PLANT AND PROCESS FOR REDUCTION OF THE CARBON DIOXIDE CONTENT OF ATMOSPHERIC AIR

Abstract

The disclosure relates to a plant, especially power plant, for reduction of the carbon dioxide content in atmospheric air, especially for improvement of atmospheric air quality. The plant has at least one electrolysis unit for oxygen production, at least one carbonization unit for carbon synthesis, especially a Bosch reaction unit, and at least one unit for cleaning of ambient air from an outside atmosphere surrounding the plant. The carbonization unit synthesizes carbon from carbon dioxide which is obtained from the atmosphere by means of the carbon dioxide sorption unit and this carbon is stored, in order to effectively reduce the proportion of carbon dioxide in the atmosphere. The disclosure further relates to a method of operating such a plant, with which the carbon dioxide content in the atmosphere can be efficiently reduced.

Claims

1-23. (canceled)

24. A plant adapted for reduction of carbon dioxide content of atmospheric air comprising: at least one electrolysis unit configured for oxygen production, the electrolysis unit connected to at least one water supply line to receive a water quantity, the electrolysis unit adapted to decompose the received water quantity by electrolysis into an oxygen partial quantity and a hydrogen partial quantity; at least one hydrogen transport device adapted to connect the electrolysis unit to a carbonation unit for carbon synthesis; at least one carbon dioxide sorption unit having at least one air inlet for supplying ambient air of an outside atmosphere surrounding the plant, the carbon dioxide sorption unit configured to extract a carbon dioxide quantity from the ambient air; and at least one carbon dioxide transport device adapted to connect the carbon dioxide sorption unit to the carbonation unit, wherein the electrolysis unit has at least one oxygen outlet for emission of the oxygen partial quantity, and the carbon dioxide sorption unit has at least one air outlet for emission of cleaned ambient air, wherein the oxygen outlet and the air outlet open into the outside atmosphere, wherein the carbonation unit has a carbon outlet for removal of carbon, and wherein at least one power generating unit is provided for self-sufficient power supply of the plant using one or more regenerative energy sources for power generation.

25. The plant according to claim 24, wherein the hydrogen transport device and the carbon dioxide transport device are additionally connected to a methanol synthesis unit for production of methanol, wherein the methanol synthesis unit has a methanol outlet for the removal of methanol.

26. The plant according to claim 24, wherein the power generating unit comprises one or more of: a photovoltaic unit configured for conversion of solar energy into power, a wind power unit for the conversion of wind energy into power, a water power unit for the conversion of water energy into power, or a thermal unit for the conversion of thermal energy into power.

27. The plant according to claim 24, wherein the carbonation unit is connected to the electrolysis unit by at least one water transport device.

28. The plant according to claim 24, wherein the carbonation unit is connected to a carbon store by a carbon transport device.

29. The plant according to claim 28, wherein the carbon transport device is formed at least partially by a water return line.

30. The plant according to claim 24, wherein the carbonation unit has a catalyst comprising one of iron, cobalt, nickel or ruthenium.

31. The plant according to claim 24, wherein at least one carbon dioxide extraction unit is connected to the water supply line for extraction of carbon dioxide from the water quantity.

32. A plant configured to use carbon dioxide content in atmospheric air for production of a liquid fuel comprising: at least one electrolysis unit configured for oxygen production, the electrolysis unit connected to at least one water supply line to receive a water quantity, the electrolysis unit adapted to decompose a received water quantity by electrolysis into an oxygen partial quantity and a hydrogen partial quantity; at least one hydrogen transport device, adapted to connect the electrolysis unit to a methanol synthesis unit for the production of methanol; at least one carbon dioxide extraction unit connected to the water supply line for extraction of carbon dioxide from the water quantity; at least one carbon dioxide sorption unit having at least one air inlet for supplying ambient air of an outside atmosphere surrounding the plant, the carbon dioxide sorption unit configured to extract a carbon dioxide quantity from the ambient air; and at least one carbon dioxide transport device adapted to connect the carbon dioxide sorption unit to the methanol synthesis unit, wherein the electrolysis unit has at least one oxygen outlet for emission of the oxygen partial quantity and the carbon dioxide sorption unit has at least one air outlet for emission of cleaned ambient air, wherein the oxygen outlet and the air outlet open into the outside atmosphere, wherein the methanol synthesis unit has a methanol outlet for removal of methanol, and wherein at least one power generating unit is provided for self-sufficient power supply of the plant using one or more regenerative energy sources for the power supply.

