Production process and production system for producing methane / gaseous and/or liquid hydrocarbons

Abstract

A process for the production of synthetically produced methane (57)/gaseous and/or liquid hydrocarbons (114, 115, 116, 117). For this purpose, hydrogen (44, 84, 150) from an electrolytic arrangement (41, 81, 151, 159) which is operated by means of regeneratively generated electric energy and carbon dioxide (19, 46, 86) are synthesized in a methane synthesis (FIGS. 2-48) or Fischer-Tropsch synthesis (FIGS. 3-96) or other suitable hydrocarbon synthesis, the carbon dioxide (19, 46, 86) being produced from an air/gas flow (3, 134) by means of a carbon dioxide recovery system (FIG. 1). The carbon dioxide (19, 46, 86) is obtained from the air/gas flow (3, 134) in the carbon dioxide recovery system (FIG. 1) by way of a reversible adsorption process. Also a production system (57) for the production of synthetically produced methane/gaseous and/or liquid hydrocarbons (114, 115, 116, 117), in particular for carrying out the production process according to the invention, comprising an electrolytic arrangement (41, 81, 151, 159) which is operated by means of regeneratively generated electric energy (42, 82, 153) for producing hydrogen (44, 84, 150), a carbon dioxide recovery system (FIG. 1) for producing carbon dioxide (19, 46, 86) from an air/gas flow (3, 134) and a methane (FIG. 2) or Fischer-Tropsch synthesis (FIG. 3) or any other suitable hydrocarbon synthesis for synthesizing hydrogen (44, 84, 150) and carbon dioxide (19, 45, 86) to methane (57)/gaseous and/or liquid hydrocarbons (114, 115, 116, 117).

Claims

1. A process for the synthesis at least one of gaseous and liquid hydrocarbons, the method comprising the steps: producing an oxygen and hydrogen gas stream by electrolysis of water in an electrolysis device; adsorbing carbon dioxide and water from atmosphere on an adsorption material in a carbon dioxide separator; reversing the adsorption process and desorbing the adsorbed carbon dioxide and water in a temperature-vacuum-variation process wherein heat is introduced into the adsorption material and the pressure around the adsorbent material is lowered; recovering the desorbed water and carbon dioxide; supplying the recovered water to at least one of the carbon dioxide separator, a synthesis plant and the electrolysis device; mixing hydrogen produced by electrolysis of water, recovered water and recovered carbon dioxide to obtain a crude synthesis gas; and feeding the crude synthesis gas to the synthesis plant and carrying out an exothermic methane- or Fischer-Tropsch synthesis or other exothermic hydrocarbon synthesis in the synthesis plant to produce the at least one of gaseous and liquid hydrocarbons; wherein the heat for the desorption of the adsorbed carbon dioxide and water from the adsorption material in the carbon dioxide separator is at least partly derived from the exothermic synthesis in the synthesis plant or from a cooling of the oxygen and hydrogen gas stream from the electrolysis device.

2. The process according to claim 1, wherein the heat is obtained from steam produced in the synthesis process.

3. The process according to claim 1, wherein the electrolysis device is a Solid Oxide Electrolysis Cell (SOEC) operating with regeneratively generated electric energy, and wherein heat obtained from cooling of the oxygen and hydrogen gas stream is used for reversing of the adsorption process.

4. The process according to claim 1, wherein excess and/or not usable residual gas accumulating in the manufacturing process is combusted to produce flue gas and at least one of material and heat energy from the flue gas is used, wherein at least one of heat energy of the flue gas is used to reverse the adsorption process and flue gas is used as the air/gas stream or as an additive in the air-/gas stream.

5. The process according to claim 1, wherein low-temperature waste heat at temperatures below 80? C. is used for regeneration of the adsorbed water in the carbon dioxide separator.

6. The process according to claim 1, wherein a heat pump process is used to transfer heat from the synthesis process, heat energy from combustion of residual gas and heat collected from cooling the oxygen and hydrogen stream produced in the electrolysis devide.

7. The process according to claim 1, wherein the carbon dioxide recovery system is operated continuously, the carbon dioxide requirement of the synthesis process is carried out discontinuously due to variations of available regeneratively generated of electrical power and the carbon dioxide recovered (19, 46, 86) is intermediate stored in a buffer storage.

8. The process according to claim 1, wherein the synthesis process is carried out batchwise due to variations in available regeneratively generated electric energy and the usable heat for desorbing the adsorbed carbon dioxide is temporarily stored in a buffer storage.

9. The process according to claim 1, wherein water desorbed from the adsorption material in the carbon dioxide separator is used for electrolysis.

10. The process according to claim 1, wherein in addition to oxygen and hydrogen also carbon monoxide is recovered from carbon dioxide by means of the electrolysis device operated by regeneratively generated electric energy.

11. The process according to claim 10, wherein the electrolysis device is a steam electrolysis, and wherein the steam is obtained directly from a carbon dioxide-steam mixture taken from the vessel (1) during the desorption of the carbon dioxide without the water vapor being condensed in the meantime.

12. The process according to claim 7, wherein the intermediate buffering of the carbon dioxide occurs in a first buffer and a parallel thereto connected second buffer at a higher pressure, wherein the second buffering takes place via a liquefying of the evolved carbon dioxide.

13. The process according to claim 12, wherein the long-term intermediate buffering takes place via a liquefying of the desorbed carbon dioxide.

14. The process according to claim 1, wherein carbon dioxide from an air/gas stream exhausted from the synthesis plant is adsorbed on the amine-functionalized adsorption material in the carbon dioxide separator.

15. A process for the synthesis at least one of gaseous and liquid hydrocarbons, the method comprising the steps: producing an oxygen and hydrogen gas stream by electrolysis of water in an electrolysis device; adsorbing carbon dioxide (19, 46, 86) and water from atmosphere on an amine-functionalized adsorption material in a carbon dioxide separator; reversing the adsorption process and desorbing the adsorbed carbon dioxide and water in a temperature-vacuum-variation process wherein heat is introduced into the adsorption material and the pressure around the adsorbent material is lowered; recovering the desorbed water and carbon dioxide; supplying the recovered water to at least one of the carbon dioxide separator, a synthesis plant and the electrolysis device; mixing hydrogen produced by electrolysis of water, recovered water and recovered carbon dioxide to obtain a crude synthesis gas; and feeding the crude synthesis gas to the synthesis plant and carrying out an exothermic methane- or Fischer-Tropsch synthesis or other exothermic hydrocarbon synthesis in the synthesis plant to produce the at least one of gaseous and liquid hydrocarbons; wherein the heat for the desorption of the adsorbed carbon dioxide and water from the adsorption material in the carbon dioxide separator is at least partly derived from the exothermic synthesis in the synthesis plant or from a cooling of the oxygen and hydrogen gas stream from the electrolysis device.

