AU2010362120A1

AU2010362120A1 - Method and installation for synthesising hydrocarbon

Info

Publication number: AU2010362120A1
Application number: AU2010362120A
Authority: AU
Inventors: Lothar Brehm
Original assignee: Silicon Fire AG
Current assignee: Silicon Fire AG
Priority date: 2010-10-06
Filing date: 2010-10-06
Publication date: 2013-04-18
Also published as: AU2010362092B2; AU2010362092A1; WO2012045349A1; WO2012045373A1; ES2584532T3; EP2624947A1; EP2625136A1; EP2624947B1

Abstract

The invention relates to a reactor (10) for synthesising a liquid hydrocarbon, preferably a methanol-containing hydrocarbon. A starting material is used, which contains a gas having a carbon component and a hydrogen component. The reactor (10) comprises a plurality of reactor elements connected in parallel and each of the reactor elements has a gas inlet (21) at a first tube end and a product outlet (23) at a second tube end (22.2). Each of the reactor elements comprises at least one first reactor tube (20.1) and a second reactor tube (20.2) arranged running in the opposite direction. In addition, each of the reactor elements comprises at least one guide element (30.1, 30.2), which is located between the first reactor tube (20.1) and the second reactor tube (20.2) and connects said tubes fluidically. At least one filling opening (24.1, 24.2) for introducing a catalyst for the synthesis of the liquid hydrocarbon is provided on each reactor element. The connection in parallel of the reactor elements is ensured owing to the fact that the gas inlets (21) of a plurality of reactor elements can be charged with the starting material (AS) from a common starting material feed, and owing to the fact that the product outlets (23) of a plurality of reactor elements can be connected fluidically to a downstream region of the installation.