33. The plant according to claim 32, wherein the electrolysis unit has an output rate of an oxygen partial quantity per year of at least 700000 metric tons and the carbon dioxide sorption unit has an extraction rate of a carbon dioxide quantity per year of at least 400000 metric tons.

34. The plant according to claim 32, wherein the electrolysis unit is adapted to separate an oxygen partial quantity of at least 1.2 kg or a hydrogen partial quantity of at least 0.1 kg from a water quantity of at least 1.5 kg.

35. The plant according to claim 32, wherein the carbon dioxide sorption unit is adapted to extract a carbon dioxide quantity of at least 1.1 kg from an ambient air quantity of at least 3300 kg.

36. The plant according to claim 28, wherein the water supply line and the water return line are resistant to salt water for receiving salt water from a water reservoir or returning the salt water into the water reservoir.

37. The plant according to claim 32, wherein the water supply line has a desalination device.

38. The plant according to claim 24, wherein the carbonation unit comprises one of a Bosch reaction unit, a Kvaerner process unit, or a carbon dioxide plasma burner unit.

39. The plant according to claim 24, wherein at least one buffer store is provided for storing energy.

40. A method for operating a plant comprising: receiving a water quantity by at least one electrolysis unit for oxygen production through at least one water supply line, and decomposing the received water quantity by electrolysis into an oxygen partial quantity and a hydrogen partial quantity; directing the hydrogen partial quantity by at least one hydrogen transport device at least partially to a carbonation unit; cleaning ambient air of an outside atmosphere surrounding the plant by at least one carbon dioxide sorption unit having at least one air inlet for delivery of the ambient air; and directing the carbon dioxide quantity by at least one carbon dioxide transport device to the carbonation unit, wherein the oxygen partial quantity and the cleaned ambient air are emitted into the outside atmosphere, and the hydrogen partial quantity and the carbon dioxide quantity are converted in the carbonation unit to water, carbon and heat, wherein the plant is supplied in a self-sufficient manner with power from one or more regenerative energy sources.

41. The method according to claim 40, wherein a portion of one of the hydrogen partial quantity or the carbon dioxide quantity is directed at least partially to a methanol synthesis unit for production of methanol.

42. The method according to claim 40, wherein the water is directed from the carbonation unit at least partially to the electrolysis unit and used for production of hydrogen.

43. The method according to claim 40, wherein the carbon is delivered to a carbon store for long-term storage.

44. The method according to claim 40, wherein the heat is directed from the carbonation unit to the carbon dioxide sorption unit and used as energy for carbon sorption.

45. The method according to claim 40, wherein a Bosch reaction takes place in the carbonation unit for production of carbon from hydrogen and carbon dioxide.

46. A method for operating a plant comprising: receiving a water quantity by at least one electrolysis unit for oxygen production through at least one water supply line, and decomposing the received water quantity by electrolysis into an oxygen partial quantity and a hydrogen partial quantity; directing the hydrogen partial quantity by at least one hydrogen transport device at least partially to a methanol synthesis unit; cleaning ambient air of an outside atmosphere surrounding the plant by at least one carbon dioxide sorption unit having at least one air inlet for delivery of the ambient air; and directing the carbon dioxide quantity to the methanol synthesis unit by at least one carbon dioxide transport device, wherein the oxygen partial quantity and the cleaned ambient air are emitted into the outside atmosphere, and the hydrogen partial quantity and the carbon dioxide quantity are converted to methanol in the methanol synthesis unit, and wherein the plant is supplied with power in a self-sufficient manner from one or more regenerative energy sources.

Description

[0090] The invention is explained more closely below with further details with reference to the enclosed drawings. The illustrated embodiments represent examples as to how the plant according to the invention can be configured.

