon atoms trend closer to one the longer the hydrocarbon molecule is. 
     The energy to drive plasma-based reforming systems is electrical energy. When the electricity is generated using means that do not emit greenhouse gases, the production of hydrogen and syngas can have greatly reduced carbon footprints. 
     Devices and methods for creating plasma-based reforming and pyrolyzing units have previously been disclosed in PCT/US2020/019689, which is incorporated by reference in its entirety. In this disclosure, systems for chemical production that have an optimized carbon footprint by incorporating such plasma-based reforming and/or pyrolyzing units are disclosed. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       To better illustrate the invention and to aid in a more thorough description which provides other advantages and objectives of the invention the following drawings are referenced. It is noted that these embodiments are specific examples of the invention and not to be understood as limiting cases for the scope of this invention. The drawings are as follows: 
         FIG. 1 : Block diagram of a system for chemical production according to the prior art. 
         FIG. 2 : Block diagram of a system for chemical production with an optimized carbon footprint according to the first embodiment. 
         FIG. 3 : Block diagram of a system for the chemical production of synthetic hydrocarbon products with an optimized carbon footprint according to the first embodiment. 
         FIG. 4 : Block diagram of a system for chemical production with an optimized carbon footprint according to the second embodiment. 
         FIG. 5 : Block diagram of a system for the chemical production of synthetic hydrocarbon products and oxygen with an optimized carbon footprint according to the second embodiment. 
         FIG. 6 : Block diagram of a system for the chemical production of synthetic hydrocarbon products and carbon with an optimized carbon footprint according to the second embodiment. 
         FIG. 7 : Block diagram of a system for the chemical production of ammonia and carbon with an optimized carbon footprint according to the second embodiment. 
         FIG. 8 : Block diagram of a system for chemical production with an optimized carbon footprint according to the third embodiment. 
         FIG. 9 : Block diagram of a system for the chemical production of hydrogen and carbon with an optimized carbon footprint according to the third embodiment. 
         FIG. 10 : Block diagram of a system for chemical production with an optimized carbon footprint according to the fourth embodiment. 
         FIG. 11 : Block diagram of a system for the chemical production of synthetic hydrocarbon products and carbon with an optimized carbon footprint according to the fourth embodiment. 
         FIG. 12 : Block diagram of a system for the chemical production of ammonia and carbon with an optimized carbon footprint according to the fourth embodiment. 
         FIG. 13 : Block diagram of a system for chemical production with an optimized carbon footprint according to the fifth embodiment. 
         FIG. 14 : Block diagram of a system for the chemical production of ammonia, carbon, carbon dioxide, and electricity with an optimized carbon footprint according to the fifth embodiment. 
         FIG. 15 : Block diagram of a first example enhanced oil and gas recovery system using carbon product. 
         FIG. 16 : Block diagram of a second example enhanced oil and gas recovery system using carbon product. 
         FIG. 17 : Block diagram of a third example enhanced oil and gas recovery system using carbon product. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION: 
       FIG. 1  gives a block diagram of a system for chemical production according to the prior art  1 . Reactants  2  are fed into a steam-methane reformer  3 . For steam-methane reforming the reactants  2  comprise water in vapor form and methane, generally from a methane-rich source such as natural gas. Methane and air are provided as fuel  4  to drive the reforming reaction, the fuel  4  is separately fed into the steam-methane reformer  3 . The fuel  4  generally comes from a methane-rich source, such as natural gas. The methane and air provided as a fuel  4  to drive the reforming reaction is combusted in the steam-methane reformer  3 , wherein the combustion produces carbon dioxide  5 . The heat generated by combustion drives the reforming of the reactants  2  into an initial product  6  of hydrogen and carbon monoxide. 
     The initial product  6  flows to a shift reactor  7  where the ratio of hydrogen to carbon monoxide is altered. A shift feedstock  8  is also fed into the shift reactor  7  and a shifted product  9  is formed. If the desired shifted product  9  is hydrogen, the shift feedstock  8  comprises water and the water-gas shift would occur to form additional hydrogen (CO+H2O CO2+H2). If the desired shifted product  9  is syngas having a ratio of hydrogen to carbon monoxide less than three the shift feedstock  8  would comprise carbon dioxide and the reverse water-gas shift would occur to form additional carbon monoxide (CO2+H2 CO+H2O). 
     The shifted product  9  flows out of the shift reactor  7  into a gas conditioner  10 . Depending on what molecules need to be removed from the shifted product  9  the gas conditioner  10  may take a variety of forms. To remove water from the shifted product  9  the gas conditioner  10  may contain a vapor-liquid separator. To remove carbon dioxide from the shifted product  9  the gas conditioner  10  may contain a carbon dioxide removal system such as amine scrubbing. Other parts of the gas conditioner  10  may include compression, cooling, heating, targeted molecule removal, molecule addition, and additional syngas ratio modification. Conditioned gas  11 , such as hydrogen or syngas with a specified hydrogen to carbon monoxide ratio, exit the gas conditioner  10  and enter the processing unit  12 . The processing unit uses the conditioned gas  11  to produce a final product  13 . The processing unit  12  may be as simple as bottling or depositing the conditioned gas  11  into a pipeline. The processing unit  12  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     As discussed above, replacing steam-methane reformers with plasma-based reformers and pyrolysis units can lead to systems for chemical production that have a reduced carbon footprint. Additionally, the wider range of feedstocks which can be processed in plasma-based reformers, as compared to steam-methane reformers, yield new system configurations for producing chemical products and co-products. 
     Embodiment 1 
       FIG. 2  gives a block diagram of a system for chemical production with an optimized carbon footprint according to the first embodiment  101 . First reactants  102  are fed into a first reformer unit  103  along with a first portion of electricity  104 . The energy in the first portion of electricity  104  is used to drive the reformation of the first reactants  102  into a first initial product  105 . The first reformer unit  103  is configured to use the first portion of electricity  104  to molecularly alter the composition of the first reactants  102 . 
     The first initial product  105  may flow into an optional first initial product conditioner  106 . In the optional first initial product conditioner  106  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  107  may be included to reinject a portion of the gases back into the first reformer unit  103 . Gases not recycled to the first reformer unit  103  exit the optional first initial product conditioner  106  as a first conditioned initial product  108 . If an optional first initial product conditioner  106  is not included the first initial product  105  and first conditioned initial product  108  are equivalent. 
     Second reactants  109  are fed into a second reformer unit  110  along with a second portion of electricity  111 . The energy in the second portion of electricity  111  is used to drive the reformation of the second reactants  109  into a second initial product  112 . The second reformer unit  110  may be configured to use the second portion of electricity  111  to molecularly alter the composition of the second reactants  109 . 
     The second initial product  112  may flow into an optional second initial product conditioner  113 . In the optional second initial product conditioner  113  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional second recycling line  114  may be included to reinject a portion of the gases back into the second reformer unit  110 . Gases not recycled to the second reformer unit  110  exit the optional second initial product conditioner  113  as a second conditioned initial product  115 . If an optional second initial product conditioner  113  is not included the second initial product  112  and second conditioned initial product  115  are equivalent. 
     The first conditioned initial product  108  and the second conditioned initial product  115  flow into a conditioner  116 . The conditioner  116  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  116  mixes the first conditioned initial product  108  and the second conditioned initial product  115 . The conditioner  116  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  116  depends partly on if the optional first initial product conditioner  106  and the optional second initial product conditioner  113  were included. Although not shown a recycling line could also be included flowing from the conditioner  116  to the first reformer unit  103 , the second reformer unit  110 , or both reformers. A conditioned intermediate product  117  exits the conditioner  116 . 
     The conditioned intermediate product  117  flows to a processing unit  118  where a final chemical product  119  is formed. The processing unit  118  may be as simple as bottling or depositing the conditioned intermediate product  117  into a pipeline. The processing unit  118  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     Example of the First Embodiment: a System for the Chemical Production of Synthetic Hydrocarbon Products with an Optimized Carbon Footprint 
       FIG. 3  gives a block diagram of a system for the chemical production of synthetic hydrocarbon products with an optimized carbon footprint according to the first embodiment  121 . First reactants  122 , which are methane and water, are fed into a first reformer unit  123  along with a first portion of electricity  124 . The energy in the first portion of electricity  124  is used to drive the reformation of the methane and water into a hydrogen-rich syngas initial product  125 . The hydrogen-rich syngas initial product  125  has a hydrogen to carbon monoxide ratio of greater than 2.5. 