Description

S43-0048P-WO-AU/che/ 13.3.2013 1 Silicon Fire AG, Switzerland 5 S43-0048P-WO-AU Australia 10 Method and installation for the synthesis of hydrocarbon 15 [0001] The present application relates to methods and installations for providing storable and transportable hydrocarbon-containing energy carriers. In particular, it relates to methanol synthesis. [0002] Carbon dioxide CO 2 is a chemical compound of carbon and oxygen. 20 Carbon dioxide is a colorless and odorless gas. At low concentration, it is a natural component of the air and arises in living beings during cell respiration, but also during the combustion of carbonaceous substances if sufficient oxygen is present. The CO 2 share in the atmosphere has risen significantly since the beginning of industrialization. The main causes of this are CO 2 emissions caused 25 by humans - so-called anthropogenic CO 2 emissions. The carbon dioxide in the atmosphere absorbs a part of the thermal radiation. This property makes carbon dioxide a so-called greenhouse gas (GHG) and one of the contributing causes of the global greenhouse effect. 30 [0003] For these and also for other reasons, research and development is currently being made in greatly varying directions to find a way to reduce the anthropogenic CO 2 emissions. In particular in conjunction with power generation, which is frequently performed by the combustion of fossil energy carriers, such as coal, oil, or gas, but also using other combustion processes, for example, S43-0048P-WO-AU/che/ 13.3.2013 2 waste combustion, there is a great demand for reducing the CO 2 emission. More than 20 billion tons per year of CO 2 are discharged by such processes into the atmosphere. 5 [0004] Inter alia, the principle of climate neutrality is sought, in that approaches are pursued in which attempts are made to compensate for the power production, which is linked to CO 2 emissions, at one location by the generation of alternative energies at other locations. This approach is shown very schematically in Figure 1. Emitters of greenhouse gases (GHG), such as 10 industrial enterprises (for example, automobile producers) 1 or power plant operators 2, invest or operate wind farms 3, for example, at other locations in the scope of compensation projects, in order to generate power there without GHG emissions. Climate neutrality can thus result solely in numeric terms. Numerous companies are attempting to purchase a "climate-neutral West" in this 15 way. [0005] It is considered to be a problem that currently nearly all regenerative electrical power which is generated is fed into the public AC voltage integrated network, whose frequency can only vary within very narrow limits (e.g., +/ 20 0.4%). This can only be achieved if the power generation in the network is practically always equal to the consumption. The necessity for wind and solar power plants to always have maintain the sufficient reserve and frequency regulating capacities has the result that the power supply using these plants is accordingly more costly. Wind and solar power plants in the integrated electrical 25 network therefore entail further "hidden" costs and problems. [0006] Already with the current state of development of wind power plants, the electrical power supply network can be subjected to serious problems in many countries if, for example, as a result of a lack of wind or strong wind, the 30 wind power malfunctions to a large extent, above all if this malfunction occurs suddenly and unexpectedly. In any case, however, reserve and frequency regulating capacities which are adapted to the installed wind and solar performance are required. 35 [0007] Consequently, solar and wind power plants which feed into an S43-0048P-WO-AU/che/ 13.3.2013 3 integrated electrical network can hardly replace the installed performances of other power plants in the integrated network. As a result, solar and wind power can approximately only be assessed with the saved fuel costs of the other thermal power plants present in the network. 5 [0008] It has already been shown that the regenerative forms of energy may be combined particularly advantageously with fossil forms of energy. Details can be inferred in this regard, for example, from the following parallel applications of the present applicant: published international application W02010069385A1; 10 published international application W02010069622A1; European patent application EP 10155530.8. [0009] Such a combination allows hydrocarbon-based energy carriers to be produced in corresponding Silicon Fire plants. These Silicon Fire plants are 15 particularly suitable for producing methanol therewith. [00010] Numerous methods and reactors for producing methanol are known. Corresponding exemplary patent applications and patents are cited hereafter: - EP 0 790 226 B1; 20 - WO 2010/037441 Al; - EP4483919A2. [00011] Large, complex, and very costly synthesis reactors have heretofore been used in the synthesis plants for producing hydrocarbon-based energy 25 carriers such as methanol. A few large companies have the corresponding know how for the design and production of these reactors and for the development of suitable catalysts. [00012] However, the demand exists for smaller and less expensive synthesis 30 reactors, particularly because the trend is currently going in the direction of small plants and even in the direction of transportable plants in the size of sea cargo containers. The large-scale industrial synthesis reactors are not suitable here. 35 [00013] The object prevents itself of providing a corresponding reactor and a S43-0048P-WO-AU/che/ 13.3.2013 4 corresponding method, to be able to convert a carbonaceous and hydrogenous gas, for example, synthesis gas containing H 2 and C0 2 , efficiently and cost effectively into a hydrocarbon-based energy carrier, for example, methanol. Particular attention is directed to the reduction of the structural size of the 5 synthesis reactor. In addition, the synthesis reactor is to be as scalable as possible, to be able to implement reactors of greatly varying capacity using the corresponding components. [00014] According to the invention, a method and a reactor for providing 10 storable and transportable, preferably methanol-based energy carriers are provided. In addition, a method for using such a reactor is proposed. [00015] According to the invention, a carbonaceous share of gas, preferably carbon oxides, is used as the carbon supplier. The carbonaceous share of gas is 15 caused to react with a hydrogen share in the presence of a catalyst, in order to convert these gases into an energy carrier, preferably an alcohol, and particularly preferably a methanol-containing product. [00016] Carbon dioxide is preferably taken from a combustion process or an 20 oxidation process of carbon or hydrocarbons by means of CO 2 capture. For example, CO 2 can be provided via a pipeline or also in steel bottles or tanks. However, carbon monoxide (CO) or methane gas (CH 4 ) or other fossil or biogenic gases can also be used as the carbonaceous share of gas. 25 [00017] The hydrogen can be provided via a pipeline or also in steel bottles or tanks. However, the hydrogen is preferably produced on location by means of water electrolysis. Alternatively, the hydrogen can also be produced by an oxidation reaction of elementary silicon or another elementary metal. 30 [00018] According to the invention, carbon dioxide as a carbon supplier can also be taken from crude natural gas, which can have a share greater than 10% of carbon dioxide depending on the natural gas source. Carbon dioxide can also originate, for example, from processes of lime burning or calcination to form soda. 35 S43-0048P-WO-AU/che/ 13.3.2013 5 [00019] According to the invention, the most consistent and long-term possible plant operation of a corresponding Silicon Fire plant is sought, which is achieved by uniform charging using a computer-controlled process control. 5 [00020] The Silicon Fire plant according to the invention is controlled and the individual processes are "linked" to one another so that - the total yield and the quality (for example, the purity) of the reaction products are as maximal as possible, - and/or the CO 2 (total) emissions are as minimal as possible, 10 - and/or the most consistent and long-term possible plant utilization is achieved, - and/or the product-specific investment and operating costs of the Silicon Fire plant are as minimal as possible. 15 [00021] Regenerative electrical power is preferably used for operating the Silicon Fire plant. [00022] Methanol is preferably produced as the storable and transportable form of energy using a Silicon Fire plant. I.e., the renewable energy is converted 20 chemically into a noncritical and relatively easily storable and transportable (liquid) form of energy [00023] In addition, depending on the embodiment, fossil gaseous methane can also be converted in an efficient chemical process directly into liquid 25 methanol, which is again noncritical and relatively easily storable and transportable in relation to a gas. The complex gas liquefaction plants and the corresponding liquid gas tanker ships may thus be replaced [00024] The production of liquid hydrocarbons as a relatively easily storable 30 and transportable form of energy can be shut down or even interrupted at any time. The processing plant parts for producing the hydrocarbon can be shut down or deactivated relatively easily and rapidly. The decision-making responsibility is in the scope of responsibility of the operator of the Silicon Fire plant here. 35 [00025] Liquid hydrocarbon can be used as an energy buffer. Thus, for S43-0048P-WO-AU/che/ 13.3.2013 6 example, a liquid hydrocarbon can be stored, in order to be able to provide additional electrical power in the event of peak energy demand in the integrated electrical network. If needed, methanol can either be combusted in thermal power plants, or electrical power can be generated therewith in fuel cells (e.g., 5 direct methanol fuel cells; called MFC). [00026] If needed, the methanol can be catalytically converted into a cracked gas made of hydrogen and carbon monoxide before the combustion. Advantages result therefrom in the case of certain conversion processes. 10 [00027] Preferred embodiments of the invention are based on hydrogen production with the aid of electrical power, which is generated regeneratively as much as possible and originates, e.g., from wind, water, and/or solar power plants. Hydrogen which is produced on location via electrolysis or through the 15 use of elementary silicon, for example, thus does not need to be stored or highly compressed or cryogenically liquefied and transported over large distances, but rather is used as an intermediate product, which is preferably fed at the location of its production to the above-mentioned reaction for producing hydrocarbons. 20 [00028] An energy-converting process, in which regenerative energy is converted into electrical power, depending on the embodiment of the invention, follows material-converting (chemical) processes, for example, specifically the intermediary provision of hydrogen and the conversion of the hydrogen together with a carbon carrier (e.g., carbon dioxide) to form methanol. 