[0091] In these there are shown

[0092] FIG. 1 a perspective view of a plant according to the invention for reduction of the carbon dioxide content in atmospheric air according to a preferred example embodiment;

[0093] FIG. 2 a perspective view of a plant according to the invention for reduction of the carbon dioxide content in atmospheric air and for the production of a climate-neutral liquid fuel according to a preferred example embodiment;

[0094] FIG. 3 a perspective view of a plant according to the invention for the production of a climate-neutral liquid fuel according to a preferred example embodiment; and

[0095] FIG. 4 a flow chart of a method according to the invention for operating the plants according to FIG. 1 or 2 according to a preferred example embodiment.

[0096] FIG. 1 shows a perspective view of a plant 10 for reduction of the carbon dioxide content in atmospheric air according to a preferred example embodiment. The plant 10 comprises an electrolysis unit 11 for oxygen production and a carbon dioxide sorption unit 12 for cleaning ambient air UL of an outside atmosphere surrounding the plant 10. The plant 10 further comprises a power generating unit 31 for the self-sufficient power supply of the plant 10, which is described more closely later.

[0097] The electrolysis unit 11 is configured to decompose a water quantity M.sub.H20 by electrolysis into an oxygen partial quantity M.sub.O2 and a hydrogen partial quantity. The electrolysis unit 11 thus forms a unit for water electrolysis. The electrolysis unit 11 is connected to a water supply line 13 to receive the water quantity M.sub.H2O. As can be seen in FIG. 1, a pump unit 25 is arranged between the electrolysis unit 11 and the water supply line 13. The pump unit 25 has at least one pump for conveying water from a water reservoir 26. The water reservoir 26 can be a sea with sea water. Alternatively, the water reservoir 26 can be a lake with fresh water. It is also possible that the water supply line 13 is connected to a river, in order to remove fresh water for the water electrolysis. In the plant 10 shown in FIG. 1, the water supply line 13 is connected to a sea for the removal of sea water. The plant 10 is arranged near the coast, in order to keep short the distance to be overcome for water supply, in particular the water supply line 13.

[0098] The pump unit 5 is configured to convey sea water from the sea and to make it available to further plant parts or respectively units for further processing. In order to prepare the sea water for the electrolysis process by the electrolysis unit 11, the plant 10 has a sea water desalination unit 27. The sea water desalination unit 27 is connected to the pump unit 25 by at least one pipeline or is integrated into the pump unit 25. The sea water desalination unit 27 is adapted to separate a particular salt content from the conveyed sea water quantity M.sub.H2O, so that after the desalination process by the sea water desalination unit 27 the sea water has a reduced salt content. The desalinated sea water quantity M.sub.H2O corresponds to the water quantity M.sub.H2O which is decomposed by the electrolysis unit 11 into an oxygen partial quantity M.sub.O2 and a hydrogen partial quantity. The electrolysis unit 11 is connected to the sea water desalination unit 27 by at least one pipeline. In order to convey the desalinated sea water from the sea water desalination unit 27 to the electrolysis unit 11, at least one further pump can be interposed.

[0099] As described above, the electrolysis unit 11 is designed to decompose the received water quantity M.sub.H2O into a hydrogen partial quantity and an oxygen partial quantity M.sub.O2. For emitting the produced oxygen partial quantity M.sub.O2, the electrolysis unit 11 has an oxygen outlet 16, which opens into the outside atmosphere. It is possible that the electrolysis unit 11 has one or more oxygen outlets 16 for emitting the produced oxygen partial quantity M.sub.O2.

[0100] The plant 10 has, furthermore, at least one hydrogen transport device, not illustrated, which is adapted to make available to a carbonation unit 34 for further processing the hydrogen partial quantity which is separated from the water quantity M.sub.H2O. It is possible that, for this, the plant 10 has an intermediate hydrogen store, which is connected to the hydrogen transport device. After the electrolysis process, the hydrogen transport device directs the separated hydrogen partial quantity from the electrolysis unit 11 to the intermediate hydrogen store or to the carbonation unit 34 directly. Alternatively, it is possible that the hydrogen transport device delivers the hydrogen partial quantity to a further plant part which is not illustrated, in order to be further processed.

[0101] According to FIG. 1, the carbon dioxide sorption unit 12 has an air inlet 14 for the supply of the ambient air UL and a downstream sorber device 15. It is possible that the carbon dioxide sorption unit 12 has one or more air inlets 14. The sorber device 15 is connected to the air inlet 14. The sorber device 15 is adapted to extract a carbon dioxide quantity from the ambient air UL. The carbon dioxide sorption unit 12 has, furthermore, an air outlet 17. The air outlet 17 serves for the emission of the ambient air UL which has been cleaned of carbon dioxide. The air outlet 17 can be aligned in vertical direction upwards and/or part of a chimney 19.