Description

(1) Embodiments of the invention will be described in detail with reference to the accompanying drawings in the description of the figures, which are intended to illustrate the invention and are not to be regarded as limiting:

(2) In the drawings there is shown in:

(3) FIG. 1 a schematic representation of one embodiment of a carbon dioxide recovery system part;

(4) FIG. 2 a schematic representation of one embodiment of a methane production plant part;

(5) FIG. 3 a schematic representation of one embodiment of a synthesis plant part by means of Fischer-Tropsch synthesis;

(6) FIG. 4 a schematic representation of an embodiment of a steam electrolysis based on a SOEC (Solid Oxide Electrolysis Cell);

(7) FIG. 5 a schematic representation of the regeneration operation of one embodiment;

(8) FIG. 6 a schematic representation of an embodiment of a co-electrolysis for Fischer-Tropsch synthesis,

(9) FIG. 7 a schematic representation of another embodiment of a co-electrolysis for methane production, and

(10) FIGS. 8 to 13 diagrams showing system parameters, namely, position of the valves, status of the compressors, pressure in the containers, excess amount of steam, pressure in Ruth buffer and amount of energy stored in Ruth buffer in Another Embodiment.

(11) It should be noted at this point that the overall system consists of the carbon dioxide recovery system part (FIG. 1) and the plant part for methanation (FIG. 2) or synthesizing (FIG. 3). The water vapor electrolysis unit (FIG. 4) can be used both in the methanation plant section (FIG. 2) and in the synthesizing plant part with Fischer-Tropsch synthesis (FIG. 3).

(12) In FIG. 1 is a schematic representation of an embodiment of a carbon dioxide recovery system part (FIG. 1).

(13) The carbon dioxide recovery system part (FIG. 1) is used for the recovery of carbon dioxide 19 from the ambient air or a gas stream and provides, if needed, also condensed water 20 from the ambient air or a gas stream for further material use. For this, a carbon dioxide recovery system part is selected, which initially binds carbon dioxide via an adsorption operation from the air flow and subsequently releases the carbon dioxide by a temperature-vacuum-variation processes for further use.

(14) Adsorption Operation:

(15) Ambient air 3 is sucked by blower 2 through a vessel 1 filled with adsorbent material. The ambient air usually contains 0.04 Vol.-% carbon dioxide and, depending on the climate, a certain amount of water vapor. The carbon dioxide is enriched to a high proportion on the surface of the adsorbent material, which is preferably functionalized with amine groups. Further, water accumulates on the surface of the adsorption material, wherein usually at least 2 moles of water per 1 mole of carbon dioxide, but at a minimum at least 1 mole per 1 mole of carbon dioxide, is adsorbed.

(16) Regeneration operation by means of temperature-vacuum-variation method:

(17) If the surface of the adsorber 1 is saturated or enriched with carbon dioxide, it must be regenerated.

(18) First, vessel 1 is evacuated to a pressure of 20-400 mbar.sub.abs, and subsequently heating fluid 11 is pumped out of heating medium container 10 at a temperature of 20-120? C. by means of heating pump 12 through a heat exchanger 13.

(19) In the heat exchanger 13 the heating fluid 11 is heated by an external heat source 14 (the heat according to the invention comes from the parts according to FIG. 2 or FIG. 3 or FIG. 4) to 80-130? C. Subsequently, the heating fluid enters the vessel 1, where it transfers heat to the adsorption material via the heat exchanger surfaces 4. As a result of the transfer of heat, the bound carbon dioxide and water is desorbed and sucked out of the vessel 1 by means of liquid ring compressor 15.

(20) The cooled heating fluid 11 runs back into the heating medium container 10, from which it can be fed again to the process.

(21) The hot extracted mixture of carbon dioxide and water vapor is cooled in a cooler (e.g. cooling tower 16) and passes through the liquid ring compressor 15, into which cold condensate 17 is introduced in order to improve the suction effect and for further cooling, into the separation vessel 18.

(22) In the separation vessel 18, the carbon dioxide 19 is separated from the condensate 17/20, which originates from the atmospheric humidity and was also deposited on the adsorber material, by gravity. A portion of the condensate, after cooling with coolant 21 in the cooler 22, is fed to the liquid ring compressor. The excess condensate 20 is discharged after the separation vessel 18.

(23) The highly concentrated carbon dioxide 19 is supplied for further use to the plant parts shown in FIG. 2 or FIG. 3.

(24) After the regeneration process the heat transfer surfaces 4 are flowed-through by a coolant.

(25) The coolant 5 absorbs the sensible heat of the adsorption material and the vessel 1 and removes it from vessel 1. The heated coolant subsequently passes into a cooling tower 6, where the heat absorbed is released back into the environment. To improve the cooling effect, in particular at high ambient temperatures, water 7 in the cooling tower can be atomized onto the heat exchanger surfaces of the cooling tower, where it evaporates.

(26) The cold coolant 5 is collected in a coolant tank 8 and from there is returned to the adsorber tank 1 by means of a coolant pump 9.

(27) After the cooling of the vessel 1 and the adsorbing material below a temperature of maximum 50? C. tank 1 is ventilated and the adsorption process can be started anew.

(28) Alternative regeneration operation by means of temperature-vacuum-variation processes for the decoupling of waste heat both in the temperature range 80-130? C. and in the temperature range 50-90? C.:

(29) If the surface of the adsorber 1 is saturated or enriched with carbon dioxide, it must be regenerated.

(30) First vessel 1 is evacuated to a pressure of 20-400 mbar.sub.abs, then from the 10 Heating medium container heating fluid 11 by means of heating pump 12 through a heat exchanger pumped.

(31) First, vessel 1 is evacuated to a pressure of 20-400 mbar.sub.abs, and subsequently heating fluid 11 having a temperature of 20-50? C. is pumped out of heating medium container 10 by means of heating pump 12 through an additional heat exchanger which is arranged in series with the heat exchanger 13/14.

(32) In the serially-connected additional heat exchanger, the heating fluid 11 is heated to 45-85? C. by an external heat source, wherein the heat originates according to the invention from the parts according to FIG. 2 or FIG. 3 or FIG. 4. Subsequently, the heating fluid enters the vessel 1, where it delivers heat to the adsorption material via the heat exchanger surfaces 4. As a result of the supply of heat a part of the adsorbed water and part of the adsorbed CO.sub.2 is desorbed (and typically in the specified temperature range, the desorption of water takes place in preference to CO.sub.2 desorption) and is extracted from the vessel 1 by a liquid ring compressor 15.