25 [00029] According to the invention, however, methanol can also be produced by using fossil energy or through an intelligent energy mix (see, for example, W02010069622A1) from fossil and regenerative energy. 30 [00030] In consideration of corresponding energy, plant, and economic guidelines, together with the requirement for careful usage of all material, energetic, and economic resources, a novel energy-technology solution is provided according to the invention. 35 [00031] Further advantageous embodiments can be inferred from the S43-0048P-WO-AU/che/ 13.3.2013 7 description, the figures, and the dependent claims. [00032] Various aspects of the invention are schematically shown in the drawings. 5 Figure 1: shows an outline which illustrates the principle of climate neutrality through investment in or operation of compensation projects; Figure 2: shows an outline which illustrates the fundamental steps of the method according to one of the international patent applications 10 mentioned at the beginning, or a corresponding Silicon Fire plant, respectively; Figure 3: shows an outline which illustrates the fundamental steps of the method according to the invention, or a corresponding Silicon Fire plant, respectively; 15 Figure 4A: shows a schematic view, from which the fundamental aspects of a reactor element as a reaction pipe according to the invention may be seen; Figure 4B: shows a schematic detail enlargement in partial section, from which details of the reactor element according to Figure 4A may be seen; 20 Figure 5A: shows a side view of a further reactor element according to the invention; Figure 5B: shows a top view of the reactor element according to Figure 5A; Figure 5C: shows a side view of the upper region of the reactor element according to Figure 5A in a detail view X; 25 Figure 5D: shows a section through the upper region of the reactor element according to Figure 5A; Figure 5E: shows a section along section line C-C in Figure 5D; Figure 6A: shows a side view of a further reactor element according to the invention; 30 Figure 6B: shows a top view of the reactor element according to Figure 6A and the possible angle variant of the arrangement of the individual parts of the reaction pipe according to Figure 5B; Figure 7A: shows a lateral sectional view (along section line A-A in Figure 7B) of a reactor according to the invention; 35 Figure 7B: shows a top view of the reactor according to Figure 7A; S43-0048P-WO-AU/che/ 13.3.2013 8 Figure 7C: shows a lateral outside view of the reactor according to Figure 7A; Figure 8: shows a top view of a reactor according to Figure 7A, wherein the two upper ring lines including feed lines are indicated in schematic form. 5 [00033] The term energy carrier is used here for liquid materials, which can be used directly either as a fuel or combustible. In particular, this relates to methanol 108 or a methanol-containing energy carrier here. The term "methanol-containing product" is used here, since the product which is provided at the outlet of a reactor does not consist 100% of methanol. Rather, it is a so [0 called physical mixture made of methanol and water, which is referred to here as a methanol-containing product. Pure methanol can then be obtained by a subsequent distillation process. [00034] The direction from the intake side to the outlet side, i.e., the flow 15 direction in the interior of a reactor 10, is referred to as the process direction here. [00035] In the case of methanol 108 as the energy carrier, certain boundary conditions are to be maintained during the production, storage, and transport, 20 which are similar to the conditions for handling other fossil liquid fuels and combustibles. The existing infrastructure can be used without problems here. On the material side, certain adaptations may be necessary, in order to take the corrosive properties of the methanol into consideration, for example. The safety measures with respect to health, fire, and explosion protection are also to be 25 adapted, for example. [00036] Figure 2 shows a schematic block diagram of the most important modules/components, or method steps, of a Silicon Fire plant 100 according to the international patent applications mentioned at the beginning. This plant 100 30 is designed so that a method for providing storable and transportable energy carriers 108 can be executed. The corresponding method is based on the following fundamental steps. [00037] For example, carbon dioxide 101 is provided as the carbon supplier. 35 The required DC electrical power El is generated as much as possible here by S43-0048P-WO-AU/che/ 13.3.2013 9 means of renewable energy technology and provided to the Silicon Fire plant 100. Solar thermal plants 300 and photovoltaic plants 400, which are based on solar modules, are particularly suitable as the renewable energy technology. Water power can also be used, for example. It is also possible to provide a 5 combination of multiple plant types 300 and 400, since the area requirement in relation to the electrical output of a solar thermal plant 300 is less than that of a photovoltaic plant 400. [00038] According to Figure 2, water electrolysis 105 is carried out using the 10 DC electrical power El, in order to produce hydrogen 103, or hydrogen ions, as an intermediate product. [00039] Figure 2 shows a plant 100, which is constructed so that it reduces or compensates for the disadvantages mentioned at the beginning. For this reason, 15 in the case of the Silicon Fire plan 100, a cost-effective and ecologically optimum combination of regenerative power supply (by the plants 300 and/or 400) and conventional power supply, by a part of an integrated network 500 here, is preferably implemented. This Silicon Fire plant 100 therefore provides substantially using the regenerative electrical power El directly in accordance 20 with its occurrence for chemical reactions (the electrolysis reaction 105 here) and therefore chemically binding and storing it. A further share of the required energy is obtained here, for example, from the integrated network 500. This share is converted into direct current (power) E2. For this purpose, a corresponding converter 501 is used, as schematically indicated in Figure 2. The 25 corresponding plant parts or components are also designated here as the power supply plant 501. [00040] The energy supply of the plant 100 according to Figure 2 is controlled and regulated by means of an intelligent plant controller 110. In principle, the 30 respective instantaneously available excess energy share E2 is acquired from the integrated network 500, while the other energy share (El here) is acquired as much as possible from a plant-related solar power plant 300 and/or 400 (and/or from a wind power plant and/or from a water power plant). An intelligent reversal of the previous principle thus occurs here, in the case of which the 35 energy variations of renewable power plants 300, 400 are absorbed by switching S43-0048P-WO-AU/che/ 13.3.2013 10 conventional power plants in and out. Additional performance and frequency regulating capacities for the regenerative power plants do not have to be maintained in the integrated network 500 to operate a Silicon Fire plant 100. This principle allows the operator of a Silicon Fire plant 100 to incorporate 5 additional technical and economic parameters in the controller of the plant 100. These parameters are so-called input variables I1, 12, etc., which are incorporated by the controller 110 in decisions. A part of the parameters can be predefined within the controller 110 in a parameter memory 111. Another part of the parameters can come from the outside. For example, price and/or availability 10 information from the operator of the integrated network 500 can be introduced here. [00041] Figure 3 schematically shows a plant 700 according to the invention, which is constructed so that it reduces or compensates for the disadvantages 15 mentioned at the beginning. A part of this plant 700 corresponds to the plant 100 according to Figure 2. Therefore, reference is made to the preceding description of the corresponding elements in this regard. [00042] In this embodiment, as described, high purity hydrogen 103, which is 20 converted here into methanol 108, for example, is produced by water electrolysis 105. The energy for this purpose originates entirely or substantially (preferably more than 8 0%) in this embodiment from regenerative energy sources 300 and/or 400 (or from other regenerative energy sources). 25 [00043] An array of control or signal lines can be provided, as shown on the basis of the lines 112, 113, 114 shown as examples. These lines 112, 113, and 114 control energy or mass flows of the plant 700. [00044] So-called software-based decision processes are implemented in the 30 plant controller 110. A processor of the controller 110 executes control software and makes programmed decisions in consideration of parameters. These decisions are converted into switching or control commands, which cause the control/regulation of energy and mass flows via control or signal lines 112, 113, 114, for example. 35 S43-0048P-WO-AU/che/ 13.3.2013 11 [00045] According to a particularly preferred embodiment of the invention, carbon dioxide 101 is used as a gaseous carbon supplier, as schematically indicated in Figure 3. The carbon dioxide 101 is preferably taken from a combustion process or an oxidation process via CO 2 capture (for example, a 5 Silicon Fire flue gas cleaning plant). The carbon dioxide 101 can also be separated and provided from crude natural gas. The carbon dioxide 101 can also come from other sources. The carbon dioxide 101 is preferably provided via a pipeline, a steel bottle, or a tank. 10 [00046] Furthermore, electrical DC power El is provided in the embodiment shown. The DC power El is preferably generated predominantly regeneratively (for example, by one of the plants 300 and/or 400 in Figure 3). The DC power El is used in the embodiment shown for carrying out water electrolysis to produce hydrogen 103 as an intermediate product. The electrolysis plant, or the 15 performance of such an electrolysis, is identified in Figure 3 by the reference sign 105. The carbon dioxide 101 is brought together with the hydrogen 103. The corresponding gas is designated here as the starting material AS. The starting material AS is brought to reaction (methanol synthesis in a reactor 10, according to the invention), in order to convert the gaseous (intermediate) products 101, 20 103 into methanol 108, for example. The reaction is carried out in the reactor 10 according to the invention. The removal or the provision, respectively, of the methanol 108 is identified in Figure 3 by the reference sign 107. [00047] Further fundamental details of this method and the corresponding 25 Silicon Fire plant 700 are described hereafter. [00048] Water electrolysis using direct current El is capable of being able to produce hydrogen 103 as an intermediate product. The required hydrogen 103 is produced in an electrolysis plant 105 by the electrolysis of water H 2 0 according 30 to the following equation::