[0102] In practice, the sorber device 15 is arranged between the air inlet 14 and the air outlet 17. In operation, the ambient air UL flows through the air inlet 14 to the sorber device 15, which separates, in particular filters, a particular carbon dioxide quantity from the air UL, wherein after the sorber device 15 the cleaned ambient air UL flows through the air outlet 17 into the outside atmosphere. Generally, it is possible that several air inlets 14, several sorber facilities 15 and several air outlets 17 are provided.

[0103] In practice, in FIG. 1 a single chimney 19 is illustrated with a height H of 200 metres, which by way of example shows the outer construction of the carbon dioxide sorption unit 12. As illustrated in FIG. 1, the air outlet 17 opens, like the oxygen outlet 16, into the outside atmosphere.

[0104] The plant 10 furthermore comprises a carbon dioxide transport device, which is configured to make available the carbon dioxide quantity, separated from the ambient air UL, to a carbon dioxide intermediate store and/or to the carbonation unit 34 of the plant 10 for further processing. Preferably, at least a portion of the hydrogen partial quantity and at least a portion of the carbon dioxide quantity are thus delivered to the carbonation unit 34, so that the extracted carbon dioxide quantity is processed with the separated hydrogen partial quantity to further intermediate and/or end products. In practice, at least a portion of the carbon dioxide quantity and at least a portion of the hydrogen partial quantity can be converted to water, carbon (graphite) and heat in a Bosch reaction, which is carried out in the carbonation unit (34), which is preferably configured as a Bosch reaction unit.

[0105] As shown in FIG. 1, the plant 10 has a planar plant region 23. The planar plant region 23 directly adjoins the electrolysis unit 11. On the planar plant region 23 a power generating unit 31 is arranged, which is a photovoltaic unit 24. The photovoltaic unit 24 is connected to the respective units of the plant 10 for power supply. The photovoltaic unit 24 is adapted such that the entire plant 10 is able to be operated in an energy-autonomous manner. This is be understood to mean that the electric current for operating the entire plant 10 is provided exclusively by solar energy by means of the photovoltaic unit 24. In other words, no fossil energy sources are used for the operation of the plant 10.

[0106] The planar plant region 23 has a longitudinal extent 32 of ca. 5000 metres and a transverse extent 33 of ca. 2000 metres. In other words, the planar plant region of the plant 10 is formed on an area of 10 square kilometres. The plant region shown in FIG. 1 containing the electrolysis unit 11 can have a partial longitudinal extent 29 of ca. two kilometres. Other partial longitudinal, longitudinal and transverse extents 29, 32, 33 are possible.

[0107] Proceeding from an overall area of the plant 10 of ca. twelve square kilometres, the plant 10 produces at least 580 metric tons of oxygen per hectare (0.01 square kilometres) per year. Compared to a conventional natural forest, which emits an annual oxygen quantity of 15 to 30 metric tons per hectare, the plant 10 has a 5 to 40 times higher oxygen output into the atmosphere. The plant 10 can therefore be designated as an artificial forest, which has a higher oxygen output rate than natural forest. In this respect, the plant according to the invention offers an approximately 30 times more efficient land utilization than the natural forest.

[0108] The sea water desalination unit 27 described above is connected to a water return line 28, through which a sea water quantity M.sub.H2O with increased salt content which is to be returned is returned into the sea. In practice, a particular salt content is extracted from the removed sea water quantity and is subsequently returned into the sea again with a portion of the removed sea water quantity as water quantity M.sub.H2O which is to be returned. Thereby, a water cycle is provided, which is harmless for nature.

[0109] The preferred installation site of the plant 10 is near to the coast of a sea. Particularly preferably, the plant 10 is constructed in a desert. The plant 10 according to FIG. 1 is a large power plant. The plant 10 has at least one mounting region 18, which is connected to a base of a building and/or of a structure. Generally it is possible that the electrolysis unit 11 and/or the carbon dioxide sorption unit 12 are arranged in a shared building or in separate buildings.