     The hydrogen-rich syngas initial product  125  may flow into an optional hydrogen-rich syngas initial product conditioner  126 . In the optional hydrogen-rich syngas initial product conditioner  126  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  127  may be included to reinject a portion of the gases back into the first reformer unit  123 . Gases not recycled to the first reformer unit  123  exit the optional hydrogen-rich syngas initial product conditioner  126  as a conditioned hydrogen-rich syngas initial product  128 . If the optional hydrogen-rich syngas initial product conditioner  126  is not included the hydrogen-rich syngas initial product  125  and the conditioned hydrogen-rich syngas initial product  128  are equivalent. 
     Second reactants  129 , which are methane and carbon dioxide, are fed into a second reformer unit  130  along with a second portion of electricity  131 . The energy in the second portion of electricity  131  is used to drive the reformation of the methane and carbon dioxide into a hydrogen-lean syngas initial product  132 . The hydrogen-lean syngas initial product  132  has a hydrogen to carbon monoxide ratio of 0 to 1.5. 
     The hydrogen-lean syngas initial product  132  may flow into an optional hydrogen-lean syngas initial product conditioner  133 . In the optional hydrogen-lean syngas initial product conditioner  133  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional second recycling line  134  may be included to reinject a portion of the gases back into the second reformer unit  130 . Gases not recycled to the second reformer unit  130  exit the optional hydrogen-lean syngas initial product conditioner  133  as a conditioned hydrogen-lean syngas initial product  135 . If the optional hydrogen-lean syngas initial product conditioner  133  is not included the hydrogen-lean syngas initial product  132  and the conditioned hydrogen-lean syngas initial product  135  are equivalent. 
     The conditioned hydrogen-rich syngas initial product  128  and the conditioned hydrogen-lean syngas initial product  135  flow into a conditioner  136 . The conditioner  136  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  136  mixes the conditioned hydrogen-rich syngas initial product  128  and the conditioned hydrogen-lean syngas initial product  135 . The conditioner  136  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  136  depends partly on if the optional hydrogen-rich syngas initial product conditioner  126  and the optional hydrogen-lean syngas initial product conditioner  133  were included. Although not shown a recycling line could also be included flowing from the conditioner  136  to the first reformer unit  123 , the second reformer unit  130 , or both reformers. Conditioned syngas  137  exits the conditioner  136 . 
     The conditioned syngas  137  flows to a Fischer-Tropsch unit  138  where a synthetic hydrocarbon product  139  is formed. Most synthetic hydrocarbon products  139  require a syngas with a hydrogen to carbon monoxide ratio of about 2. By separately controlling the throughput of the first reformer unit  123  and the second reformer unit  130 , syngas with ratios between about 1 and 3, could be produced. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant synthetic hydrocarbon product  139  can be reduced as compared to the state-of-the-art. 
     Preferably the first reformer unit  123  and the second reformer unit  130  comprise plasma-based reformer units, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  123  and the second reformer unit  130  comprise a microwave discharge. The operating pressure of the first reformer unit  123  and the second reformer unit  130  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  123  and the second reformer unit  130  are between 0.95 and 5 atm. 
     Regarding recycling in this example, including an optional first recycling line  127  and/or an optional second recycling line  134  may help prevent solid carbon formation in the first reformer unit  123  and/or the second reformer unit  130 . The optional hydrogen-rich syngas initial product conditioner  126  and the optional hydrogen-lean syngas initial product conditioner  133  may simply comprise a filter to remove any solids and a pump to drive the flows back to the reforming units. Hydrogen-rich gases may prove best for reducing carbon solid formation within the reformer units, as such it is also possible to include an optional recycling line from optional hydrogen-rich syngas initial product conditioner  126  to the second reformer unit  130 . The recycling of hydrocarbon-rich downstream byproducts produced in the Fischer-Tropsch unit  138  to the first reformer unit  123 , second reformer unit  130 , or both reformer units will help to improve efficiency and reduce consumables consumption. 
     The conditioner  136  will likely comprise a compressor as Fischer-Tropsch processes usually require pressures over 10 atm. Depending on the sulfur content of the methane source used in the first reactants  122  and second reactants  129 , the conditioner  136  may also comprise a sulfur removal bed. Further, depending on the requirements of the Fischer-Tropsch unit  138 , slipped water and carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of a synthetic hydrocarbon product  139  has been described above the conditioned syngas  137  could also be used as reduction gas for steel refining, to make methanol, to make alcohols, or to make aldehydes. Each alternative product may require syngas with a different hydrogen to carbon monoxide ratio, the throughput of the first reformer unit  123  and the second reformer unit  130  may be altered to match the ratio needed. 
     Embodiment 2 
       FIG. 4  gives a block diagram of a system for chemical production with an optimized carbon footprint according to the second embodiment  201 . First reactants  202  are fed into a first reformer unit  203  along with a first portion of electricity  204 . The energy in the first portion of electricity  204  is used to drive the reformation of the first reactants  202  into a first initial product  205 . The first reformer unit  203  is configured to use the first portion of electricity  204  to molecularly alter the composition of the first reactants  202 . 
     The first initial product  205  may flow into an optional first initial product conditioner  206 . In the optional first initial product conditioner  206  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  207  may be included to reinject a portion of the gases back into the first reformer unit  203 . Gases not recycled to the first reformer unit  203  exit the optional first initial product conditioner  206  as a first conditioned initial product  208 . If an optional first initial product conditioner  206  is not included the first initial product  205  and first conditioned initial product  208  are equivalent. 
     Second reactants  209  are fed into a second reformer unit  210  along with a second portion of electricity  211 . The energy in the second portion of electricity  211  is used to drive the reformation of the second reactants  209  into a second initial product  212  and a second secondary initial product  213 . The second reformer unit  210  is configured to use the second portion of electricity  211  to molecularly alter the composition of the second reactants  209 . 
     The second initial product  212  may flow into an optional second initial product conditioner  214 . In the optional second initial product conditioner  214  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional second recycling line  215  may be included to reinject a portion of the gases back into the second reformer unit  210 . Gases not recycled to the second reformer unit  210  exit the optional second initial product conditioner  214  as a second conditioned initial product  216 . If an optional second initial product conditioner  214  is not included the second initial product  212  and second conditioned initial product  216  are equivalent. 
     The first conditioned initial product  208  and the second conditioned initial product  216  flow into a conditioner  217 . The conditioner  217  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  217  mixes the first conditioned initial product  208  and the second conditioned initial product  216 . The conditioner  217  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  217  depends partly on if the optional first initial product conditioner  206  and the optional second initial product conditioner  214  were included. Although not shown, a recycling line could also be included flowing from the conditioner  217  to the first reformer unit  203 , the second reformer unit  210 , or both reformers. A conditioned intermediate product  218  exits the conditioner  217 . 
     The conditioned intermediate product  218  flows to a processing unit  219  where a final chemical product  220  is formed. The processing unit  219  may be as simple as bottling or depositing the conditioned intermediate product  218  into a pipeline. The processing unit  219  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, metallic ore reduction and hydrocarbon formation or oil refining. 
     The second secondary initial product  213 , produced in the second reformer unit  210 , is fed to a secondary product processing unit  221  where a secondary final chemical product  222  is formed. If needed, though not shown, an additional conditioning unit could be included to prepare the second secondary initial product  213  for the secondary product processing unit  221 . The secondary product processing unit  221  may be as simple as packing, bottling, or moving the second secondary initial product  213 . The secondary product processing unit  221  may also include further molecule processing steps such as forming carbon dioxide for enhanced oil and gas recovery. The sale of the secondary final chemical product  222  may help offset the costs of the final chemical product  220 , making the price of the final chemical product  220  which has a reduced carbon footprint more competitive with state-of-the-art products that do not have a reduced carbon footprint. 
     Example of the Second Embodiment: a System for the Chemical Production of Synthetic Hydrocarbon Products and Oxygen with an Optimized Carbon Footprint 
       FIG. 5  gives a block diagram of a system for the chemical production of synthetic hydrocarbon products and oxygen with an optimized carbon footprint according to the second embodiment  231 . First reactants  232 , which are methane and carbon dioxide, are fed into a first reformer unit  233  along with a first portion of electricity  234 . The energy in the first portion of electricity  234  is used to drive the reformation of the methane and carbon dioxide into a hydrogen-lean syngas initial product  235 . The hydrogen-lean syngas initial product  235  has a hydrogen to carbon monoxide ratio of 0 to 1.5. 