H

2 0 - 286.02 kJ = H 2 + 0.5 02. (reaction 1) [00049] The required (electrical) power El for this reaction of 286.02 kJ/mol 35 corresponds to 143010 kJ per kg H 2

.

S43-0048P-WO-AU/che/ 13.3.2013 12 [00050] The synthesis of the methanol 108 (CH 3 0H) can be performed in the reactor 10 of the Silicon Fire plant 700 according to the exothermic reaction between carbon dioxide 101 (CO 2 ) and hydrogen 103 (H 2 ) as follows: 5

CO

2 + 3 H 2 = CH 3 0H + H 2 0 - 49.6 kJ (methanol-water mixture, vaporized) (reaction 2) [00051] The resulting reaction heat of 49.6 kJ/mol = 1550 kJ per kg methanol 10 = 0.43 kWh per kg of methanol 108 is dissipated from the corresponding reactor 10. For this purpose, the reactor 10 comprises a fluid chamber 14 (see, for example, Figure 7A), i.e., the reactor pipes 20.n are enclosed in the reactor 10 by a reactor sheath and cooled by a fluid (preferably water). 15 [00052] Typical synthesis conditions in the synthesis reactor 10 are approximately 50 to 80 bar and approximately 270 OC. The reaction heat can be "transferred", for example, to other plant elements, for example, a vaporizer of the distillation column or other downstream plant regions. 20 [00053] The (methanol) synthesis is carried out according to the invention using a catalyst 60 (see, for example, Figure 4B), in order to keep the reaction temperature, reaction pressure, and reaction duration low in comparison to other methods and to ensure that high purity liquid hydrocarbon (e.g., methanol 108) results as the reaction product. 25 [00054] If the Silicon Fire plant 700 is located close to a CO 2 source, liquefaction of CO 2 for the transport can be omitted. Otherwise, it is relatively simple according to the prior art to liquefy the CO 2 and also to bring it over long distances to a Silicon Fire plant 700. If liquefaction and optionally storage and 30 transport over longer distances are omitted, the CO 2 is presumably available in a cost-neutral manner in consideration of CO 2 avoidance credits. The costs for the "purchase" of the CO 2 are also relatively low in the case of transport. [00055] In Figure 3, it is indicated on the basis of the dashed arrow 112, 35 which originates from the controller 110, that the controller 110 regulates the S43-0048P-WO-AU/che/ 13.3.2013 13 power flow El. The arrow 112 represents a control or signal line. Other possible control or signal lines 113, 114 are also shown. The control or signal line 113 regulates the CO 2 quantity, for example, which is available for the reaction 106. For example, if less hydrogen 103 is produced, proportionally less CO 2 must then 5 also be supplied. The optional control or signal line 114 can regulate the H 2 quantity, for example. Such a regulation is advisable if there is a hydrogen buffer store, from which hydrogen 103 can be removed, even if no hydrogen or less hydrogen is being produced at the moment by electrolysis 105 (or by the use of elementary silicon). 10 [00056] Studies have shown that it is particularly cost-effective and environmentally friendly if the Silicon Fire plant 100 is designed or controlled so that between 15% and 40% of the methanol 108 is produced from regenerative energy, while further methanol for the supplementation to 100% is provided 15 from other hydrocarbons (e.g., from methane gas). [00057] An embodiment of the operating concept of the plant 100 is particularly preferred which provides the acquisition of cost-effective electrical power in the off-peak times from an integrated network 500 (as in Figure 2). 20 [00058] Details of a particularly preferred embodiment of a reactor 10 for the synthesis of methanol 108 are shown in Figures 4A to 7C. The statements which are made hereafter on the synthesis of methanol 108 may also be transferred to the synthesis of other liquid hydrocarbons. 25 [00059] As already described, the methanol 108 is synthesized using a starting material A, which contains CO 2 gas 101 and hydrogen gas 103, for example. The corresponding reactor 10 comprises a reactor element 15.1 or a plurality of reactor elements 15.m arranged parallel to one another (m is a whole 30 number which is greater than or equal to 2 here). In all embodiments, a reactor element 15.m comprises at least n = 2 reactor pipes 20.n (n is a whole number which is greater than or equal to 2 here). A reactor element 15.m having n = 2 reactor pipes 20.1 and 20.2 is shown in Figures 4A and 4B. In such an arrangement, which always comprises a redirection element 30.1 (a 1800 35 redirection element here) in the case of n = 2 reactor pipes 20.1 and 20.2, a S43-0048P-WO-AU/che/ 13.3.2013 14 constellation results in which both the gas inlet 21 for the starting material AS and also the product outlet 23 are either seated on the upper end of the reactor element 15.m (as shown in Figure 4A) or on the lower end of the reactor element 15.m. Specific design conditions thus result, if it is a reactor 10 which comprises 5 a larger number (e.g., m greater than 6) of reactor elements 15.m in a bundle. [00060] The term "parallel arrangement" is used here to describe that the starting material AS runs through the individual reactor elements 15.m in parallel with respect to volume and time to one another from a reaction and flow aspect. 10 Since the starting material AS is successively converted into a methanol containing material as it flows through the reactor pipes 20.n of the reactor elements 15.m, the fluid intermediate step which arises in the reactor 10 is designated here as the reaction fluid. On the intake side of the reactor 10, the methanol concentration of the reaction fluid is zero and the concentration of the 15 gaseous starting material AS is approximately 100%. In the direction of the outlet side, the corresponding concentrations shift in opposite directions until at the outlet (at product outlet 23) a methanol-containing material having a high methanol concentration (preferably a methanol-water mixture in the ratio 1:2) is formed. 20 [00061] It is an advantage of the invention that each reactor element 15.m is implemented as an independent singular synthesis reactor. Through the parallel arrangement of m reactor elements 15.1 to 15.m, the capacity of the reactor 10 may be varied (in accordance with the number m). In contrast, the number n 25 has a direct influence on the structural size of the reactor 10. [00062] Each of the reactor elements 15.m has a gas inlet 21 on a first pipe end 22.1 and a product outlet 23 on the second pipe end 22.2. Each of the reactor elements 15.m has at least one redirection element 30.k (preferably in 30 the form of a 1800 redirection element), which is between the first pipe end 22.1 and the second pipe end 22.2 of the respective reactor element 15.m. [00063] If one reactor element 15.m comprises n = 2 reactor pipes 20.1 and 20.2, then it has k = 1 1800 redirection elements 30.k. If one reactor element 35 15.m comprises n = 3 reactor pipes 20.1, 20.2, and 20.3, then it has k = 2 1800 S43-0048P-WO-AU/che/ 13.3.2013 15 redirection elements 30.k. This principle may also be transferred accordingly two reactor elements 15.m having more than three (i.e., n greater than 3) reactor pipes 20.n. 5 [00064] According to the invention, the reactor pipes 20.n of a reactor element 15.m are arranged to run in opposing directions. An arrangement to run in opposing directions designates a spatial constellation with respect to flow in which the reaction fluid flows outward and downward in a reactor pipe 20.1, for example, while the reaction fluid then flows upward after the deflection in a 10 redirection element 30.1 in a second reaction pipe 20.1. Preferably, the reactor pipes 20.n of a reactor element 15.m are seated closely to one another in all embodiments. The mutual clearance (outer wall to outer wall) is preferably less than the external diameter of one of the reactor pipes 20.n. 15 [00065] In Figures 5A - 5E, 6A, 6B, reactor elements 15.m having n=3 reactor pipes 20.1, 20.2, and 20.3 and k=2 1800 redirection elements 30.1, 30.2 are shown. The advantage of an odd number n is that the inlet side and the outlet side are on opposite ends of the reactor element 15.m. Space is thus obtained for arranging a shared intake manifold or distributor 11.1, 11.2 (for 20 example, in the form of a ring line) on one side and for arranging the product outlet or outlets 23 on the other side. [00066] Each of the reactor elements 15.m comprises at least one upper filling opening 24.1 for decanting a catalyst 60 for the synthesis of methanol. 25 Preferably, in all embodiments each reactor pipe 20.n and/or each upper redirection element 30.2 comprises a separate filling opening 24.1 or 24.2, respectively. The filling openings 24.2 on the upper redirection elements 30.2 are preferably somewhat larger than the upper filling openings 24.1 in all embodiments, since two reactor pipes 20.2, 20.3 are filled from above through 30 the redirection element 30.2. If needed, lower emptying openings 25.1, 25.2 can also be provided (see, for example, Figure 5A and Figure 6A). The emptying openings 25.2 on the lower redirection elements 30.1 are preferably somewhat larger than the lower emptying openings 25.1 in all embodiments, since two reactor pipes 20.1, 20.2 are emptied from below through the redirection element 35 30.1.

S43-0048P-WO-AU/che/ 13.3.2013 16 [00067] The catalyst 60 and/or inert material 61 can be decanted into the filling openings 24.2. The catalyst 60 and/or the inert material 61 can be emptied through the emptying openings 25.2. The filling openings 24.1, 24.2 and/or the 5 emptying openings 25.1, 25.2 can be provided in all embodiments of the invention. [00068] The filling openings 24.1, 24.2 and/or the emptying openings 25.1, 25.2 are preferably closable in all embodiments, e.g., using a screw closure or 10 using a cap. [00069] The parallel arrangement of the reactor pipes 20.n is ensured in that the gas inlets 21 of a plurality of reactor elements 15.m can be charged with the starting material AS by a shared manifold for the synthesis gas 11.1, 11.2 15 (preferably in the form of a shared ring line), and the product outlets 23 of a plurality of reactor elements 15.m are connectable with respect to flow to a downstream plant region (for example, a distillation column). [00070] Further details of a reactor element 15.m according to Figures 5A 20 5E are described hereafter. A reactor element 15.m is shown in these figures, which is especially designed to be arranged in an outer ring (outer bundle) of a reactor 10. The reactor element 15.m comprises n = 3 reactor pipes 20.1, 20.2, 20.3. It has a first upper filling opening 24.1 and an upper gas inlet 21. The first reactor pipe 21 extends vertically downward and opens into a first redirection 25 element 30.1. A lower emptying opening 25.2 is provided on the first redirection element 30.1. A second reactor pipe 20.2 extends vertically upward from the first redirection element 30.1 and opens into a second redirection element 30.2. An upper filling opening 24.2 is provided on the second redirection element 30.2. A third reactor pipe 20.3 extends vertically downward from the second 30 redirection element 30.2. The third reactor pipe 20.3 has a lower emptying opening 25.1 and a lower product outlet 23. [00071] The constellation shown has an effective reaction length LE (called the reactor path) which corresponds to three times the individual length L, since 35 the three reactor pipes 20.1, 20.2, 20.3 offer a folded (meandering) course for S43-0048P-WO-AU/che/ 13.3.2013 17 the reaction fluid. [00072] Figure 5C shows that the redirection element 30.2 can have a funnel shape. This shape is preferred. However, the outer envelope is not important, 5 but rather the interior, which must be designed so that there is a flow connection from one reactor pipe 20.2 to the next reactor pipe 20.3, which does not form an interfering cross-section reduction or barrier. In Figure 5D, one can look from above into the interior of the redirection element 30.2. Figure 5E shows a section. It can be seen in the sectional view that the interior is funnel-shaped 10 here. [00073] Each redirection element 30.k can preferably have a partition wall 31 in the interior, which is used for the separate filling of the individual reactor pipes 20.n. This partition wall 31 is preferably used only at the moment of filling. It is 15 also possible during filling to temporarily cover one of the two reactor pipes in the interior of the redirection element 30.k, so that at this moment the other reactor pipe can be filled. [00074] Figure 5B shows that the gas inlet 21 and the product outlet 23 can 20 be arranged diagonally, for example. The directions are preferably selected so that a shared starting material feed 11 may be attached to the inlet as a manifold/distributor. On the outlet side, the product outlets 23 are preferably arranged so that two or more of them may be combined. 25 [00075] The reactor elements 15.m are special in the following aspect. They are filled or provided with the catalyst 60 so that a reactor route results which comprises a catalyst section, which is followed by a section having inert material 61. After the section having the inert material 61, a catalyst section again follows. This principle can be seen in Figure 4B. The first reactor pipe 20.1 is 30 filled with the catalyst 60. The redirection element 30.1 is filled with the inert material 61 and the second reactor pipe 20.2 is in turn filled with the catalyst 60. Catalyst columns or sections, which are supported on the inert material 61, result in the two reactor pipes 20.1, 20.2. Because the inert material 61 was introduced into the redirection element 30.1, no catalyst 60 can penetrate into 35 the base region (lowermost region) of the redirection element 30.1.