(33) The cooled heating fluid 11 flows back into the heating medium container 10 from which it can be recycled back into the process.

(34) Subsequently, heating fluid 11 is pumped at a temperature of 70-120? C. from the heating medium container 10 by means of heating pump 12 through the heat exchanger 13.

(35) In the heat exchanger 13, the heating fluid 11 is heated to 80-130? C. by an external heat source 14 (the heat according to the invention coming from the parts according to FIG. 2 or FIG. 3 or FIG. 4). Subsequently, the heating fluid enters the vessel 1, where it delivers heat to the adsorption material via the heat exchanger surfaces 4. By the heat supply, especially carbon dioxide is desorbed and sucked out of the vessel 1 by means of liquid ring compressor 15.

(36) The cooled heating fluid 11 flows back into the heating medium container 10 from which it can be recycled back into the process.

(37) The hot extracted carbon dioxide is cooled in the cooling tower 16 and passes into the separation vessel 18 via the liquid ring compressor 15 into which cold condensate 17 is added to improve the suction effect and for further cooling.

(38) In the separation vessel 18, the carbon dioxide 19 is separated by gravity from the condensate 17/20, which originated from the atmospheric humidity and was also deposited on the adsorber material. A portion of the condensate, after cooling with coolant 21 in the cooler 22, is fed to the liquid ring compressor. The excess condensate 20 is discharged after the separation vessel 18.

(39) The highly concentrated carbon dioxide 19 is supplied for further use in the plant parts shown in FIG. 2 or FIG. 3.

(40) After the regeneration process the heat transfer surfaces 4 are flowed through by a coolant. The coolant 5 absorbs the sensitive heat of the adsorption material and the vessel 1 and removes it from vessel 1. The heated coolant subsequently passes into a cooling tower 6, where the absorbed heat is released to the environment again. To improve the cooling effect, in particular at high ambient temperatures, water 7 in the cooling tower can be atomized onto the heat exchanger surfaces of the cooling tower, where it evaporates.

(41) The cold coolant 5 is collected in a coolant tank 8 and from there is returned to the adsorber tank 1 by means of a coolant pump 9.

(42) After the cooling of the vessel 1 and the adsorbing material below a temperature of maximum 50? C. vessel 1 is ventilated and the adsorption process can be started again.

(43) Carbon dioxide preparation for subsequent use in a methaneor Fischer-Tropsch synthesis or other suitable hydrocarbon synthesis:

(44) By the required regeneration of the adsorption material a continuous separation of carbon dioxide from the air can take place. However, a parallel connection of several adsorption vessels 1 and the associated cooling and heating circuits and a time-staggered operation enable very probably the transformation of the discontinuous process into a quasi-continuous process, so that this embodiment represents a particularly preferred embodiment.

(45) The carbon dioxide 19 recovered quasi-continuously at ambient pressure from the CO.sub.2 preparation process is compressed by a compressor 23, with a subsequent gas cooling 24 for discharging the compressor heat, to a pressure which is higher than the pressure in the subsequent synthesis plants, and then stored in a gas buffer 25.

(46) The water condensate 26 accumulated as a result of cooling is removed via a condensate trap 27 from the gas buffer 25.

(47) The control valve 29 serves to control the pressure in the vessel 18, which depends on the quantity of CO.sub.2 discharged from the compressor 23.

(48) If the compressor 23 takes less CO.sub.2 from the vessel 18 than is produced in the CO.sub.2-production, the control valve 29 opens and releases the excess CO.sub.2 quantity to the atmosphere or to another intermediate storage, for example a gas bag.

(49) If the compressor 23 takes more CO.sub.2 than is produced, initially the control valve 29 closes, subsequently the transport capacity of the compressor 23 is reduced further, so that the pressure in the tank 18 remains constant at a predetermined value.

(50) If the tank pressure 28 has reached its maximum permissible value, then the compressor 23 is turned off.

(51) The removal of carbon dioxide from the container 25 occurs via the control valve 30, which maintains the pressure in the subsequent synthesis plant constant at a predetermined value.

(52) If the pressure in the container 25 is below a permissible value, which must be higher than the pressure in the subsequent synthesis plant, the compressor 23 switches on again and fills the gas buffer 25.

(53) The difference between the buffer pressure and extraction pressure, the buffer volume and the required CO.sub.2 quantity per unit time are determined by the time that can be bridged with the buffer.

(54) Since the additional pressure increase for gas buffering costs additional compression energy over the required operating pressure of the synthesis plant addition, this should not be too high for economic reasons.

(55) That means that longer bridging or transitory period times are determined mainly by the buffer volume. Since this is limited, a buffer with a low excess pressure is only suitable as a short-term back-up to compensate for short-term pressure fluctuations.

(56) In order to ensure a higher CO.sub.2 hedge for longer periods of time, it is proposed to build, in parallel with the short-time buffer 25, a long term buffer 31, which operates at a higher pressure.

(57) This long-term buffer 31, connected to the compressor 32 and the subsequent condenser 33 for condensation of the moisture in the gas which is removed as condensate 34 through the condensate trap 35 from the container 31, is filled with CO.sub.2 from the container 25 to a pressure well above the operating pressure of the synthesis plant and the maximum pressure of the container 25.

(58) The compressor 32 is only operated when the container 25 has already reached its maximum pressure. In this case, the capacity of the compressor 23 is not reduced, but operated together with the compressor 32 with rated power. Once the container 31 has reached the maximum pressure 36, the compressor 32 is turned off and the power of the compressor 23 is reduced according to the consumption in the synthesis plant.

(59) In times of an increased CO.sub.2-requirement in the synthesis plant, the carbon dioxide from the container 25 is first removed through the control valve 30. If the pressure in the container dropped below the operating pressure of the synthesis plant, that is, the container 25 is empty, the control valve 37 opens and the synthesis plant is supplied with CO.sub.2 from the long term buffer 31.

(60) In the case of reduction of the CO.sub.2-requirement in the first synthesis plant the control valve 37 closes, the pressure 28 in the container 25 rises up to the maximum allowable value. Subsequently, the compressor 32 starts and fills the buffer 31 to the maximum pressure value 36, whereupon the compressor 32 shuts down. Upon further oversupply of CO.sub.2, finally, the pumping capacity of the compressor 23 is reduced.

(61) A further increase the buffer amount of CO.sub.2 is possible when the CO.sub.2 is liquefied and stored in liquid form. Due to the higher density, a higher amount of CO.sub.2 is thus stored for the same volume.