     The hydrogen-lean syngas initial product  235  may flow into an optional hydrogen-lean syngas initial product conditioner  236 . In the optional hydrogen-lean syngas initial product conditioner  236  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  237  may be included to reinject a portion of the gases back into the first reformer unit  233 . Gases not recycled to the first reformer unit  233  exit the optional hydrogen-lean syngas initial product conditioner  236  as a conditioned hydrogen-lean syngas initial product  238 . If the optional hydrogen-lean syngas initial product conditioner  236  is not included the hydrogen-lean syngas initial product  235  and the conditioned hydrogen-lean syngas initial product  238  are equivalent. 
     Water  239  is fed into an electrolysis unit  240  along with a second portion of electricity  241 . The energy in the second portion of electricity  241  is used to drive the reformation of the water  239  into hydrogen  242  and oxygen  243 . 
     The hydrogen  242  may flow into an optional hydrogen conditioner  244 . In the optional hydrogen conditioner  244  any unwanted molecules (such as water or oxygen) can be removed and the gas may be compressed, and/or an optional second recycling line  245  may be included to reinject a portion of the gases back into the electrolysis unit  240 . Gases not recycled to the electrolysis unit  240  exit the optional hydrogen conditioner  244  as conditioned hydrogen  246 . If the optional hydrogen conditioner  244  is not included the hydrogen  242  and the conditioned hydrogen  246  are equivalent. 
     The conditioned hydrogen-lean syngas initial product  238  and the conditioned hydrogen  246  flow into a conditioner  247 . The conditioner  247  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  247  mixes the conditioned hydrogen-lean syngas initial product  238  and the conditioned hydrogen  246 . The conditioner  247  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  247  depends partly on if the optional hydrogen-lean syngas initial product conditioner  236  and the optional hydrogen conditioner  244  were included. Although not shown, a recycling line could also be included flowing from the conditioner  247  to the first reformer unit  233 , the electrolysis unit  240 , or both. Conditioned syngas  248  exits the conditioner  247 . 
     The conditioned syngas  248  flows to a Fischer-Tropsch unit  249  where a synthetic hydrocarbon product  250  is formed. Most synthetic hydrocarbon products  250  require syngas with a hydrogen to carbon monoxide ratio of about 2. By separately controlling the throughput of the first reformer unit  233  and the electrolysis unit  240 , syngas with ratios between about 1 and 3, could be produced. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant synthetic hydrocarbon products  250  can be reduced as compared to the state-of-the-art. 
     Oxygen  243 , produced in the electrolysis unit  240 , is fed to a compressor  251  where compressed oxygen  252  is formed. If needed, though not shown, an oxygen conditioning unit could be included to prepare the oxygen  243  for the compressor  251 . The sale of the compressed oxygen  252  may help offset the costs of the synthetic hydrocarbon product  250 , making the price of the synthetic hydrocarbon product  250  which has a reduced carbon footprint more competitive with state-of-the-art hydrocarbon products that do not have a reduced carbon footprint. 
     Preferably the first reformer unit  233  comprise a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  233  comprises a microwave discharge. The operating pressure of the first reformer unit  233  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  233  is between 0.95 and 5 atm. 
     Regarding recycling in this example, including the optional first recycling line  237  may help prevent solid carbon formation in the first reformer unit  233 . The inclusion of the optional second recycling line  245  may be unnecessary. The optional hydrogen-lean syngas initial product conditioner  236  may simply comprise a filter to remove any solids and a pump to drive the flows back to the reforming units. The recycling of hydrocarbon-rich downstream byproducts (not shown) produced in the Fischer-Tropsch unit  249  to the first reformer unit  233  will help to improve efficiency and reduce consumables consumption. 
     The conditioner  247  will likely comprise a compressor as Fischer-Tropsch processes usually require pressures over 10 atm. 
     Depending on the sulfur content of the methane source used in the first reactants  232 , the conditioner  247  may also comprise a sulfur removal bed. Further, depending on the requirements of the Fischer-Tropsch unit  249 , formed water or slipped carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of a synthetic hydrocarbon product  250  has been described above the conditioned syngas  248  could also be used as reduction gas for steel refining, to make methanol, to make alcohols, or to make aldehydes. Each alternative product may require syngas with a different hydrogen to carbon monoxide ratio, the throughput of the first reformer unit  233  and the electrolysis unit  240  may be altered to match the ratio needed. 
     Example of the Second Embodiment: a System for the Chemical Production of Synthetic Hydrocarbon Products and Carbon with an Optimized Carbon Footprint 
       FIG. 6  gives a block diagram of a system for the chemical production of synthetic hydrocarbon products and carbon with an optimized carbon footprint according to the second embodiment  261 . First reactants  262 , which are methane and carbon dioxide, are fed into a first reformer unit  263  along with a first portion of electricity  264 . The energy in the first portion of electricity  264  is used to drive the reformation of the methane and carbon dioxide into a hydrogen-lean syngas initial product  265 . The hydrogen-lean syngas initial product  265  has a hydrogen to carbon monoxide ratio of 0 to 1.5. 
     The hydrogen-lean syngas initial product  265  may flow into an optional hydrogen-lean syngas initial product conditioner  266 . In the optional hydrogen-lean syngas initial product conditioner  266  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  267  may be included to reinject a portion of the gases back into the first reformer unit  263 . Gases not recycled to the first reformer unit  263  exit the optional hydrogen-lean syngas initial product conditioner  266  as a conditioned hydrogen-lean syngas initial product  268 . If the optional hydrogen-lean syngas initial product conditioner  266  is not included the hydrogen-lean syngas initial product  265  and the conditioned hydrogen-lean syngas initial product  268  are equivalent. 
     Methane  269  is fed into a second reformer unit  270  along with a second portion of electricity  271 . The energy in the second portion of electricity  271  is used to drive the reformation (pyrolysis) of the methane  269  into hydrogen  272  and carbon  273 . 
     The hydrogen  272  may flow into an optional hydrogen conditioner  274 . In the optional hydrogen conditioner  274  any unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gas may be compressed, and/or an optional second recycling line  275  may be included to reinject a portion of the gases back into the second reformer unit  270 . Gases not recycled to the second reformer unit  270  exit the optional hydrogen conditioner  274  as conditioned hydrogen  276 . If the optional hydrogen conditioner  274  is not included the hydrogen  272  and the conditioned hydrogen  276  are equivalent. 
     The conditioned hydrogen-lean syngas initial product  268  and the conditioned hydrogen  276  flow into a conditioner  277 . The conditioner  277  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  277  mixes the conditioned hydrogen-lean syngas initial product  268  and the conditioned hydrogen  276 . The conditioner  277  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  277  depends partly on if the optional hydrogen-lean syngas initial product conditioner  266  and the optional hydrogen conditioner  274  were included. Although not shown, a recycling line could also be included flowing from the conditioner  277  to the first reformer unit  263 , the second reformer unit  270 , or both. Conditioned syngas  278  exits the conditioner  277 . 
     The conditioned syngas  278  flows to a Fischer-Tropsch unit  279  where synthetic hydrocarbon products  280  are formed. Most synthetic hydrocarbon products  280  require syngas with a hydrogen to carbon monoxide ratio of about 2. By separately controlling the throughput of the first reformer unit  263  and the second reformer unit  270 , syngas with ratios between about 1 and 3, could be produced. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant synthetic hydrocarbon products  280  can be reduced as compared to the state-of-the-art. 
     Carbon  273 , produced in the second reformer unit  270 , is fed to a carbon processing unit  281  where carbon product  282  is formed. If needed, though not shown, a carbon conditioning unit could be included to prepare the carbon  273  for the carbon processing unit  281 . The sale of the carbon product  282  may help offset the costs of the synthetic hydrocarbon product  280 , making the price of the synthetic hydrocarbon product  280  which has a reduced carbon footprint more competitive with state-of-the-art hydrocarbon products that do not have a reduced carbon footprint. 