S43-0048P-WO-AU/che/ 13.3.2013 18 [00076] The catalyst 60 is typically subjected to a reduction step in the reactor pipes 20.n, wherein the catalyst 60 experiences a volume reduction, which is at least partially compensated for by the inert material 61 slipping, 5 filling, or sliding in. The inert material 61 can also slide in or fill up cavities which result upon the reduction of the catalyst. In addition, the inert material 61 prevents flow-related jumping of the catalyst 60 up into rising reactor pipes (for example, in reactor pipe 20.2). 10 [00077] The inert material 61 is used in all embodiments. [00078] Figure 5B shows that the three reactor pipes 20.1, 20.2, 20.3 lie or stand in a shared first plane Fl. Figure 6B shows that the three reactor pipes 20.1, 20.2, 20.3 can also have an angled arrangement, in which a first outer 15 reactor pipe 20.1 lies or stands with the middle reactor pipe 20.2 in a shared first plane F1 and a second outer reactor pipe 20.3 lies or stands with the middle reactor pipe 20.2 in a shared second plane F2. Very dense packing or bundling may thus be achieved in all embodiments. 20 [00079] The description of Figures 4A to 4E may be transferred 1:1 to Figures 5A, 5B. The embodiment in Figures 5A, 5B substantially differs only through the angled arrangement. The angled arrangement (at an angle of 1300 here) was selected to be able to arrange the corresponding reactor elements 15.m in the inner bundle of a reactor 10. The gas inlet 21 and the product outlet 23 25 preferably point in different directions here. [00080] Figures 7A to 7C show a reactor 10 which was developed and optimized according to the stated object. The reactor 10 comprises a bundle of reactor elements 15.m here. In the concrete example shown, the reactor 10 30 comprises an inner bundle having 8 reactor elements 15.m according to Figure 6A, 6B and an outer bundle having 12 reactor elements 15.m according to Figures 5A - 5E (i.e., m = 20). So as not to interfere with the illustration in Figure 7A to 7C as a result of an excess number of reference lines and reference signs, only a part of the elements were provided with reference lines and 35 reference signs. The reactor 10 preferably comprises a fluid chamber 14, which S43-0048P-WO-AU/che/ 13.3.2013 19 has a cylinder shape here. The fluid chamber 14 encloses the entire bundle of the reactor elements 15.m, wherein only the upper and lower ends of the reactor elements protrude out of the fluid chamber 14. Therefore, the first and second filling openings 24.1, 24.2 and the inlet-side gas inlets 21 and the outlet-side 5 product outlets 23 lie outside the fluid chamber 14. The fluid chamber is used for the purpose of providing an isothermal environment in a preferred operating mode of the reactor 10. A fluid (e.g., water or gas) can enter the fluid chamber 14 through a fluid feed 16 for this purpose. A fluid drain 17 is provided on the fluid chamber 14 in order to drain off the fluid. Depending on the situation, it can 10 be cooled or heated. The emptying openings 25.1, 25.2 preferably also lie outside the fluid chamber 14. [00081] In all embodiments, a controller of the reactor 10 is preferably used, which applies hot fluid to the fluid chamber at the beginning during the "startup" 15 of the reactor 10, in order to start up the synthesis reaction. A cooled fluid is preferably subsequently fed, in order to dissipate reaction heat which arises during the exothermic synthesis and thus provide an isothermal environment. Depending on the capacity of the reactor 10, reaction heat can be fed by means of a fluid into the fluid chamber 14 and the synthesis reaction can run in the 20 endothermic range. [00082] The fluid chamber 14 is preferably designed in all embodiments so that at least the reaction sections of the reactor pipes 20.n, which are filled with the catalyst 60, and the redirection elements 30.k lie in the isothermal 25 environment. [00083] Figure 7B shows the top view of the reactor 10. It may be seen that the gas inlets 21 of the outer bundle point radially outward. They all end at a shared first radius. The gas inlets 21 of the inner bundle point diagonally outward 30 and all end at a shared second radius, which is smaller than the first radius. This type of alignment and arrangement of the gas inlets 21 allows two ring lines 11.1 and 11.2 to be provided, as schematically indicated in Figure 8. A first upper ring line 11.1 has a radius which corresponds to the first radius, so that the gas inlets 21 of the outer bundle can all be charged with the starting material AS by the 35 first upper ring line 11.1. A first feed line 12.1 can preferably be provided on the S43-0048P-WO-AU/che/ 13.3.2013 20 first upper ring line 11.1. A second upper ring line 11.2 has a radius which corresponds to the second radius, so that the gas inlets 21 of the inner bundle can all be charged with the starting material AS by the second upper ring line 11.2. A second feed line 12.2 can preferably be provided on the second upper 5 ring line 11.2. However, all feed lines 21 of the inner 8 reactor elements and the outer 12 reactor elements can also be charged by a shared ring line, which is used as a manifold or distributor. [00084] Figures 7B and 8 show that filling openings 24.1, 24.2 are preferably 10 freely accessible from above, in order to allow simple filling and/or ventilation and/or flushing (for example, with inert gas). [00085] Figure 7C shows the reactor 10 from the outside. The reference signs are the same as in the other figures. Therefore, reference is made to the 15 description of the other figures. The fluid chamber 14 has an envelope diameter D here, which can be approximately 1 m, for example. The height H of the fluid chamber 14 is approximately 2.2 m here, for example. Therefore, reactor elements 15.m may be housed in the fluid chamber 14, which each have a total reaction path of approximately 5.7 m. The total reaction path of approximately 20 5.7 m is composed here of three partial paths, since each of the reactor elements 15.m comprises n = 3 reactor pipes 20.1, 20.2, and 20.3. The mutual pipe spacing AR (see Figure 5E) can be approximately 60 mm, for example, and the individual reactor pipes 20.n can have an external diameter of 42 mm and an internal diameter of 33 mm, for example. 25 [00086] In all embodiments of the invention, the starting material AS is preferably preheated and/or introduced at elevated pressure through the feed lines 12.1, 12.2 and the ring lines 11.1, 11.2 into the reactor elements 15.m. The pressure and the temperature are dependent on the type of the catalyst 60. 30 The temperature is preferably in the range between 100 and 350 0 C. The pressure is typically between 10 and 150 bar. [00087] It is considered to be an important advantage of the invention that, for example, in the case of a synthesis method for producing methanol from CO 2 35 gas 101 and hydrogen 103, which requires 4 I of catalyst volume, in order to S43-0048P-WO-AU/che/ 13.3.2013 21 ensure a desired production quantity per day, the structural height of the reactor 10 can be significantly reduced in relation to typical linear reactors. A typical reactor would usually have, for example, an overall structural height which is in the range of approximately 6 m, while in contrast the height H according to the 5 invention in the case of triple folded reactor elements 15.m is approximately 2.2 m. The overall height (i.e., including the filling openings 24.1, 24.2, the emptying openings 25.1, 25.2, the gas inlets 21, and the product outlets 23), would then be approximately 2.6 m. 10 [00088] It is a further advantage that as a result of the "folding" of the reactor pipes 20.n, it becomes simpler to predefine and maintain uniform (for example, isothermal) environmental conditions for all sections of the reactor elements 15.m. In the case of a linear reactor pipe, which is 6 m long, for example, it is significantly more difficult to predefine and maintain homogeneous 15 environmental conditions than in the case of a folded arrangement according to the invention. Homogeneous environmental conditions are particularly important to achieve uniform conversion and to prevent the catalyst 60 from being loaded unevenly. In addition, for example, cooler regions can result in an interruption or influence of the synthesis. 20 [00089] Plants of the present sizes must be constructed compactly. For this case, short reactors 10, which are placed in a container, for example, are advantageous. In addition, the support plates which are typical in the case of longer reactor pipes are omitted. 25 [00090] A reactor 10 according to the invention can achieve a conversion rate which is higher than in the case of linear tube reactors. [00091] The "folding" can change the synthesis kinetics under certain 30 circumstances. This would be the case, for example, if bottlenecks or blockades would occur in the redirection elements 30.k. Therefore, the inert material 61 is preferably used in the redirection elements 30.k in all embodiments. Dewpoint shifts can also be avoided by the use of the inert material 61. The design of the redirection elements 30.k, the equipping with the inert material 61, and the 35 arrangement thereof within the fluid in the fluid chamber 14 prevent the S43-0048P-WO-AU/che/ 13.3.2013 22 methanol condensation in the interior of the reactor elements 15.m from the reaction fluid. [00092] Hard ceramic inert material 61 (preferably in spherical form) is 5 particularly preferably used in all embodiments. [00093] The inert material 61 in the lower redirection elements (for example, 30.1) is particularly preferably used as a support or carrier structure under the catalyst bed (similarly, for example, to a gravel bed under a filter) in all 10 embodiments. [00094] The inert material 61 in the upper redirection elements (for example, 30.2) is preferably used in all embodiments - as a safeguard against flow-related damage in the event of stronger incident 15 flow, and/or - as a retention layer against "dancing" catalyst 60, and/or - as a retention layer in the event of pressure surges directed backward (for example, in the event of a reactor emergency shut off) or in the event of downward flows in the reactor 10. 20 [00095] The loose inert material 61, which is used in all embodiments, also has the advantage that solid metal installed parts are not required. In addition, the inert material 61 can be decanted and removed again without problems. 25 [00096] The aspects of the various embodiments may be combined with one another without problems through small adaptations. [00097] Further fundamental aspects of a method according to the invention for providing storable and transportable energy carriers are described hereafter. 30 [00098] The reactor 10 is especially suitable for the synthesis of regenerative methanol CH 3 0H from carbon dioxide CO 2 and hydrogen H 2 , which is produced via the (endothermic) electrolysis of water using regenerative electrical power according to reaction 1, as already mentioned above. 35 S43-0048P-WO-AU/che/ 13.3.2013 23