(62) The liquid storage is a special case of long-term buffer and is not specifically discussed in detail, however, this configuration is of great importance.

(63) FIG. 2 shows a schematic representation of an embodiment of a methane production system part.

(64) The production of methane from carbon dioxide and hydrogen, produced with electrolysis using regeneratively generated of electrical energy, is carried out according to the reaction by Sabatier:
CO.sub.2+4H.sub.2.fwdarw.CH.sub.4+2H.sub.2O?H.sub.R=?165 kJ/molR1

(65) Deionized water 40 is separated into oxygen 43 and hydrogen 44 in an electrolysis apparatus 41 with regeneratively produced electrical energy 42. Oxygen 43 is transferred for use or if unused is discharged to the environment.

(66) The hydrogen 44 is compressed in a compressor 45 to process pressure, and is mixed with carbon dioxide 46, which is already available at process pressure, and is supplied as a mixed gas 47 to a synthesis reactor 48.

(67) The synthesis reactor 48 is filled with a sufficient quantity of a suitable catalyst 49 and, as the Sabatier reaction is exothermic, is cooled with boiling water loop 50.

(68) The cooling temperature and thus also the boiling water pressure are chosen such that a high conversion of carbon dioxide to methane takes place.

(69) This high turnover is usually achieved when the reaction gas 51 leaves the reactor 48 at a temperature of about 250 to 300? C.

(70) After the reactor 48, the reaction gas is preferably cooled to low temperatures, in order to separate the water of reaction from the gas mixture. The cooling initially takes place in a heat exchanger 52 in which the cold feed water is preheated. The required low temperatures are ultimately achieved in a cooler 53 operated with coolant.

(71) The cold gas mixture 54 passes into a separator 55, in which the reaction water 56 is separated from the methane-rich gas 57.

(72) The generated methane 57 is supplied to the desired further use.

(73) The boiling water 50 used for cooling is removed from the steam drum 58 and via pump 59 is supplied to reactor 48 for removing heat of reaction. The circulating amount of boiling water 50 was selected so that only a small part of the boiling water evaporates due to the heat absorption. The steamy boiling water leaving the reactor enters the steam drum 58, in which the separation between boiling water and saturated steam takes place. The saturated steam 61 is pressure controlled and removed from the steam drum 58 and supplied to a use, for example a heat sink 62. The steam condensate returned from the heat recovery is compressed by pump 64, preheated in the heat exchanger 52, and returned back into the steam drum 58. Possible loss of steam condensate 65 can be replaced by a new feed water 66.

(74) According to the invention, the carbon dioxide 19 separated from the air 3 in the CO.sub.2-producing plant part (FIG. 1) as carbon dioxide 46 for the production of methane 57 (FIG. 2), or as carbon dioxide 86 is employed for the production of liquid hydrocarbons (114, 115, 116, 117) (FIG. 3) with the aid of hydrogen 44 or 84, produced in a water electrolysis 41 or 81 by means of regeneratively generated electric energy (42, 82). Furthermore, steam 61 or 122 resulting in the synthesis process (FIG. 2 and FIG. 3) is used as a heat source 14 for the desorption of carbon dioxide deposited on the adsorbent material.

(75) Heat storage for storing heat from the synthesis process (see FIG. 2 and FIG. 3):

(76) The description is made on the basis of the example of methane synthesis according to FIG. 2. The steam storage in the synthesis of liquid hydrocarbons of FIG. 3 is analogous to the steam storage in the methane synthesis.

(77) The steam pressure 61 evolved discontinuously in the synthesis plant is used as a heat source 14 for the desorption of the carbon dioxide accumulated in the adsorber.

(78) Due to the discontinuous operation of the synthesis plant (FIG. 2/3) because of the different availability of the regeneratively generated electrical energy, occasionally temporarily an excess of steam occurs, which cannot be used in the desorption (FIG. 1). At other times, in which the synthesis plant (FIG. 2/3) is operated with lower load, insufficient steam is available to supply the heat for the desorption (FIG. 1).

(79) To even out the heat supply for desorption, steam pressure 61 accruing discontinuously in the synthesis plant (FIG. 2/3) is therefore stored in a heat accumulator 67. The heat storage unit 67 is for example a boiling water filled variable pressure buffer (Ruth buffer). Other suitable heat storages include layer storage, molten salt storage and thermochemical storage.

(80) During the charging process the excess pressure steam 68 generated in the synthesis is passed through the valve 69 into the buffer 67. The remaining steam 70 is reduced via the throttle valve 71 to the pressure 72 and is used as heating steam 73 for heating the heating medium 11 in the heat exchanger 13. At the beginning of the charging process boiling water and saturated steam are in the buffer 67 at the steam output pressure 72. Due to the supply of pressurized steam 68 the boiling water in the tank 67 is heated and the pressure in the container increases. The maximum possible pressure corresponds to the pressure of the supplied pressure steam 68. Due to the increase in pressure the steam portion is reduced and the water content increased in the container. The supplied heat is stored in the form of boiling water.

(81) If there is a deficiency of heat for the CO.sub.2 desorption, because the synthesis plant (FIG. 2/3) directly provides too little steam, the throttle valve 74 is opened and the desired difference in amount of steam 75 removed from the heat accumulator 67. Due to the withdrawal of steam, the pressure in the container 67 drops, and water in the boiling water tank is evaporated. A steam removal is possible up to the pressure 72. After discharging steam, the heat accumulator can be recharged.

(82) The steam condensate 76 accumulating in the heat exchanger 13 is returned as feed water 63 back into the synthesis process.

(83) Equipment for the generation of methane (FIG. 2) and liquid hydrocarbons (FIG. 3) from carbon dioxide and hydrogen, produced by regeneratively generated electric energy, are typically used as electric energy storage and are powered with regeneratively generated electric energy, which is superfluous to the power grid system, i.e., which would result, when not in use, for uneconomic isolation or even shutdown of conventional power generators.

(84) In FIG. 3 a schematic representation of an embodiment of a synthesis plant part by means of Fischer-Tropsch synthesis is shown.

(85) For the production of liquid hydrocarbons from carbon dioxide and hydrogen, produced in an electrolysis using regeneratively generated electric energy, a Fischer-Tropsch synthesis (FIG. 3) is used.