     Preferably the first reformer unit  263  and the second reformer unit  270  comprise plasma-based reformers, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  233  and the second reformer unit  270  comprise microwave discharges. The operating pressure of the first reformer unit  233  and the second reformer unit  270  are preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  233  and the second reformer unit  270  are between 0.95 and 5 atm. 
     Regarding recycling in this example, including an optional first recycling line  267  and/or an optional second recycling line  275  may help prevent solid carbon formation in the first reformer unit  263  and/or the second reformer unit  270 . The inclusion of the optional second recycling line  275  may be especially useful in the preferred embodiment where the second reformer unit is a plasma-based reformer. In such a reformer hydrogen gas from the second recycling line  275  could be used as a plasma gas within the plasma region of the reformer, and the methane  269  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The optional hydrogen-lean syngas initial product conditioner  266  and the optional hydrogen conditioner  274  may simply comprise a filter to remove any solids and a pump to drive the flows back to the reforming units. Hydrogen-rich gases may prove best for reducing carbon solid formation within the reformer units, as such it is also possible to include an optional recycling line from the optional hydrogen conditioner  274  to the first reformer unit  263 . The recycling of hydrocarbon-rich downstream byproducts produced in the Fischer-Tropsch unit  279  to the first reformer unit  263 , second reformer unit  270 , or both reformer units will help to improve efficiency and reduce consumables consumption. 
     The conditioner  277  will likely comprise a compressor as Fischer-Tropsch processes usually require pressures over 10 atm. Depending on the sulfur content of the methane source used in the first reactants  262  and the methane  269 , the conditioner  277  may also comprise a sulfur removal bed. Further, depending on the requirements of the Fischer-Tropsch unit  279 , formed water or slipped carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of a synthetic hydrocarbon product  280  has been described above the conditioned syngas  278  could also be used as reduction gas for steel refining, to make methanol, to make alcohols, or to make aldehydes. Each alternative product may require syngas with a different hydrogen to carbon monoxide ratio, the throughput of the first reformer unit  263  and the second reformer unit  270  may be altered to match the ratio needed. 
     The carbon product  282  produced will depend largely on the quality of the carbon  273  produced. If high quality carbons such as carbon nanotubes, graphene, graphite, or carbon black are produced the carbon processing unit  281  may include product separation, refining, and/or packaging of the carbon product  282 . If the carbon  273  is not directly marketable as a high-end carbon product it could be used as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). 
     Example of the Second Embodiment: a System for the Chemical Production of Ammonia and Carbon with an Optimized Carbon Footprint 
       FIG. 7  gives a block diagram of a system for the chemical production of ammonia and carbon with an optimized carbon footprint according to the second embodiment  291 . Air  292  is taken into an air separation unit  293  along with a first portion of electricity  294 . The energy in the first portion of electricity  264  is used to drive the isolation of nitrogen from other gases in air, thus reforming the air  292  into a stream of nitrogen  295 . Nitrogen-lean air, not shown, may be vented. 
     The nitrogen  295  may flow into an optional nitrogen conditioner  296 . In the optional nitrogen conditioner  296  unwanted molecules (such as water, oxygen, carbon dioxide) can be removed and the gas may be compressed, and/or an optional first recycling line  297  may be included to reinject a portion of the gas back into the air separation unit  293 . Gases not recycled to the air separation unit  293  exit the optional nitrogen conditioner  296  as conditioned nitrogen  298 . If the optional nitrogen conditioner  296  is not included the nitrogen  295  and the conditioned nitrogen  298  are equivalent. 
     Methane  299  is fed into a second reformer unit  300  along with a second portion of electricity  301 . The energy in the second portion of electricity  301  is used to drive the reformation (pyrolysis) of the methane  299  into hydrogen  302  and carbon  303 . 
     The hydrogen  302  may flow into an optional hydrogen conditioner  304 . In the optional hydrogen conditioner  304  any unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gas may be compressed, and/or an optional second recycling line  305  may be included to reinject a portion of the gases back into the second reformer unit  300 . Gases not recycled to the second reformer unit  300  exit the optional hydrogen conditioner  304  as conditioned hydrogen  306 . If the optional hydrogen conditioner  304  is not included the hydrogen  302  and the conditioned hydrogen  306  are equivalent. 
     The conditioned nitrogen  298  and the conditioned hydrogen  306  flow into a conditioner  307 . The conditioner  307  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  307  mixes the conditioned nitrogen  298  and the conditioned hydrogen  306 . The conditioner  307  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  307  depends partly on if the optional nitrogen conditioner  296  and the optional hydrogen conditioner  304  were included. Although not shown, a recycling line could also be included flowing from the conditioner  307  to the air separation unit  293 , the second reformer unit  300 , or both. Conditioned nitrogen and hydrogen  308  exit the conditioner  307 . 
     The conditioned nitrogen and hydrogen  308  flows to a Haber-Bosch unit  309  where ammonia  310  is formed. Ammonia  310  production requires a hydrogen to nitrogen ratio of about 3. By separately controlling the throughput of the air separation unit  293  and the second reformer unit  300 , the hydrogen to nitrogen ratio can be tailored to the application. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant ammonia  310  can be reduced as compared to the state-of-the-art. 
     Carbon  303 , produced in the second reformer unit  300 , is fed to a carbon processing unit  311  where carbon product  312  is formed. If needed, though not shown, a carbon conditioning unit could be included to prepare the carbon  303  for the carbon processing unit  311 . The sale of the carbon product  312  may help offset the costs of the ammonia  310 , making the price of the ammonia  310  which has a reduced carbon footprint more competitive with state-of-the-art ammonia products that do not have a reduced carbon footprint. 
     Preferably the second reformer unit  300  comprises a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the second reformer unit  300  comprises a microwave discharge. The operating pressure of the second reformer unit  300  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the second reformer unit  300  is between 0.95 and 5 atm. 
     Regarding recycling in this example, the inclusion of the optional first recycling line  297  may be unnecessary. Including the optional second recycling line  305  may help prevent solid carbon formation in the second reformer unit  300 . The inclusion of the optional second recycling line  305  may be especially useful in the preferred embodiment where the second reformer unit is a plasma-based reformer. In such a reformer hydrogen gas from the second recycling line  305  could be used as a plasma gas within the plasma region of the reformer, and the methane  299  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The conditioner  307  will likely comprise a compressor as Haber-Bosch processes usually require pressures around 200 atm. Depending on the sulfur content of the methane source used for methane  299  the conditioner  307  may also comprise a sulfur removal bed. Further, depending on the requirements of the Haber-Bosch unit  309 , formed water or slipped carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of ammonia  310  has been described above additional processing steps may occur after the production of ammonia to form other products. Other possible products include urea, uric acid, ammonia hydroxide, and/or ammonium nitrate and other fertilizers. 
     The carbon product  312  produced will depend largely on the quality of the carbon  303  produced. If high quality carbons such as carbon nanotubes, graphene, graphite, or carbon black are produced the carbon processing unit  311  may include product separation, refining, and/or packaging of the carbon product  312 . If the carbon  303  is not directly marketable as a high-end carbon product it could be used as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). 
     Embodiment 3 
       FIG. 8  gives a block diagram of a system for chemical production with an optimized carbon footprint according to the third embodiment  401 . First reactants  402  are fed into a first reformer unit  403  along with a first portion of electricity  404 . 
     The energy in the first portion of electricity  404  is used to drive the reformation of the first reactants  402  into a first initial product  405  and a first secondary initial product  406 . The first reformer unit  403  is configured to use the first portion of electricity  404  to molecularly alter the composition of the first reactants  402 . 
     The first initial product  405  flows to a conditioner  407 . The conditioner  407  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  407  may compress, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), add additional molecules, heat, and/or cool the gases. An optional first recycling line  408  can be included to return a portion of the gas to the first reformer unit  403 . Any gases not recycled exit the conditioner  407  as a conditioned intermediate product  409 . 
     The conditioned intermediate product  409  flows to a processing unit  410  where a final chemical product  411  is formed. The processing unit  410  may be as simple as bottling or depositing the conditioned intermediate product  409  into a pipeline. The processing unit  410  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     The first secondary initial product  406 , produced in the first reformer unit  403 , is fed to a secondary product processing unit  412  where a secondary final chemical product  413  is formed. If needed, though not shown, an additional conditioning unit could be included to prepare the first secondary initial product  406  for the secondary product processing unit  412 . The secondary product processing unit  412  may be as simple as packing, bottling, or moving the first secondary initial product  406 . The secondary product processing unit  412  may also include further molecule processing steps such as forming carbon dioxide for enhanced oil and gas recovery. The sale of the secondary final chemical product  413  may help offset the costs of the final chemical product  411 , making the price of the final chemical product  411  which has a reduced carbon footprint more competitive with state-of-the-art products that do not have a reduced carbon footprint. 