H

2 0 - 286.02 kJ/mol = H 2 + 0.502 . (reaction 1) [00099] The exothermic methanol synthesis (reaction 2, as already mentioned above) is represented by the following summation formula: 5

CO

2 + 3 H 2 = CH 3 0H + H 2 0 - 49.6 kJ (gaseous methanol). (reaction 2) [000100] The regenerative electrical power El used has the disadvantages, in particular in the case of wind and solar power, that it is relatively costly and is 10 only available irregularly and with time restrictions. [000101] Therefore, it is proposed here that the regenerative production of methanol 108 using regenerative electrical power El according to reactions 1 and 2 be supplemented by methanol synthesis which is based on the raw 15 material base of natural gas having the main component methane CH 4 , or is based on other carbon starting materials or hydrocarbon starting materials. This synthesis can be performed, for example, by exothermic direct oxidation (oxidative transformation, oxidative conversion) of the methane according to the following summation formula 20

CH

4 + 0.502 = CH 3 0H - 167.5 kJ/mol . (reaction 4) [000102] This reaction 4 is designated here as direct oxidation. The required oxygen can be taken from the above-mentioned water electrolysis (reaction 1). 25 [000103] However, the path via partial oxidation (see reaction 5) or reforming (see reactions 7 and/or 8) (preferably as autothermal reforming) can also be selected, in order to arrive at a fossil methanol share via the path of synthesis gas (essentially comprising carbon monoxide and hydrogen here). The 30 corresponding oxygen share typically comes from an air fractionation plant. [000104] Above all, the fact is novel that the (pure) oxygen, or the strongly oxygenated gas, respectively, for reaction 4 or also for the partial oxidation or the reforming originates directly or in buffered form from the hydrolysis reaction 35 (reaction 1) or from reaction 3. If the (pure) oxygen or the strongly oxygenated S43-0048P-WO-AU/che/ 13.3.2013 24 gas, respectively, is taken from the hydrolysis reaction (reaction 1), according to the mass ratios of reactions 1, 2, and 4, the oxygen from reaction 1 is sufficient to provide at most three times as much fossil methanol by means of reaction 4 than using reaction 2. If all oxygen from reaction 1 is used, the total produced 5 methanol can originate one-fourth from the "regenerative" reaction 2, which occurs in a reactor 10, and three-fourths from the "fossil" reaction 4 (for example, direct oxidation). [000105] By reducing the methanol share from reaction 4, the "regenerative" 10 share 108 of the total methanol production can be increased, for example, also with corresponding effects on the CO 2 balance of the overall methanol production and the specific CO 2 emissions during the combustion of the " overall" methanol to generate heat or as a fuel. 15 [000106] In practice, the available regenerative electrical power El is preferably maximally utilized to produce "regenerative" methanol 108 according to reactions 1 and 2 and the share of the "fossil" methanol produced according to reaction 4 is adjusted to the maximum possible value according to economic and ecological targets and boundary conditions, for example, depending on the 20 desired specific CO 2 emission of the "overall" methanol during combustion or according to the instantaneous price and the availability of the natural gas or according to the "overall" methanol quantity to be produced or according to the prices of the regenerative and fossil methanol shares. 25 [000107] It must be emphasized that the reactor 10 can, of course, also be used for other synthesis methods in all embodiments, and the synthesis can be operated using regenerative power and/or using regenerative starting material AS, or also using fossil power and/or using fossil starting material AS. 30 [000108] It is particularly advantageous that the "regenerative" methanol 108 and the "fossil" methanol can occur separately in different reactors and can either be discharged separately or can be mixed in arbitrary shares after the occurrence and possible temporary storage, so that the Silicon Fire plant 700 can deliver pure "regenerative" methanol 108 and pure "fossil" methanol, but also 35 arbitrary mixtures of both, in order to be able to be marketed, for example, as S43-0048P-WO-AU/che/ 13.3.2013 25 regenerative fuel with permissible fossil share or permissible specific CO 2 emission. [000109] The reaction heat of the exothermic reactions 2 and 4 is preferably 5 utilized, whereby the specific CO 2 emissions of the various methanol shares to be calculated would also be decreased. For the heat utilization, for example, the heating of thermal seawater desalination plants very advantageously comes into consideration under the conditions of the Persian Gulf, in particular during the colder time of year, when thermal power plants are run at part load or are even 10 shut down because of the substantially lower power demand for building air conditioning and the waste heat thereof is no longer (sufficiently) available for the seawater desalination plants connected thereto. The heat which is withdrawn by the fluid via the fluid chamber 14 from the reactor 10, for example, can also be used in other plant regions. 15 [000110] The result of reaction 4 can be achieved, for example, by the combination of following reactions 5 and 6, which have been tested at a commercial scale. 20 [000111] The partial oxidation of methane:

CH

4 + 0.502 = CO + 2H 2 -36 kJ/mol (reaction 5) [000112] and the classical methanol synthesis (for example, 250 bar, 350 OC, 25 using chromium oxide-zinc oxide catalyst): CO + 2H 2 = CH 3 0H -128.20 kJ/mol (liquid methanol). (reaction 6) [000113] If reactions 5 and 6 are combined, a quasi-oxidation of the methane 30 containing gas using oxygenated gas also occurs. [000114] Reaction 6 can run under certain circumstances in the same reactor 10 as reaction 2, possibly with change or adaptation of the catalyst filling and the catalysis conditions. However, for example, two reactors 10 according to the 35 invention having different catalyst filling can also be used.