(86) The conversion of carbon dioxide and hydrogen to hydrocarbons is carried out in two steps: Step 1: reverse water-gas shift reaction for producing carbon monoxide containing synthesis gas
CO.sub.2+H.sub.2.fwdarw.CO+H.sub.2O ?H.sub.R=+41.2 kJ/molR2 Step 2: for example, Fischer-Tropsch synthesis for the creation of liquid hydrocarbons
CO+2H.sub.2.fwdarw.CH.sub.2+H.sub.2O ?H.sub.R=?156.5 kJ/molR3

(87) To increase the product yield a part can of light gaseous hydrocarbon from the Fischer-Tropsch synthesis can be worked up over a reform process back to synthesis gas and recycled back into the Fischer-Tropsch process:
CH.sub.2+H.sub.2O.fwdarw.CO+2H.sub.2 ?H.sub.R=+156.5 kJ/molR4

(88) The reactions R2 and R4 are run in parallel in reactor.

(89) Deionized water 80 is decomposed into oxygen 83 and hydrogen 84 in an electrolysis apparatus 81 using regeneratively generated electric energy 82. Oxygen 83 is supplied to a use, or is discharged unused to the environment.

(90) The hydrogen 84 is compressed in a compressor 85 to process pressure, and together with carbon dioxide 86, which is already available at process pressure, as well as hydrocarbon-containing residual gases 89 recirculated by means of compressor 88 from the Fischer-Tropsch synthesis to a process 87 for performing the reverse water gas shift reaction (R2) and the reforming (R4).

(91) The process heat required for both endothermic reactions is provided by means regeneratively generated electric energy 90.

(92) The process 87 leaves the synthesis gas 91 with the required hydrogen-carbon monoxide molar ratio for the Fischer-Tropsch process. The excess reaction water separated by cooling 92 is discharged as a condensate 93 from the process.

(93) The synthesis gas 91 is mixed with the recycle gas 95 back compressed in compressor 94 and fed to the Fischer-Tropsch reactor 96.

(94) The Fischer-Tropsch reactor 96 is filled with a suitable catalyst 97 in sufficient quantity and, as the synthesis reaction R3 is exothermic, cooled with a boiling water circulation loop 98.

(95) The cooling temperature and hence also the boiling water pressure are selected such that, depending on the selected catalyst, the conversion of carbon monoxide and hydrogen results in the desired product.

(96) This desired product is generally achieved with the use of cobalt catalysts when the reaction product 99 leaves the reactor 96 with a temperature of about 220? C. The reaction product 99 is a mixture of reaction gas and long-chain, liquid hydrocarbons with a high number of carbon atoms. This mixture is separated in the high temperature separator 100 into liquid hydrocarbons 101 and hydrocarbon-containing gas 102.

(97) The gas is further cooled in the cooler 103 and separated by gravity in separation vessel 104 into water of reaction 105, liquid hydrocarbons 106 and residual gas 107. The cooling and separation can take place in several cooling stages.

(98) A portion 95 of the residual gas 107, used to increase the carbon monoxide conversion in the Fischer-Tropsch synthesis, is recompressed by compressor 94 and fed back again with the synthesis gas 91 to the reactor 96.

(99) In order to avoid a too high accumulation of reaction gas constituents not participating in the Fischer-Tropsch (CO.sub.2, CH.sub.4, C.sub.2 . . . , N.sub.2), a partial stream of gas 108 must be removed from the Fischer-Tropsch process.

(100) This part stream 108 can either be burned as the gas 109 in a combustion device 110 with air 111 making the flue gas 112, which is emitted to the environment, or partly re-compressed with the compressor 88 and supplied as a stream 89 to the process 87 for the reprocessing of the hydrocarbons to synthesis gas. Also in this case is to avoid nitrogen accumulation in the overall process a partial stream is combusted in the combustion device 110.

(101) The liquid hydrocarbons 101 and 106 separated in the Fischer-Tropsch process pass into a single or multi-stage product preparation 113, in which the hydrocarbons are processed into finished products having different properties. End products are for example wax 114, diesel 115, naphtha 116 and light hydrocarbon gases 117.

(102) The residual gases 118 accumulating in the product preparation 113 are burned in the combustion device 110 with air 111 together with the residual gas 109 forming flue gas 112, which typically is discharged to the environment. However, this flue gas 112 from the combustion of residual gas is used in the plant for the production of liquid hydrocarbons (FIG. 3) as a heat source 14 for the desorption and as air substitute 3 with higher carbon dioxide content or for admixing with the air to increase their CO.sub.2 content in the CO.sub.2-production (FIG. 1).

(103) The boiling water 98 used for cooling of the reactor 96 is removed from the steam drum 119 and supplied by pump 120 to the reactor 96 for removing the heat of reaction. The circulating amount of boiling water 98 was selected so that only a small part of the boiling water evaporates due to the heat absorption.

(104) The steamy boiling water 121 leaving the reactor enters the steam drum 119, wherein the separation between boiling water and saturated steam occurs.

(105) The pressure adjusted saturated steam 122 is discharged from the steam drum 119 and used, for example, supplied to a heat sink 123.

(106) The steam condensate 124 returned from the heat recovery is increased in pressure by pump 125 and resupplied to the steam drum 119.

(107) Possibly occurring steam condensate loss 126 can be replaced by a new feedwater 127.

(108) Further, in FIG. 3 utilization of heat and CO.sub.2 from the excess gas burner of a Fischer-Tropsch synthesis plant can be seen.

(109) The flue gas 112 originating from the combustion of the residual gases 109 from the Fischer-Tropsch synthesis and light hydrocarbons 118 from the product treatment with air 111 is used as material and/or energy in the CO.sub.2-producing (FIG. 1), since it was determined that this flue gas 112 can be used as the CO.sub.2 source. Further, it was recognized that the thermal energy of the flue gases 112 can be used for the desorption process. For this purpose, the flue gas 112 is passed through a heat exchanger 128, which makes available heat 129 as heat for the CO.sub.2 producing process via a heat transport circuit 14. The cooled flue gas 130 is further cooled in cooler 131 and supplied to the separation vessel 132, in that the condensed water of combustion is separated as waste water 133 from the gas stream 134. The gas stream 134 still contains carbon dioxide in addition to nitrogen and oxygen from the combustion air 111. Since the CO.sub.2 concentration is substantially higher in the gas 134 than in the ambient air, this can be mixed into the air supply in the CO.sub.2 production plant, and thus the CO.sub.2 extraction from this mixture occurs in the CO.sub.2 production plant more quickly and with less energy expenditure, respectively.

(110) FIG. 4 shows a schematic representation of an embodiment of a steam electrolysis based on a SOEC (Solid Oxide Electrolysis Cell).