     Example of the third Embodiment: a System for the Chemical Production of Hydrogen and Carbon with an Optimized Carbon Footprint 
       FIG. 9  gives a block diagram of a system for the chemical production of hydrogen and carbon with an optimized carbon footprint according to the third embodiment  421 . Methane  422  is fed into a first reformer unit  423  along with a first portion of electricity  424 . The energy in the first portion of electricity  424  is used to drive the reformation (pyrolysis) of the methane  422  into hydrogen  425  and carbon  426 . 
     The hydrogen  425  flows to a conditioner  427 . The conditioner  427  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  427  may compress, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), add additional molecules, heat, and/or cool the gases. An optional first recycling line  428  can be included to return a portion of the gas to the first reformer unit  423 . Any gases not recycled exit the conditioner  427  as conditioned hydrogen  429 . 
     The conditioned hydrogen  429  flows to a hydrogen processing unit  430  where a hydrogen product  431  is formed. The hydrogen processing unit  430  may be as simple as bottling or depositing the conditioned hydrogen  429  into a pipeline. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant hydrogen product  431  can be reduced as compared to the state-of-the-art. 
     Carbon  426 , produced in the first reformer unit  423 , is fed to a carbon processing unit  432  where carbon product  433  is formed. If needed, though not shown, a carbon conditioning unit could be included to prepare the carbon  426  for the carbon processing unit  432 . The sale of the carbon product  433  may help offset the costs of the hydrogen product  431 , making the price of the hydrogen product  431  which has a reduced carbon footprint more competitive with state-of-the-art hydrogen products that do not have a reduced carbon footprint. 
     Preferably the first reformer unit  423  comprises a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  423  comprises a microwave discharge. The operating pressure of the first reformer unit  423  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  423  is between 0.95 and 5 atm. 
     Regarding recycling in this example, the inclusion of the optional first recycling line  428  may help prevent solid carbon formation in critical areas of the first reformer unit  423 . The inclusion of the optional first recycling line  428  may be especially useful in the preferred embodiment where the first reformer unit is a plasma-based reformer. In such a reformer hydrogen gas from the first recycling line  428  could be used as a plasma gas within the plasma region of the reformer, and the methane  422  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The conditioner  427  may comprise a compressor. Depending on the sulfur content of the methane source used for methane  422  the conditioner  427  may also comprise a sulfur removal bed. Further, depending on the hydrogen purity requirements downstream, water or carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of hydrogen product  431  has been described above additional processing steps may occur after the production of hydrogen to form other products. The hydrogen processing unit  430  may also include further molecule processing steps such interfacing with other molecule sources to form ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     The carbon product  433  produced will depend largely on the quality of the carbon  426  produced. If high quality carbons such as carbon nanotubes, graphene, graphite, or carbon black are produced the carbon processing unit  432  may include product separation, refining, and/or packaging of the carbon product  433 . If the carbon  426  is not directly marketable as a high-end carbon product it could be used as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). 
     Embodiment 4 
       FIG. 10  gives a block diagram of a system for chemical production with an optimized carbon footprint according to the fourth embodiment  501 . First reactants  502  are fed into a first reformer unit  503  along with a first portion of electricity  504 . The energy in the first portion of electricity  504  is used to drive the reformation of the first reactants  502  into a first initial product  505  and a first secondary initial product  506 . The first reformer unit  503  is configured to use the first portion of electricity  504  to molecularly alter the composition of the first reactants  502 . 
     The first initial product  505  may flow into an optional first initial product conditioner  507 . In the optional first initial product conditioner  507  unwanted molecules (such as water, carbon dioxide, methane, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  508  may be included to reinject a portion of the gases back into the first reformer unit  503 . Gases not recycled to the first reformer unit  503  exit the optional first initial product conditioner  507  as a first conditioned initial product  509 . If the optional first initial product conditioner  507  is not included the first initial product  505  and first conditioned initial product  509  are equivalent. 
     The first conditioned initial product  509  and second reactants  510  flow into a second reformer unit  511 . In the second reformer unit  511  the first conditioned initial product  509  and second reactants  510  are reformed into a second initial product  512 . The second reformer unit  511  is configured to molecularly alter the composition of the first conditioned initial product  509  and the second reactants  510 . 
     The second initial product  512  flows into a conditioner  513 . The conditioner  513  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  513  may compress the gases, remove unwanted molecules (such as water, carbon dioxide, methane sulfur-containing molecules), and add additional molecules. Although not shown, a recycling line could also be included flowing from the conditioner  513  to the first reformer unit  503 , the second reformer unit  511 , or both reformers. A conditioned intermediate product  514  exits the conditioner  513 . 
     The conditioned intermediate product  514  flows to a processing unit  515  where a final chemical product  516  is formed. The processing unit  515  may be as simple as bottling or depositing the conditioned intermediate product  514  into a pipeline. The processing unit  515  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     The first secondary initial product  506 , produced in the first reformer unit  503 , is fed to a secondary product processing unit  517  where a secondary final chemical product  518  is formed. If needed, though not shown, an additional conditioning unit could be included to prepare the first secondary initial product  506  for the secondary product processing unit  517 . The secondary product processing unit  517  may be as simple as packing, bottling, or moving the first secondary initial product  506 . The secondary product processing unit  517  may also include further molecule processing steps such as forming carbon dioxide for enhanced oil and gas recovery. The sale of the secondary final chemical product  518  may help offset the costs of the final chemical product  516 , making the price of the final chemical product  516  which has a reduced carbon footprint more competitive with state-of-the-art products that do not have a reduced carbon footprint. 
     Example of the fourth embodiment: a system for the chemical production of synthetic hydrocarbon products and carbon with an optimized carbon footprint. 
       FIG. 11  gives a block diagram of a system for the chemical production of synthetic hydrocarbon products and carbon with an optimized carbon footprint according to the fourth embodiment  521 . Methane  522  is fed into a first reformer unit  523  along with a first portion of electricity  524 . The energy in the first portion of electricity  524  is used to drive the reformation (pyrolysis) of the methane  522  into hydrogen  525  and carbon  526 . 
     The hydrogen  525  may flow into an optional hydrogen conditioner  527 . In the optional hydrogen conditioner  527  any unwanted molecules (such as water, carbon dioxide, methane, sulfur-containing molecules) can be removed and the gas may be compressed, and/or an optional first recycling line  528  may be included to reinject a portion of the gases back into the first reformer unit  523 . Gases not recycled to the first reformer unit  523  exit the optional hydrogen conditioner  527  as conditioned hydrogen  529 . If the optional hydrogen conditioner  527  is not included the hydrogen  525  and the conditioned hydrogen  529  are equivalent. 
     The conditioned hydrogen  529  and carbon dioxide  530  flow into a reverse water-gas shift unit  531 . In the reverse water-gas shift unit  531  a portion of the conditioned hydrogen  529  and carbon dioxide  530  are reformed into carbon monoxide and water, and a mixture  532  comprising syngas, water, and carbon dioxide. 
     The mixture  532  of syngas, water, and carbon dioxide flow into a conditioner  533 . The conditioner  533  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  533  may remove the produced water and any slipped carbon dioxide using a vapor-liquid separator and/or amine scrubbing. The conditioner  533  may also compress the gases, remove additional unwanted molecules (such as sulfur-containing molecules), and add additional molecules. Although not shown, a recycling line could also be included flowing from the conditioner  533  to the first reformer unit  523 , the reverse water-gas shift unit  531 , or both. Conditioned syngas  534  exits the conditioner  533 . 