S43-0048P-WO-AU/che/ 13.3.2013 26 [000115] The reforming of methane using water steam (steam reforming) to form synthesis gas runs endothermically according to the following reaction: 5 CH 4 + H 2 0 (gaseous) = CO + 3H 2 + 206.2 kJ/mol (reaction 7) [000116] The reforming of methane with carbon dioxide to form synthesis gas runs endothermically according to the following reaction: 10 CH 4 + CO 2 = 2CO + 2H 2 + 247 kJ/mol (reaction 8) [000117] The three reactions 5, 7, and 8 can run jointly in a reactor 10 at temperatures of approximately 800 - 1000 0 C via catalysts and can be controlled so that they run with as much energy autonomy as possible ("autothermally") 15 and the reaction products result in a suitable synthesis gas for the classical methanol synthesis according to reaction 6. [000118] Further details can be inferred, for example, from the publication by Bharadwaj, S.S.; L.D. Schmidt: Catalytic partial oxidation of natural gas to 20 syngas. Fuel Processing Technology 42 (1995), pages 109 - 127. [000119] The use of the invention is particularly advantageous in conjunction with a method for methanol synthesis which operates at low pressures (for example, 80 bar). 25 [000120] The principle of the invention may also be transferred to large-scale plants. [000121] According to the invention, CO 2 101 is preferably used as the starting 30 material and carbon supplier for the methanol synthesis in the reactor 10. The following are preferably used as CO 2 sources: steam reforming plants, CO 2 capture plants for crude natural gas, lime kilns, calcination plants for soda, fermentation plants for bioethanol, seawater desalination plants, large-scale furnace plants for fossil fuels (for example, power plant furnaces), and other 35 plants or combustion processes, which emit relatively large quantities of C0 2

.

S43-0048P-WO-AU/che/ 13.3.2013 27 [000122] The invention allows the substantial economic disadvantages of known approaches to be avoided if - as in the case of the Silicon Fire plant 700 the transient occurring electrical solar and/or wind power is converted directly 5 into chemical reaction enthalpy and stored chemically bound, without additional capacities for reserve performance and/or frequency regulation in the integrated network and the expenditures required for this purpose being required. [000123] In the case of photovoltaic power generation by means of a 10 photovoltaic plant 400, it is a further advantage that the direct current El primarily occurring from the solar cells of the photovoltaic plant 400 can be used directly for the chemical process (electrolysis 105), without having to be converted via inverters into alternating current for the voltage transformation. 15 [000124] In another embodiment of the invention, an ATR process (autothermal reforming) can also be used for the processing of the starting material AS. In the case of the autothermal reforming, a hydrocarbon-containing or a carbonaceous starting material is oxidized in a reaction zone in the presence of a substoichiometric quantity of oxygen (for example, oxygen), which is 20 inadequate for complete oxidation. In addition, water steam and/or carbon dioxide are supplied, to be able to produce synthesis gas in this manner, which substantially comprises carbon monoxide and hydrogen. The starting material can be natural gas or another hydrocarbon. It is also possible to convert coal, oil, combustion gases, biomass, oil sands, or oil slate using the ATR process into a 25 suitable synthesis gas. [000125] The synthesis gas made of carbon monoxide and hydrogen or carbon dioxide and hydrogen or carbon monoxide, carbon dioxide, and hydrogen can be converted in a reactor 10 according to the invention using a respective suitable 30 catalyst 60 into methanol 108, as described (carbon monoxide and carbon dioxide are designated here as carbon oxides). Depending on the synthesis reaction, for example, copper-based catalysts 60 (for example, CuO catalysts) or zinc oxide catalysts 60 (for example, ZnO catalysts), or chromium oxide-zinc oxide catalysts 60 can be used. All other known catalysts are also suitable for 35 use in a reactor 10. Solid bed catalysts or fluidized bed catalysts are particularly S43-0048P-WO-AU/che/ 13.3.2013 28 suitable. The catalyst 60 can also comprise a suitable carrier (for example, carbon, silicate, aluminum (for example, A1 2 0 3 ) or ceramic). Instead of the mentioned "metal" catalysts 60, an organic catalyst 60 can also be used. 5 [000126] The catalyst 60 preferably has a grain, bead, or particle size between 1 and 10 mm in all embodiments. A grain, bead, or particle size between 3 and 8 mm is particularly preferable. The inert material 61 preferably also has a grain, bead, or particle size in all embodiments which is somewhat smaller than the grain, bead, or particle size of the catalyst 60. Embodiments in which the grain 10 size of the inert material 61 is smaller than the grain size of the catalyst 60 are particularly preferable, so that the catalyst 60 does not slip into cavities in the inert material 61. [000127] The "folding" of the reactor pipes 20.n and the use of the redirection 15 elements 30.k is considered to be an advantage, so that, for example, temperature measuring points can be arranged on the redirection elements 30.k. The synthesis reaction can thus be better monitored and more precisely controlled. 20 [000128] In another embodiment of the invention, carbon dioxide is supplied during the ATR process. The addition of CO 2 can be advantageous if the stoichiometric ratios are not optimum for the synthesis of methanol 108 because of the starting materials. 25 [000129] In a particularly preferred embodiment of the invention, the (regenerative and/or fossil) methanol is used as an energy carrier for storage and transportation. [000130] According to the invention, carbon dioxide as a carbon supplier can 30 also be taken from the crude natural gas, which can have more than 10% carbon dioxide share depending on the natural gas source. After the delivery of the crude natural gas, gas washing (by means of gas washing technology or another gas separation technology) is already carried out currently, in order to separate the CO 2 from the actual natural gas. This CO 2 is usually emitted into the 35 atmosphere. According to the invention, the C0 2 , which is provided in S43-0048P-WO-AU/che/ 13.3.2013 29 substantially pure form, can be used as the carbon supplier 101. [000131] For the use of the methanol 108 in internal combustion engines, for example, also in combined gas/steam turbine plants, a catalytic cleavage (for 5 example, at approximately 380 0 C) before the combustion according to reaction 9:

CH

3 0H (liquid) = 2H 2 + CO +128.20 kJ/mol (reaction 9) 10 can provide the following advantages. An internal combustion engine normally operated using gas does not have to be refitted for a liquid fuel. The reaction heat of the endothermic methanol cleavage reaction 9 of 128.20 KJ/mol or 4006 kJ/kg methanol can be applied by the 15 exhaust gas waste heat of an internal combustion engine, whereby the original heating value of the methanol of 19900 kJ/kg is increased by the supplied reaction heat by approximately 20 %. The application of a corresponding methanol cleavage for power plant processes is described, for example, in MuBenbrock, K: "M6glichkeiten zur Nutzung von Methanol in 20 Kraftwerksprozessen [Possibilities for Using Methanol in Power Plant Processes"", VGB Kraftwerkstechnik 71 (1991), volume 8, pages 759 - 764.