[0110] The power supply unit 31 preferably has a power store, which is not illustrated, which is adapted for power supply of the plant 10 in nighttime operation.

[0111] The plant 10 according to FIG. 2 is largely identical to the plant 10 according to FIG. 1 and differs only by a supplementation of the plant 10 by a methanol synthesis unit 37. The methanol synthesis unit 37 is connected to the electrolysis unit 11 or to a hydrogen intermediate store by a hydrogen transport device, and to the carbon dioxide sorption unit 12 by a carbon transport device. From the delivered hydrogen and carbon, the methanol synthesis unit 37 synthesizes methanol, which can be removed from the plant 10 via a methanol outlet 38. The methanol can be distributed worldwide to decentralized methanol delivery points by means of a fuel distribution system, which can comprise ships, in particular tankers, tank freight trains and/or tank trucks. The methanol delivery points can be filling stations at which the methanol is provided for the fueling of motor vehicles, aircraft, ships or locomotives.

[0112] Through a corresponding control of the method in the plant 10, an adjustment can be carried out as to which proportion of the carbon which is sorbed in the carbon dioxide sorption unit is used for the production of the liquid fuel methanol or for the production of graphite for storage in a carbon store. Initially, probably a ratio of 20% graphite and 80% methanol will be expedient, wherein the proportion of methanol is reduced successively in the further course, and the proportion of graphite is increased, when the requirement for methanol production falls in particular through the construction of further plant 10.

[0113] Generally, the plant illustrated in FIGS. 1 and 2 additionally use the carbonation unit 34, which is preferably a Bosch reaction unit. In particular, a reactor building can be provided, in which a reactor, preferably a fluidized bed reactor, is arranged, wherein in the reactor a Bosch reaction can take place. The carbonation unit 34 is preferably integrally incorporated into the plant 10, but can also be configured as a separate auxiliary plant. The carbonation unit 34 has a carbon outlet 36 which in the illustrated example embodiments is formed by the water return line 28 or opens into the latter. The required water quantity M.sub.H2O removed from the water reservoir 26 for the electrolysis is not entirely split into hydrogen and oxygen in the plant 10. Rather, a residual quantity of water remains, which is returned into the water reservoir 26 as returned water quantity M.sub.H2O via the water return line 28. The graphite produced in the carbonation unit 34 is preferably also directed here into the water reservoir 26, which is preferably the sea. A cone of inert graphite, which can be additionally used as a reef, thus forms on the seabed and thus promotes the biodiversity in the sea.

[0114] In FIG. 3 a plant 10 is shown, that substantially is intended for the transition phase in which the production of a climate-neutral liquid fuel has priority. The plant 10 according to FIG. 3 corresponds substantially to the plant 10 according to FIG. 2, but dispenses with the carbonation unit 34. However, this can be retrofitted later. The plant 10 according to FIG. 3 thus serves exclusively for the production of a liquid fuel, in particular of methanol.

[0115] For the plant 10 illustrated in the drawings, it generally applies that the carbon dioxide can be removed from the air not only via the carbon dioxide sorption unit. Rather, it is also possible that the plant 10 has a carbon dioxide extraction unit which is connected to the water supply line 13 and extracts carbon dioxide from the removed water quantity M.sub.H2O. The carbon dioxide extraction unit can be provided alternatively to the carbon dioxide sorption unit 12. However, it is preferred if the carbon dioxide extraction unit is provided additionally to the carbon dioxide sorption unit 12.

[0116] The method for operating the plant 10 according to FIG. 1 and/or according to FIG. 2 is described more closely in the following.

[0117] In a first method step, a water quantity M.sub.H2O is received by means of the electrolysis unit 11 for oxygen production through the water supply line 13. Subsequently, the received water quantity M.sub.H2O is decomposed into an oxygen partial quantity M.sub.O2 and a hydrogen partial quantity by an electrolysis process. The hydrogen partial quantity is made available by at least one hydrogen transport device to a carbonation unit 34 for further processing, wherein in the present example embodiment the carbonation unit 34 carries out a Bosch reaction.