     The conditioned syngas  534  flows to a Fischer-Tropsch unit  535  where synthetic hydrocarbon products  536  are formed. Most synthetic hydrocarbon products  536  require syngas with a hydrogen to carbon monoxide ratio of about 2. By separately controlling the throughput of the first reformer unit  523  and the reverse water-gas shift unit  531 , syngas with any ratio could be produced. By driving the reforming process with at least a portion of the first portion of electricity  524  being generated without emitting greenhouse gases the carbon footprint of the resultant synthetic hydrocarbon products  536  can be reduced as compared to the state-of-the-art. Further, if the first portion of electricity  524  is generated without emitting greenhouse gases all carbon in the resultant synthetic hydrocarbon products  536  will originate from the carbon dioxide  530 , thus forming a closed carbon cycle (upon combustion). 
     Carbon  526 , produced in the first reformer unit  523 , is fed to a carbon processing unit  537  where carbon product  538  is formed. If needed, though not shown, a carbon conditioning unit could be included to prepare the carbon  526  for the carbon processing unit  537 . The sale of the carbon product  538  may help offset the costs of the synthetic hydrocarbon product  536 , making the price of the synthetic hydrocarbon product  536  which has a reduced carbon footprint more competitive with state-of-the-art hydrocarbon products that do not have a reduced carbon footprint. 
     Preferably the first reformer unit  523  comprises a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  523  comprise a microwave discharge. The operating pressure of the first reformer unit  523  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  523  is between 0.95 and 5 atm. 
     Regarding recycling in this example, including the optional first recycling line  528  may help prevent solid carbon formation in portions of the first reformer unit  523 . The inclusion of the optional first recycling line  528  may be especially useful in the preferred embodiment where the first reformer unit  523  is a plasma-based reformer. In such a reformer hydrogen gas from the first recycling line  528  could be used as a plasma gas within the plasma region of the reformer, and the methane  522  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The optional hydrogen conditioner  527  may simply comprise a filter to remove any solids and a pump to drive the flows back to the first reformer unit  523 . Depending on the pressure in the first reformer unit  523  and of the hydrogen  525  the optional hydrogen conditioner  527  may be required in order to pressurize the hydrogen  525  prior to entering the reverse water-gas shift unit  531 . The carbon dioxide  530  will also have to be pressurized to match that of the hydrogen  525 , or alternatively the carbon dioxide  530  could be compressed with the hydrogen  525  in the hydrogen conditioner  527 , not shown. 
     As mentioned previously, the conditioner  533  will likely comprise units for the removal of produced water and any slipped carbon dioxide. The conditioner  533  will likely also comprise a compressor as Fischer-Tropsch processes usually require pressures over 10 atm. Depending on the sulfur content of the methane source used in the methane  522  the conditioner  533  may also comprise a sulfur removal bed. 
     While the production of a synthetic hydrocarbon product  536  has been described above the conditioned syngas  534  could also be used as reduction gas for steel refining, to make methanol, to make alcohols, or to make aldehydes. Each alternative product may require syngas with a different hydrogen to carbon monoxide ratio, the throughput of the first reformer unit  523  and the reverse water-gas shift unit  531  may be altered to match the ratio needed. 
     The carbon product  538  produced will depend largely on the quality of the carbon  526  produced. If high quality carbons such as carbon nanotubes, graphene, graphite, or carbon black are produced the carbon processing unit  537  may include product separation, refining, and/or packaging of the carbon product  538 . If the carbon  526  is not directly marketable as a high-end carbon product it could be used as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). 
     Example of the Fourth Embodiment: a System for the Chemical Production of Synthetic Hydrocarbon Products and Carbon with an Optimized Carbon Footprint 
       FIG. 12  gives a block diagram of a system for the chemical production of ammonia and carbon with an optimized carbon footprint according to the fourth embodiment  541 . Methane  542  is fed into a first reformer unit  543  along with a first portion of electricity  544 . The energy in the first portion of electricity  544  is used to drive the reformation (pyrolysis) of the methane  542  into hydrogen  545  and carbon  546 . 
     The hydrogen  545  may flow into an optional hydrogen conditioner  547 . In the optional hydrogen conditioner  547  any unwanted molecules (such as water, carbon dioxide, methane, sulfur-containing molecules) can be removed and the gas may be compressed, and/or an optional first recycling line  548  may be included to reinject a portion of the gases back into the first reformer unit  543 . Gases not recycled to the first reformer unit  543  exit the optional hydrogen conditioner  547  as conditioned hydrogen  549 . If the optional hydrogen conditioner  547  is not included the hydrogen  545  and the conditioned hydrogen  549  are equivalent. 
     The conditioned hydrogen  549  and air  550  flow into combustion reformer unit  551 . In the combustion reformer unit  551  a portion of the conditioned hydrogen  549  and the oxygen within the air  550  are combusted reforming into water. A hydrogen and nitrogen-rich mixture  552 , which will also contain at least water and small amounts of carbon dioxide (from within the air) exits the combustion reformer unit  551 . 
     The hydrogen and nitrogen-rich mixture  552  flows into a conditioner  553 . The conditioner  553  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  553  may use a vapor-liquid separator to remove the water produced by combustion and naturally present in the air  550 . The conditioner  553  may also use amine scrubbing to remove the carbon dioxide. The conditioner  553  may also compress the gases, remove additional unwanted molecules (such as sulfur-containing molecules), and add additional molecules. Although not shown, a recycling line could also be included flowing from the conditioner  553  to the first reformer unit  543 . A mixture  554  of conditioned nitrogen and hydrogen exit the conditioner  553 . 
     The mixture  554  of conditioned nitrogen and hydrogen flows to a Haber-Bosch unit  555  where ammonia  556  is formed. Ammonia  556  production requires a hydrogen to nitrogen ratio of about 3. By separately controlling the throughput of the first reformer unit  543  and the air  550  to the combustion reformer unit  551 , the hydrogen to nitrogen ratio can be tailored to the application. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant ammonia  556  can be reduced as compared to the state-of-the-art. 
     Carbon  546 , produced in the first reformer unit  543 , is fed to a carbon processing unit  557  where carbon product  558  is formed. If needed, though not shown, a carbon conditioning unit could be included to prepare the carbon  546  for the carbon processing unit  557 . The sale of the carbon product  558  may help offset the costs of the ammonia  556 , making the price of the ammonia  556  which has a reduced carbon footprint more competitive with state-of-the-art ammonia products that do not have a reduced carbon footprint. 
     Preferably the first reformer unit  543  comprises a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  543  comprises a microwave discharge. The operating pressure of the first reformer unit  543  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  543  is between 0.95 and 5 atm. 
     Including the optional first recycling line  548  may help prevent solid carbon formation some regions off the first reformer unit  543 . The inclusion of the optional first recycling line  548  may be especially useful in the preferred embodiment where the first reformer unit  543  comprises a plasma-based reformer. In such a reformer hydrogen gas from the optional first recycling line  548  could be used as a plasma gas within the plasma region of the reformer, and the methane  542  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The conditioner  553  will likely comprise a compressor as Haber-Bosch processes usually require pressures around 200 atm. Depending on the sulfur content of the methane source used for methane  542  the conditioner  553  may also comprise a sulfur removal bed. 
     While the production of ammonia  556  has been described above additional processing steps may occur after the production of ammonia to form other products. Other possible products include urea, uric acid, ammonia hydroxide, and/or ammonium nitrate and other fertilizers. 
     The carbon product  558  produced will depend largely on the quality of the carbon  546  produced. If high quality carbons such as carbon nanotubes, graphene, graphite, or carbon black are produced the carbon processing unit  557  may include product separation, refining, and/or packaging of the carbon product  558 . If the carbon  546  is not directly marketable as a high-end carbon product it could be used as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). 
     Embodiment 5 
       FIG. 13  gives a block diagram of a system for chemical production with an optimized carbon footprint according to the fifth embodiment  601 . First reactants  602  are fed into a first reformer unit  603  along with a first portion of electricity  604 . The energy in the first portion of electricity  604  is used to drive the reformation of the first reactants  602  into a first initial product  605  and a first secondary initial product  606 . The first reformer unit  603  is configured to use the first portion of electricity  604  to molecularly alter the composition of the first reactants  602 . 
     The first initial product  605  may flow into an optional first initial product conditioner  607 . In the optional first initial product conditioner  607  unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules) can be removed and the gases may be compressed, and/or an optional first recycling line  608  may be included to reinject a portion of the gases back into the first reformer unit  603 . Gases not recycled to the first reformer unit  603  exit the optional first initial product conditioner  607  as a first conditioned initial product  609 . If an optional first initial product conditioner  607  is not included the first initial product  605  and first conditioned initial product  609  are equivalent. 