(111) For the production of hydrogen 150 in a water vapor electrolysis 151 based on a SOEC (Solid Oxide Electrolysis Cell) water vapor 152 is recuperatively preheated by the hot product gases oxygen and hydrogen and at high temperatures, with the help of regeneratively generated electric energy 153, is decomposed into oxygen 154 and hydrogen 150.

(112) The not recuperative usable heat is extracted from the hydrogen stream 157 and 158, as well as from the oxygen stream, with coolant 155 and 156.

(113) If in the synthesis (FIG. 2 or FIG. 3) instead of a water electrolyzer (41, 81) a water vapor electrolyzer (FIG. 4) is used, then a fraction of the excess heat 155, 156, and 157 and 158 from the product gas cooling of the water vapor electrolysis 151 should be used as a heat source 14 for desorption of carbon dioxide.

(114) Furthermore, heat storage for storing heat from the steam electrolysis is provided.

(115) If a water vapor electrolysis 41 or 81 is used to produce hydrogen 44 and 84 instead of a water electrolyzer 151, generally the entire steam 61 or 122 generated in the synthesis is used in for the generation of hydrogen. Thus no or only a smaller proportion of the steam is available for heat supply for the CO.sub.2 desorption.

(116) In this case, part of the heat flow 158 or 156 extracted from the water vapor electrolysis for the final cooling of the oxygen 154 and the hydrogen 150 can be used as the heat supply 14 for CO.sub.2 desorption.

(117) Co-Electrolysis for Fischer-Tropsch Synthesis According to FIG. 3 and FIG. 6:

(118) To produce a carbon monoxide and hydrogen-containing synthesis gas 91 from carbon dioxide 86, water 80 or water vapor 152 (corresponding to FIG. 4) and residual gas 89 then instead of the water electrolysis 81 or water vapor electrolysis 151 (corresponding to FIG. 4) and the RWGS/reforming process 87 a co-electrolysis (Co-SOC) 159 (corresponding to FIG. 6) are used, based on a Solid Oxide Electrolysis Cell (SOEC), in which regeneratively generated electric energy 153 is used to convert water vapor and carbon dioxide of a steam-carbon dioxide mixture 160 into hydrogen and carbon monoxide containing synthesis gas 91 and oxygen 161.
H.sub.2O.sub.D.fwdarw.H.sub.2+0.5O.sub.2 ?H.sub.R=241.8 kJ/mol
CO.sub.2.fwdarw.CO+0.5O.sub.2 ?H.sub.R=283.0 kJ/mol

(119) By the high temperature in the co-electrolysis 159 of approximately 850? C. also the residual gas 89, which contains, in addition to hydrogen and carbon monoxide unreacted in the synthesis, also methane and other non-condensable hydrocarbons, especially by reforming the hydrocarbons with water vapor is worked up to synthesis gas.
C.sub.xH.sub.y+xH.sub.2O.fwdarw.xCO+(0.5y+x)H.sub.2

(120) To provide the steam-carbon dioxide mixture 160 for co-electrolysis 159 there may be used, for example, carbon dioxide 86 from the CO.sub.2 production unit described in FIG. 1 and water vapor 73 (corresponding to FIG. 3) according to the state of the art of the synthesis cooling (for example, from the document EP 2491998 A1). Therewith however no steam would remain available for the provision of heat in the heat exchanger 13 of the CO.sub.2 production unit.

(121) It is therefore proposed in accordance with FIG. 5, that in the regeneration operation, by means of a suitable vacuum pump 168, the from the vessel 1 drawn off hot carbon dioxide water vapor mixture with a water vapor content, depending on the relative air humidity of the respectively previous CO.sub.2 adsorption, of 0.5 to 10, in particular 2 to 5 kmol per kmol carbon dioxide in the condenser 16 is only cooled to the extent, that so much water vapor remains in the hydrocarbon stream 19, as required for the subsequent co-electrolysis 159 (corresponding to FIG. 6) for producing a synthesis gas 91 with the mole ratio required a for the synthesis of H.sub.2CO.

(122) The vacuum pump 168 has to compress the gas 169 present after cooler 16, saturated with water vapor, without condensation during the entire concentration process. Intercooling is permitted here only to the extent, that this does not lead to a condensing out of water. In a related embodiment even an overheating of the steam-containing gas by the compression process is desirable and advantageous, so that after the vacuum pump 168 in the buffer 170 and the piping up to the co-electrolysis 159 (FIG. 6) condensation is less liable to occur due to heat losses.

(123) In a corresponding alternative embodiment, an at least partially intermediate cooling could well take place by means of a two-stage pumping arrangement.

(124) Insulation and possibly accessory heating of the equipment to a temperature greater than the dew point of the steam-carbon dioxide mixture is advantageous in order to avoid condensation up to co-electrolysis.

(125) Suitable vacuum pumps are, for example, dry-running (uncooled) reciprocating compressors and screw compressors.

(126) Since the carbon dioxide-water vapor mixture 171 after the cooling in the cooler 16 is at the dew point, as a reference variable for controlling the water vapor content in the carbon dioxide, the temperature 162 depending on the pressure 163 in the gas mixture is used.

(127) TABLE-US-00001 At the dew p.sub.D = p.sub.s(t) point applies: p.sub.D + p.sub.CO2 = p.sub.tot r.sub.D = p.sub.D/p.sub.tot with p.sub.D partial pressure of steam in the gas mixture p.sub.s(t) boiling pressure of steam at the temperature .sup.f.sub.D molar proportion or space proportion of steam in the gas mixture p.sub.CO2 partial pressure of CO.sub.2 in the gas mixture p.sub.tot total pressure

(128) There is regulated, for example, the amount of carbon dioxide-water vapor guided through a three-way valve 164 to the cooler 16 and/or the cooling performance of the cooler.

(129) In this case, the water 172 condensed out in the condenser 16 must be removed from the gas stream 171 separated via a condensate lock system 173 ahead of the vacuum pump 168.

(130) Possibly existing superheat in the gas 19 after the vacuum pump 168 can, by injection of externally preheated water 174, be used to further saturate the CO.sub.2 with water vapor. As control variables for the amount of water, there may be used the temperature 175 and the pressure 176. Excess water 177 is removed from the vessel 170 via the trap 178.

(131) If steam for the co-electrolysis is insufficient, because it cannot be covered completely through the water vapor content in the carbon dioxide 19 and possibly by externally preheated water 174, then addition steam 166 must be supplied from an external source to the co-electrolysis 159.

(132) In an alternative embodiment of the carbon dioxide producing unit, the regenerating operation can be performed by flushing the vessel 1 with steam, either with or without simultaneously applied vacuum. In this case also there results a carbon dioxide-water vapor mixture, which can be suctioned from the vessel 1 and which can be cooled in the cooler 16 to the extent, that there is still included in the carbon dioxide stream 19 as much steam as required for the subsequent co-electrolysis 159 (corresponding to FIG. 6) for producing a synthesis gas 91 with a H.sub.2CO mole ratio as required for the synthesis.