[0118] In a second method step, ambient air UL of an outside atmosphere surrounding the plant 10 is cleaned by the carbon dioxide sorption unit 12. The ambient air UL is introduced, in particular drawn in, through several air inlets 14 into the flow channels 21, and is delivered to the downstream sorber facilities 15. Subsequently, the sorber facilities 15 extract a carbon dioxide quantity from the delivered ambient air UL. The carbon dioxide quantity is delivered to the Bosch reaction by the carbon dioxide transport device. Subsequently, after the breaking-down process, the obtained oxygen partial quantity M.sub.O2, and the cleaned ambient air UL after the extraction of the carbon dioxide quantity, is emitted into the outside atmosphere. Thereby, the oxygen content in the air is increased and the CO.sub.2 content in the air is reduced.

[0119] Furthermore, the hydrogen partial quantity together with the carbon dioxide quantity is converted by means of the Bosch reaction into water, carbon or respectively graphite, and heat, which is explained more closely in the following with the aid of the flow chart according to FIG. 4. The method described here, in particular the method shown in FIG. 4, is preferably carried out in one of the plant according to FIGS. 1 and 2.

[0120] In the method, sea water is desalinated, and the desalinated sea water is subsequently split by means of electrolysis into hydrogen and oxygen. The oxygen O.sub.2 is emitted to the ambient air, in particular into the atmosphere, so that the oxygen content in the environment of the plant is increased. Parallel thereto, carbon dioxide CO.sub.2 is collected from the ambient air UL, in particular the atmosphere, by means of a carbon dioxide sorption. The carbon dioxide or respectively the carbon dioxide quantity which is removed from the ambient air UL is directed, like the electrolytically produced hydrogen or respectively the hydrogen partial quantity, to the carbonation unit 34. In a Bosch reaction, which is carried out by means of a catalyst, such as for example iron, cobalt, nickel and/or ruthenium, 1 part pure carbon (graphite) and 2 parts water arise. The water is preferably directed back to the electrolysis, in order to reduce the consumption of sea water and the effort, connected therewith, for its desalination.

[0121] The carbon or respectively graphite can be subsequently delivered to a carbon store via the carbon transport device 35. The carbon store can be, for example, the water reservoir 26 or respectively the sea. As the graphite arising in the Bosch reaction has scarcely any to no impurities and is solidified in a rock-like manner, there are no objections to dumping the graphite in the sea.

[0122] The Bosch reaction preferably takes place at temperatures between 530? C. and 730? C., and particularly preferably in a fluidized bed reactor. With the use of a fluidized bed reactor, in particular iron granulate can be used as catalyst.

[0123] In the Bosch reaction, heat occurs as a product, in addition to water and graphite. This heat is utilized efficiently for the carbon dioxide sorption. Here, the heat can function as energy carrier for the carbon dioxide sorption, for example in order to promote the natural ventilation in the chimneys 19.

[0124] The energy required for the electrolysis, the carbon dioxide sorption and the Bosch reaction originates from regenerative energy sources, in practice from the photovoltaic unit 24, so that no additional production of carbon dioxide takes place here.

[0125] Through the method which is described here, it is consequently possible to remove carbon dioxide efficiently from the earth's atmosphere and to divide it into its components graphite and oxygen. The oxygen can be returned into the atmosphere, and the graphite can be stored permanently in a carbon store, for example in the sea.

[0126] By the invention, an improvement to atmospheric air quality is efficiently achieved.

LIST OF REFERENCE NUMBERS

[0127] 10 plant [0128] 11 electrolysis unit [0129] 12 carbon dioxide sorption unit [0130] 13 water supply line [0131] 14 air inlet [0132] 15 sorber device [0133] 16 oxygen outlet [0134] 17 air outlet [0135] 18 mounting region [0136] 19 chimney [0137] 23 planar plant region [0138] 24 photovoltaic unit [0139] 25 pump unit [0140] 26 water reservoir [0141] 27 sea water desalination unit [0142] 28 water return line [0143] 29 partial longitudinal extent [0144] 31 power generating unit [0145] 32 longitudinal extent [0146] 33 transverse extent [0147] 34 carbonation unit [0148] 35 carbon transport device [0149] 36 carbon outlet [0150] 37 methanol synthesis unit [0151] 38 methanol outlet [0152] UL ambient air [0153] UL cleaned ambient air [0154] M.sub.H2O removed water quantity [0155] M.sub.H2O returned water quantity [0156] M.sub.O2 oxygen partial quantity