S43-0048P-WO-AU/che/ 13.3.2013 30 Reference signs: vehicle industry/automobile construction 1 power plant operator 2 wind farm 3 reactor 10 shared starting material feed 11 first upper ring line 11.1 second upper ring line 11.2 feed lines 12.1, 12.2 fluid chamber 14 reactor elements 15.m fluid feed 16 fluid drain 17 reactor pipes 20.n gas inlet 21 first pipe end 22.1 second pipe end 22.2 product outlet 23 filling opening 24.1, 24.2 emptying opening 25.2, 25.2 redirection element 30.k partition wall 31 catalyst 60 inert material 61 Silicon Fire plant (from parallel application) 100 carbon dioxide 101 water 102 hydrogen 103 provision of carbon dioxide 104 performance of electrolysis 105 discharge/provision of methanol 107 transportable energy carrier 108 (plant) controller 110 parameter memory 111 control or signal lines 112, 113, 114 solar thermal plant 300 conversion of heat into direct current 301 solar plant (photovoltaic plant) 400 integrated network 500 conversion of AC voltage into direct current 501 (power supply plant) starting material containing silicon dioxide 601 silicon 603 S43-0048P-WO-AU/che/ 13.3.2013 31 reduction method 602 silicon dioxide as back-reaction product 604 hydrolysis 605 Silicon Fire plant (invention) 700 arrows 701, 702 pipe spacing AR starting material AS envelope diameter D DC power El first plane F1 second plane F2 height H effective length LE input variables I1, 12, etc. primary energy P1, P2

Claims

1. A reactor (10) for the synthesis of a liquid hydrocarbon, preferably a 5 methanol-containing hydrocarbon (108), using a starting material (AS), which contains a gas having a carbon share and a hydrogen share, wherein the reactor (10) comprises a plurality of reactor elements (15.m) connected in parallel to one another and wherein each of the reactor elements (15.m) has a gas inlet (21) at a first pipe end (22.1) and a product outlet (23) at a 10 second pipe end (22.2), characterized in that - each of the reactor elements (15.m) comprises at least one first reactor pipe (20.1) and one second reactor pipe (20.n) arranged in the opposite direction, - each of the reactor elements (15.m) comprises at least one redirection 15 element (30.k), which is seated between the first reactor pipe (20.1) and the second reactor pipe (20.2) and connects them with respect to flow, - each of the reactor elements (15.m) comprises at least one filling opening (24.1, 24.2) for introducing a catalyst (60) for the synthesis of the liquid hydrocarbon, 20 wherein the connection in parallel of the reactor elements (15.m) is ensured in that the gas inlets (21) of a plurality of reactor elements (15.m) can be charged with the starting material (AS) by a shared starting material feed (12.1, 12.2), preferably in the form of a shared ring line (11.1, 11.2), and the product outlets (23) of a plurality of reactor elements (15.m) are 25 connectable with respect to flow to a downstream plant region.

2. The reactor (10) according to Claim 1, characterized in that each of the reactor elements (15.m) comprises, viewed in the process direction - the gas inlet (21) at the first pipe end (22.1), 30 - a first reactor pipe (20.1), - a first redirection element (30.1), - a second reactor pipe (20.2), and - the product outlet (23) at the second pipe end (22.2). 35

3. The reactor (10) according to Claim 2, characterized in that, viewed in the process direction S43-0048P-WO-AU/che/ 13.3.2013 33 - after the second reactor pipe (20.2) and before the product outlet (23), a second 1800 knee element (30.2) and - a third reactor pipe (20.2) follow. 5

4. The reactor (10) according to Claim 3, characterized in that the first pipe end (22.1) lies on top and the second pipe end (22.2) lies on the bottom.

5. The reactor (10) according to one of the preceding claims, characterized in that the redirection element (30.k) is at least partially filled or equipped 10 with an inert material (61).

6. The reactor (10) according to Claim 5, characterized in that a granular, grainy, spherical, net-like, latticed, or honeycomb material is used as the inert material (61). 15

7. The reactor (10) according to Claim 5 or 6, characterized in that a ceramic material is used as the inert material (61).

8. The reactor (10) according to one of the preceding claims, characterized 20 in that the redirection element (30.k) is a 1800 redirection element (30.k), which is implemented as a deflection chamber which causes a 1800 deflection of a fluid flow in the interior of a preceding reactor pipe (20.1), viewed in the process direction, and a following reactor pipe (20.2), viewed in the process direction. 25

9. The reactor (10) according to one of the preceding claims, characterized in that it comprises at least one ring line (11.1, 11.2) on the intake side, which is used as a shared starting material feed (12.1, 12.2). 30

10. The reactor (10) according to one of the preceding claims, characterized in that it comprises a ring line on the outlet side, which connects a plurality of reactor elements (15.m) with respect to flow to the downstream plant region. S43-0048P-WO-AU/che/ 13.3.2013 34

11. The reactor (10) according to one of the preceding claims, characterized in that it comprises a fluid chamber (14), in the interior of which the reactor elements (15.m) including the redirection elements (30.k) are arranged. 5

12. The reactor (10) according to Claim 11, characterized in that the fluid chamber (14) can be charged with a fluid, to be able to provide an isothermal environmental condition depending on the situation. 10

13. The reactor (10) according to one of the preceding claims, characterized in that it is connected to a carbon oxide gas source, preferably a CO 2 gas source, and a hydrogen gas source.

14. A method for providing a storable and transportable hydrocarbon-containing 15 energy carrier (108) having the following steps: - providing (104) a gas having a carbon share (101) as a carbon supplier, - providing a hydrogen share (103), - providing a starting material (AS), which comprises the carbon share (101) and the hydrogen share (103), 20 - introducing and distributing the starting material (AS) by means of a shared starting material feed (12.1, 12.2) to a bundle of a plurality of the reactor elements (15.m), which are arranged parallel to one another, of a reactor (10), wherein a share of the starting material (AS) in one of the reactor elements (15.m) runs in each case through a reaction path, which 25 is composed of a first reactor pipe (20.1), which is equipped with a catalyst (60), at least one redirection element (30.1), which is equipped with an inert material (61), and a further reactor pipe (20.2), which is equipped with a catalyst (60), - providing the energy carrier (108) at an outlet-side end of the reactor 30 elements (15.m).

15. The method according to Claim 14, characterized in that an isothermal environmental condition is provided in a fluid chamber (14), which can be charged with a fluid. 35 S43-0048P-WO-AU/che/ 13.3.2013 35

16. The method according to Claim 14 or 15, characterized in that, before the introduction and distribution of the starting material (AS), the catalyst (60) in the reactor pipes (20.1, 20.2) is subjected to a reduction step for its activation, wherein the catalyst (60) experiences a volume reduction, which 5 is at least partially compensated for by slipping, filling, or sliding in of the inert material (61).

17. The method according to one of Claims 14 to 16, characterized in that the provision of the hydrogen share (103) is performed in that either 10 - a water electrolysis (105) is executed, in which the hydrogen share (103) is produced directly from water or an aqueous solution (H 2 0; 102), or - an energy carrier, which contains elementary silicon, is subjected to an oxidation reaction to produce the hydrogen share (103). 15

18. A use of a reactor (10) according to one of Claims 1 to 13 for the synthesis of methanol, wherein sections of the reactor element (15.m) are filled with the catalyst (60) and the redirection elements (30.k) are filled with inert material (61) before the initiation of the synthesis. 20

19. The use according to Claim 18, characterized in that each of the reactor elements (15.m) comprises at least one first reaction section, which is filled with a catalyst (60), at least one redirection element (30.1), which is filled with the inert material (61), and a further reaction section, which is filled with a catalyst (60). 25