(133) Co-Electrolysis for Methane Production (FIG. 2 and FIG. 7):

(134) In FIG. 7 there is shown a co-electrolysis 159 to produce a CO- and H.sub.2-containing synthesis gas 167 and oxygen 161 from a H.sub.2OCO.sub.2 mixture 160 from the CO.sub.2 production using regeneratively generated electric energy 153.

(135) In contrast to FIG. 2, where carbon dioxide 46 and hydrogen 44 from electrolysis 41 are used for production of methane according to the reaction 57
CO.sub.2+4H.sub.2.fwdarw.CH.sub.4+2H.sub.2O ?H.sub.R=?165.1 kJ/mol
in FIG. 7 the conversion of carbon monoxide and hydrogen from the synthesis gas 167 takes place according to the reaction to methane:
CO+3H.sub.2.fwdarw.CH.sub.4+H.sub.2O ?H.sub.R=?206.2 kJ/mol

(136) The production of methane from carbon monoxide and hydrogen is prior art.

(137) Overall, the present invention provides further advantages, namely:

(138) By reducing the cooling of the desorbed carbon dioxide and thereby maintaining the water vapor from the air humidity in the carbon dioxide of the CO.sub.2-production plant, a part of the heat used for desorption of carbon dioxide and water (evaporation) can remain mainly in the form of water vapor and be used for generation of hydrogen together with carbon monoxide from carbon dioxide in a co-electrolysis on SOEC basis.

(139) It is in this case, through the cooling of accumulated waste water (condensate) and the use of additional water, the production of hydrogen in the electrolysis is avoided.

(140) Furthermore, additional heat for evaporation of water in a water electrolysis, which requires application of electric energy, or for the external vaporization of water before a steam electrolysis is saved, whereby the efficiency of the overall process increases.

(141) The use of a co-electrolysis instead of electrolysis and a RWGS process for producing synthesis gas reduces the necessary process steps for the production of synthesis gas to an electrolysis step, resulting in savings on equipment and so reduces investment costs.

(142) By the in situ generation of the synthesis gas components CO and H.sub.2 in the co-electrolysis at one temperature intermediate coolings are avoided and heat losses are reduced, resulting in the increase in efficiency of synthesis gas production and further increasing the efficiency of the overall process and thus reducing operating costs.

ANOTHER EMBODIMENT

(143) In the following the description of the invention occurs with reference to a specific embodiment with reference to the diagrams shown in FIGS. 8 to 13 and the above-explained FIGS. 1 to 4:

(144) A plant for production of carbon dioxide from the ambient air is to be coupled with a plant for the production of methane from carbon dioxide and hydrogen produced by water electrolysis and regeneratively generated electricity.

(145) The CO.sub.2 recovery plant has an annual capacity of 1,000 t CO.sub.2/a, which corresponds, given an annual use of the facility of 8,000 hours, to a yield of 125 kg CO.sub.2/h.

(146) The CO.sub.2-requirement of the methanation plant fluctuates depending upon access of regenerative produced excess electric energy in the electrical energy distribution network between 50 kg CO.sub.2/h and 175 kg CO.sub.2/h.

(147) To balance the load fluctuations two CO.sub.2-pressure buffers and one Ruth buffer are employed for storage of the steam from the synthesis.

(148) The sizes of the buffer are:

(149) TABLE-US-00002 CO.sub.2-buffer (25): 10 m.sup.3 working pressure: 20 . . . 25 bara CO.sub.2-buffer (31): 10 m.sup.3 working pressure: 20 . . . 50 bara Ruth buffer (67): 12.7 m.sup.3 working pressure: 2 . . . 25 bara

(150) The system parameters, namely, position of the valves 29, 30, 37, status of the compressors 23 and 32, pressure in the containers 25 and 31, excess amount of steam, pressure in Ruth buffer 67 and amount of energy stored in Ruth buffer 67 are shown in the diagrams shown in FIGS. 8 to 13 as a function of time.

(151) In the nominal load case both systems (125 kg CO.sub.2/h), the steam demand of the CO.sub.2-production plant is 338 kg/h and the steam output of the methane generation system is 243 kg/h, that is, methane production system can cover only about 72% of the steam demand of the CO.sub.2-production plant.

(152) In the following it is assumed that a constant basic supply of steam for the CO.sub.2-production plant of 95 kg/h is performed by a third party. Therewith, at the nominal load of both systems, the supplemental steam out of the methane production covers steam requirement for the CO.sub.2 generation.

(153) At time 0, both plants work in the rated load operation (125 kg CO.sub.2/h). The state of the system is:

(154) TABLE-US-00003 produced CO.sub.2 quantity CO.sub.2-generating plant: 125 kg/h CO.sub.2 consumption methane generation plant: 125 kg/h position of the valves 29: closed 30: open 37: closed state of compressors 23: in operation 32: not in operation pressure in the containers 25: 25 bara 31: 50 bara excess steam: 0 kg/h pressure in Ruth storage tank 67: 2 bara energy stored in Ruth buffer 67: 1,060.5 kWh

(155) The gas buffers 25 and 31 are both loaded. The produced CO.sub.2 is quasi being pushed through container 25 with the compressor 23 and made available for methanation (FIG. 2).

(156) The pressure in Ruth buffer has dropped to delivery pressure. The steam generated in the methanation is immediately made available for CO.sub.2 production and therewith covers the current steam demand.

(157) From time 0 to time 1 for 2.38 hours the yield of the methanation is raised to 175 kilograms CO.sub.2/h.

(158) The state of the system is:

(159) TABLE-US-00004 produced CO.sub.2 quantity CO.sub.2-generating plant: 125 kg/h CO.sub.2 consumption methane generation plant: 175 kg/h position of the valves 29: closed 30: open 37: closed state of compressors 23: in operation 32: not in operation pressure in the containers 25: 20 bara 31: 50 bara excess steam: 97.2 kg/h pressure in Ruth storage tank 67: 3.23 bara energy stored in Ruth buffer 67: 1,240.5 kWh

(160) The pressure in the gas buffer 25 has dropped to 20 bara as a result of the height demand. The increased steam production of 97.2 kg/h results in a pressure increase in Ruth buffer to 3.23 bara.

(161) From time 1 to time 2 for 17.03 hours (absolute 19.41 hours), the yield of the methanation is kept constant at 175 kg CO.sub.2/h.