     Second reactants  610  are fed into a second reformer unit  611  along with a second portion of electricity  612 . The energy in the second portion of electricity  612  is used to drive the reformation of the second reactants  610  into a second initial product  613  and a second secondary initial product  614 . The second reformer unit  611  is configured to use the second portion of electricity  612  to molecularly alter the composition of the second reactants  610 . 
     The first conditioned initial product  609  and the second initial product  613  flow into a conditioner  615 . The conditioner  615  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  615  mixes the first conditioned initial product  609  and the second initial product  613 . The conditioner  615  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. The amount of conditioning that must occur in the conditioner  615  depends partly on if the optional first initial product conditioner  607  was included. Although not shown, a recycling line could also be included flowing from the conditioner  615  to the first reformer unit  603 , the second reformer unit  611 , or both reformers. A conditioned intermediate product  616  exits the conditioner  615 . 
     The conditioned intermediate product  616  flows to a processing unit  617  where a final chemical product  618  is formed. The processing unit  617  may be as simple as bottling or depositing the conditioned intermediate product  616  into a pipeline. The processing unit  617  may also include further molecule processing steps such as ammonia, urea, methanol, alcohols, and hydrocarbon formation or oil refining. 
     The second secondary initial product  614 , produced in the second reformer unit  611 , may flow into an optional second secondary product conditioner  619 . In the optional second secondary product conditioner  619  unwanted molecules (such as water, sulfur-containing molecules) can be removed and the gases may be compressed. Conditioned second secondary product  620  exits the second secondary product conditioner  619 . If an optional second secondary product conditioner  619  is not included the second secondary initial product  614  and the conditioned second secondary product  620  are equivalent. 
     First secondary initial product  606  and conditioned second secondary product  620  are flow into a third reformer unit  621 . In the third reformer unit  621  the first secondary initial product  606  and the conditioned second secondary product  620  are reformed into a third primary product  622 , a third secondary product  623 , and a third tertiary product  624 . Although not shown, if needed additional processing units could be included downstream of the third primary product  622 , third secondary product  623 , and/or third tertiary product  624  in order to form additional final products. 
     Example of the Fifth Embodiment: a System for the Chemical Production of Ammonia, Carbon, Carbon Dioxide, and Electricity with an Optimized Carbon Footprint 
       FIG. 14  gives a block diagram of a system for the chemical production of ammonia, carbon, carbon dioxide, and electricity with an optimized carbon footprint according to the fifth embodiment  631 . Methane  632  is fed into a first reformer unit  633  along with a first portion of electricity  634 . The energy in the first portion of electricity  634  is used to drive the reformation (pyrolysis) of the methane  632  into hydrogen  635  and carbon  636 . 
     The hydrogen  635  may flow into an optional hydrogen conditioner  637 . In the optional hydrogen conditioner  637  any unwanted molecules (such as water, carbon dioxide, methane, sulfur-containing molecules) can be removed and the gas may be compressed, and/or an optional first recycling line  638  may be included to reinject a portion of the gases back into the first reformer unit  633 . Gases not recycled to the first reformer unit  633  exit the optional hydrogen conditioner  637  as conditioned hydrogen  639 . If the optional hydrogen conditioner  637  is not included the hydrogen  635  and the conditioned hydrogen  639  are equivalent. 
     Air  640  is taken into an air separation unit  641  along with a second portion of electricity  642 . The energy in the second portion of electricity  642  is used to drive the isolation of nitrogen from other gases in air, thus reforming the air  640  into a stream of nitrogen  643  and nitrogen-lean air  644  comprising primarily oxygen and carbon dioxide. 
     The conditioned hydrogen  639  and the nitrogen  643  flow into a conditioner  645 . The conditioner  645  alters the properties (composition, temperature, pressure) of the gases to that which is required downstream. The conditioner  645  mixes the conditioned hydrogen  639  and the nitrogen  643 . The conditioner  645  may also compress the gases, remove unwanted molecules (such as water, carbon dioxide, sulfur-containing molecules), and add additional molecules. A mixture  646  of conditioned nitrogen and hydrogen exits the conditioner  645 . 
     The mixture  646  of conditioned nitrogen and hydrogen flows to a Haber-Bosch unit  647  where ammonia  648  is formed. Ammonia  648  production requires a hydrogen to nitrogen ratio of about 3. By separately controlling the throughput of the first reformer unit  633  and the air separation unit  641 , the hydrogen to nitrogen ratio can be tailored to the application. By driving the reforming process with at least a portion of the electricity made without emitting greenhouse gases the carbon footprint of the resultant ammonia  648  can be reduced as compared to the state-of-the-art. 
     The nitrogen-lean air  644  comprising primarily oxygen and carbon dioxide, produced in the air separation unit  641 , may flow into an optional oxygen and carbon dioxide conditioner  649 . In the optional oxygen and carbon dioxide conditioner  649  unwanted molecules can be removed and the gases may be compressed. A mixture  650  of conditioned oxygen and carbon dioxide exits the optional oxygen and carbon dioxide conditioner  649 . If an optional oxygen and carbon dioxide conditioner  649  is not included the nitrogen-lean air  644  comprising primarily oxygen and carbon dioxide and the mixture  650  of conditioned oxygen and carbon dioxide are equivalent. 
     Carbon  636 , produced in the first reformer unit  633 , and the mixture  650  of conditioned oxygen and carbon dioxide are fed to a combustion reformer unit  651 . In the combustion reformer unit  651  a portion of the carbon  636  and the oxygen within the mixture  650  of conditioned oxygen and carbon dioxide are combusted reforming into carbon dioxide. Carbon dioxide  652  is the first product of the combustion reformer unit  651 . The carbon dioxide  652  could be compressed and used for enhanced oil and gas recovery, alternatively, it could be used along with the ammonia  648  to produce urea. Carbon product  653  is the second product of the combustion reformer unit, as described in this example application for ammonia production. More carbon  636  will be produced than can be combusted with the oxygen in nitrogen-lean air  644  leading to a remaining carbon product  653 . The third product of the combustion reformer unit  651  is generated electricity  654 . The combustion of carbon and oxygen is highly exothermic, the heat produced can be used to boil water to turn steam turbines or the expanding hot carbon dioxide can be used to directly turn turbines producing generated electricity  654 . This electricity  654  may be supplied to the first reformer unit  633 , the air separation unit  641  or both. 
     Preferably the first reformer unit  633  comprises a plasma-based reformer, such as, DC glow discharge, radio frequency discharge, arc discharge, corona discharge, dielectric barrier discharge, microwave discharge, AC discharge, or a gliding arc discharge. More preferably the first reformer unit  633  comprises a microwave discharge. The operating pressure of the first reformer unit  633  is preferably between 0.1 and 10 atm. More preferably the operating pressure of the first reformer unit  633  is between 0.95 and 5 atm. 
     Including the optional first recycling line  638  may help prevent solid carbon formation in the first reformer unit  633 . The inclusion of the optional first recycling line  638  may be especially useful in the preferred embodiment where the first reformer unit  633  is a plasma-based reformer. In such a reformer hydrogen gas from the optional first recycling line  638  could be used as a plasma gas within the plasma region of the reformer, and the methane  632  could be injected downstream from the plasma-region into the hot hydrogen gas to ensure carbon does not deposit within the plasma-region. 
     The conditioner  645  will likely comprise a compressor as Haber-Bosch processes usually require pressures around 200 atm. 
     Depending on the sulfur content of the methane source used for methane  632  the conditioner  645  may also comprise a sulfur removal bed. Further, depending on the requirements of the Haber-Bosch unit  647 , water or carbon dioxide may need to be reduced as well using a vapor-liquid separator and/or amine scrubbing. 
     While the production of ammonia  648  has been described above additional processing steps may occur after the production of ammonia to form other products. Other possible products include urea (which as mentioned above could use the carbon dioxide  652 ), uric acid, ammonia hydroxide, and/or ammonium nitrate and other fertilizers. 
     The carbon product  653  produced will depend largely on the quality of the carbon  636  produced. High quality carbon products  653  include carbon nanotubes, graphene, graphite, and carbon black. Lower quality carbon products  653  include use as biochar, reverse mined (buried) for carbon sequestration, or sequestered as carbon dioxide through enhanced oil and gas recovery (additional details on this use will be presented later). If a spectrum of carbon  636  is produced lower value carbon could be combusted in the combustion reformer unit  651  while the higher value carbon could be used as the carbon product  653 . 
     Use of carbon for enhanced oil and gas recovery 
     As mentioned in many of the embodiments, the carbon product from the various systems for chemical production may be used for enhanced oil and gas recovery by producing and sequestering carbon dioxide. In this section three example systems for using the carbon product to produce and sequester carbon dioxide while recovering oil and gas product are given. 
       FIG. 15  gives a block diagram of a first example enhanced oil and gas recovery system using carbon product  701 . Carbon product from upstream production  702  enters a combustion and power generation unit  703 . Oxygen  704  from an air separation unit  705  also flows into the combustion and power generation unit  703 . The oxygen  704  is taken from the air  706  processed in the air separation unit  705 , oxygen poor air  707  from which the oxygen  704  is removed may be vented. 
     The carbon product from upstream production  702  and the oxygen  704  are combusted in the combustion and power generation unit  703  forming carbon dioxide  708 . The carbon dioxide  708  flows to a compressor  709 . 
     The combustion of carbon product from upstream production  702  and oxygen  704  in the combustion and power generation unit  703  produces heat which can be used to generate electricity directly by turning turbines with the carbon dioxide  708  or indirectly by producing steam that turns turbines. The electricity produced can include the electricity  710  for the air separation unit  705 , the electricity  711  for the compressor  709 , as well as additional electricity  712 . 
     Pressurized carbon dioxide  713  exits the compressor  709  and flows to an oil and gas field  714 . The pressurized carbon dioxide  713  aids in the recovery of oil and gas  715  from the oil and gas field  714 . A portion of the carbon dioxide  716  becomes sequestered carbon dioxide  717 , another portion of the carbon dioxide  718  is recovered from the oil and gas field  714  and returned for recompression in the compressor  709  prior to reinjection as pressurized carbon dioxide  713 . The portion of the carbon dioxide  716  that becomes sequestered carbon dioxide  717  is generally around 90%. 
     Optionally, the combustion and power generation unit  703  can operate at a pressure greater that atmospheric. In this case the air separation unit  705  provides oxygen  704  at a pressure greater than atmospheric. The solid carbon product from upstream production  702  will also have to pressurized to the same level. Combusting the carbon product from upstream production  702  and oxygen  704  at a higher pressure will produce carbon dioxide  708  also having a pressure higher than atmospheric. Less electricity  711  for the compressor  709  will be required as the carbon dioxide  708  is already partly pressurized. 
     One benefit to this enhanced oil and gas recovery technique is the power production should be sufficient to drive carbon dioxide sequestration and oil and gas recovery, this may be vital for remote sites. For example, a system for the chemical production of hydrogen and carbon with an optimized carbon footprint according to the third embodiment  421  ( FIG. 9 ) which is configured to produce 50 tonnes of hydrogen product  431  would produce about 6.3 tonnes of carbon product  433  every hour. The combustion of this 6.3 tonnes of carbon product from upstream production  702  ( FIG. 15 ) requires 16.7 tonnes of oxygen  704  and produces 23 tonnes of carbon dioxide  708  every hour. Approximately 8 MW of electricity would be generated by combustion, about 4 MW of electricity are required for electricity  710  for the air separation unit  705  and the other 4 MW of electricity are required as electricity  711  for the compressor  709 . Thus, the combustion of carbon should generate enough electricity to drive the sequestration of carbon dioxide  717  and oil and gas  715  recovery. This example assumed the air separation unit  705  was used to produce pure oxygen  704 . However, if less pure oxygen  704  can be used the air separation unit  705  will not require as much electricity  710 . An air separation unit  705  producing oxygen  704  of 95% concentration will require about 1 MW less electricity  710  per hour, in this case additional electricity  712  is produced. 
       FIG. 16  gives a block diagram of a second example enhanced oil and gas recovery system using carbon product  721 . Carbon product from upstream production  722  enters a combustion and power generation unit  723 . Air  724  is driven into the combustion and power generation unit  723 . The carbon product from upstream production  722  and the air  724  are combusted in the combustion and power generation unit  723  forming a carbon dioxide-rich gas  725 . The carbon dioxide-rich gas  725  exits the combustion and power generation unit  723  and flows into amine scrubber unit  726 . 
     The amine scrubber unit  726  separates the carbon dioxide-rich gas  725  into a stream of primarily nitrogen gas  727  which can be vented and carbon dioxide  728 . The carbon dioxide  728  flows to a compressor  729 . 
     The combustion of carbon product from upstream production  722  and air  724  in the combustion and power generation unit  723  produces heat which can be used to generate electricity directly by turning turbines with the carbon dioxide-rich gas  725  or indirectly by producing steam that turns turbines. The electricity produced can include the electricity  730  for the compressor  729 , as well as additional electricity  731 . 
     Pressurized carbon dioxide  732  exits the compressor  729  and flows to an oil and gas field  733 . The pressurized carbon dioxide  732  aids in the recovery of oil and gas  734  from the oil and gas field  733 . A portion of the carbon dioxide  735  becomes sequestered carbon dioxide  736 , another portion of the carbon dioxide  737  is recovered from the oil and gas field  733  and returned for recompression in the compressor  729  prior to reinjection as pressurized carbon dioxide  732 . The portion of the carbon dioxide  735  that becomes sequestered carbon dioxide  736  is generally around 90%. 
     One benefit to this enhanced oil and gas recovery technique is the power production should be sufficient to drive carbon dioxide sequestration and oil and gas recovery, this may be vital for remote sites. For example, a system for the chemical production of hydrogen and carbon with an optimized carbon footprint according to the third embodiment  421  ( FIG. 9 ) which is configured to produce 50 tonnes of hydrogen product  431  would produce about 6.3 tonnes of carbon product  433  every hour. The combustion of this 6.3 tonnes of carbon product from upstream production  722  ( FIG. 16 ) requires about 72 tonnes of air  724  and produces about 78 tonnes of carbon dioxide-rich gas  725  every hour. Approximately 7.5 MW of electricity would be generated by combustion, about 4.7 MW of electricity  730  are required as electricity for the compressor  729 . Thus, the combustion of carbon should generate enough electricity to drive the sequestration of carbon dioxide  736  and oil and gas  734  recovery. This example assumed the amine scrubber unit  726  produces 95% carbon dioxide  728  (about 24 tonnes per hour). The additional electricity  731  should be enough to drive air  724  into the combustion and power generation unit  723 , and the pumps and boiler in the amine scrubber unit  726 . 
       FIG. 17  gives a block diagram of a third example enhanced oil and gas recovery system using carbon product  741 . Carbon product from upstream production  742  enters a heater unit  743 . Water  744  also flows into the heater unit  743 . Within the heater unit  743  the carbon product from upstream production  742  and water  744  are mixed into a slurry and heated using electricity  745  to a temperature greater than 600° C. At these temperatures, reformation of the carbon product from upstream production  742  and water  744  into a gas  746  with hydrogen and carbon dioxide takes place. 
     The gas  746  with hydrogen and carbon dioxide flow into a separation unit  747  (such as a pressure swing absorber unit or a membrane separator), here hydrogen product  748  is separated from carbon dioxide  749 . The hydrogen product  748  can be used as is or further processed into other chemicals (as discussed above). Carbon dioxide  749  flows out of the separation unit  747  into a compressor  750 . 
     The compressor  750  uses electricity  751  to compress the carbon dioxide  749 , and pressurized carbon dioxide  752  exits the compressor  750 . The pressurized carbon dioxide  752  flows to an oil and gas field  753 . The pressurized carbon dioxide  752  aids in the recovery of oil and gas  754  from the oil and gas field  753 . A portion of the carbon dioxide  755  becomes sequestered carbon dioxide  756 , another portion of the carbon dioxide  757  is recovered from the oil and gas field  753  and returned for recompression in the compressor  750  prior to reinjection as pressurized carbon dioxide  752 . The portion of the carbon dioxide  755  that becomes sequestered carbon dioxide  756  is generally around 90%. 
     Unlike the other two example oil and gas recovery applications, this example would require access to electricity  745  for the heater unit  743  and electricity  751  for the compressor  750 . However, this example also forms hydrogen product  748 , in addition to sequestered carbon dioxide  756  and oil and gas  754 .