(162) The state of the system is:

(163) TABLE-US-00005 produced CO.sub.2 quantity CO.sub.2-generating plant: 125 kg/h CO.sub.2 consumption methane generation plant: 175 kg/h position of the valves 29: closed 30: open 37: closed state of compressors 23: in operation 32: not in operation pressure in the containers 25: 20 bara 31: 20 bara excess steam: 97.2 kg/h pressure in Ruth storage tank 67: 25 bara energy stored in Ruth buffer 67: 2,528.4 kWh

(164) The pressure in the gas buffer 31 is also decreased to 20 bara due to the greater consumption. The increased steam production of 97.2 kg/h results in a pressure increase in the Ruth buffer to 25 bara. The Ruth buffer has reached its upper pressure value.

(165) From time 2 to time 3 for 1.59 hours (21.0 hours total), the performance of the methanation is lowered to 50 kg CO.sub.2/h.

(166) The state of the system is:

(167) TABLE-US-00006 produced CO.sub.2 quantity CO2-generating plant: 125 kg/h CO.sub.2 consumption methane generation plant: 50 kg/h position of the valves 29: closed 30: open 37: closed state of compressors 23: in operation 32: not in operation pressure in the containers 25: 25 bara 31: 20 bara excess steam: ?145.8 kg/h pressure in Ruth storage tank 67: 20.6 bara energy stored in Ruth buffer 67: 2,348.6 kWh

(168) The pressure in the gas buffer 25 increased back to 25 bara due to the lower CO.sub.2-consumption in the methanation. The pressure in the gas buffer 31 is still 20 bara. The reduced steam production in the methanation leads to a steam withdrawal from the Ruth buffer of 145.8 kg/h. This lowers the pressure to 20.6 bara.

(169) From the time 3 to the time 4 for 11.35 hours (absolute 32.35 hours) the performance of the methanation remains constant at 50 kg CO.sub.2/h.

(170) The state of the system is:

(171) TABLE-US-00007 produced CO.sub.2 quantity CO2-generating plant: 125 kg/h CO.sub.2 consumption methane generation plant: 50 kg/h position of the valves 29: closed 30: open 37: closed state of compressors 23: in operation 32: in operation pressure in the containers 25: 25 bara 31: 50 bara excess steam: ?145.8 kg/h pressure in Ruth storage tank 67: 2.3 bara energy stored in Ruth buffer 67: 1,101.3 kWh

(172) The compressor 32 buffers the container 31 with the excess CO.sub.2 quantity back up to 50 bara.

(173) The reduced steam production in the methanation leads to further steam withdrawal from the Ruth buffer of 145.8 kg/h. Thereby the pressure drops to 2.3 bara.

(174) Thus, the initial state is reached again and the cycle can start again. The slightly higher pressure in the Ruth buffer is due to the fact that the steam having a higher specific enthalpy is returned than is withdrawn. By heat losses occurring in practice and/or additional coolers, this effect is compensated.

(175) The time periods have been chosen here so that the buffer is in each case fully charged and then fully discharged. In practice, the time cycles corresponding to the excess electricity availability will look different, so the buffers reach only intermediate states.

(176) When using a Fischer-Tropsch synthesis similarly as much steam is generated as in the methanation.

(177) If the heat of the steam electrolysis, also additionally, is used, it can cover about 35% of the heat requirement for desorption.

LIST OF REFERENCE NUMBERS

(178) TABLE-US-00008 FIG. 1 carbon dioxide generator FIG. 2 methane synthesis plant FIG. 3 Fischer-Tropsch synthesis plant FIG. 4 water vapor electrolysis (SOEC) 1 container with adsorber material 2 speed 3 ambient air 4 heat exchanger surface 5 coolant 6 cooling Tower 7 water 8 coolant tank 9 coolant pump 10 heating medium container 11 heating fluid 12 heating pump 13 heat exchanger 14 heat source/heat 15 liquid ring compressor 16 cooling tower 17 condensate 18 separation vessel 19 carbon dioxide 20 condensate 21 coolant 22 cooler 23 compressor 24 gas cooling 25 gas buffer 26 water condensate 27 condensate trap 28 tank pressure 29 control valve 30 control valve 31 long-term buffer 32 compressor 33 cooler 34 condensate 35 condensate traps 36 pressure 37 control valve 40 deionized water 41 electrolyzer 42 electric energy 43 oxygen 44 hydrogen 45 compressor 46 carbon dioxide 47 mixed gas 48 synthesis reactor 49 catalyst 50 boiling water circulation 51 reaction gas 52 heat exchanger 53 cooler 54 gas mixture 55 separators 56 water of reaction 57 methane 58 steam drum 59 pump 60 boiling water 61 saturated steam 62 heat sink 63 feedwater 64 pump 65 steam condensate loss 66 feedwater 70 steam 71 throttle valve 72 pressure 73 heating steam 74 throttle valve 75 differential amount of steam 76 steam condensate 80 deionized water 81 electrolyzer 82 electric energy 83 oxygen 84 hydrogen 85 compressor 86 carbon dioxide 87 RWGS/Reforming process 88 compressor 89 residual gas 90 electric energy 91 synthesis gas 92 cooling 93 condensate 94 compressor 95 recycle gas 96 Fischer-Tropsch reactor 97 catalyst 98 boiling water circulation 99 reaction product 100 high temperature separator 101 liquid hydrocarbon 102 hydrocarbon-containing gas 103 cooler 104 separation vessel 105 water of reaction 106 liquid hydrocarbon 107 residual gas 108 partial stream of residual gas 109 gas 110 incinerator 111 air 112 flue gas 113 product preparation 114 wax 115 diesel 116 naphtha 117 light hydrocarbon gas 118 residual gas 119 steam drum 120 pump 121 boiling water 122 saturated steam 123 heat sink 124 steam condensate 125 pump 126 steam condensate loss 127 feedwater 128 heat exchanger 129 heat 130 flue gas 131 cooler 132 separation vessel 133 sewage 134 gas flow 150 hydrogen 151 steam electrolysis 152 steam 153 electric energy 154 oxygen 155 excess heat 156 excess heat 157 excess heat 158 excess heat 159 co-electrolysis 160 CO.sub.2-steam mixture 161 oxygen 162 temperature 163 pressure 164 faucet 165 faucet 166 additional steam 167 syngas 168 vacuum pump 169 water vapor saturated CO.sub.2 170 containers 171 water vapor saturated CO.sub.2 with condensate 172 condensate 173 lock system 174 preheated additional water 175 temperature 176 pressure 177 condensate, excess water 178 condensate traps