EP2724081A2 - Method and installation for reducing greenhouse gases of fuels and combustibles - Google Patents

Abstract

The invention relates to a method and installations for reducing the greenhouse gases of fuels and combustibles and to the use of said fuels and combustibles as greenhouse-reduced energy carriers, especially as zero-greenhouse-gas-free fuels in transport. CO₂ from renewable sources is separated from pyrolysis gas and/or from flue gas and/or from biogas, and recuperated. The recuperated renewable CO₂ is put in a geological repository (sequestered). According to a second possible use, the recuperated renewable CO₂ replaces fossil CO₂ as a raw material. According to a third possible use, the renewable CO₂ is used as a raw material for the production of substantially greenhouse-gas-free synthetic fuels, replacing fossil fuels and thereby avoiding additional fossil greenhouse gas emissions. According to the first option of use, renewable CO₂ is removed from the environment, i.e. the atmospheric CO₂ content is actively reduced. According to the second option of use, fossil CO₂ is directly replaced by renewable CO₂, and according to the third option of use, the additional emission of fossil CO₂ and thus an increase in atmospheric CO₂ content is avoided. The greenhouse effects or greenhouse gas credits or greenhouse gas certificates produced by the three options of use are offset against the greenhouse gas emissions of fossil or renewable or synthetic fuels. The virtual-statistic offsetting of the greenhouse gas credits reduces the greenhouse gas emissions of these fuels, at best down to 0gCO₂ equivalent/MJ or down to 0gCO₂ equivalent/kWh or down to 0gCO₂ equivalent/km. Vehicles using such zero emission fuels will turn into exceptionally environmentally friendly zero emission vehicles, thereby allowing zero emission mobility without developing novel drive technologies.

Description

 Processes and plants for greenhouse gas reduction of power and heating fuels

State of the art

With carbon dioxide (C0 ₂ ), methane (CR »), nitrous oxide (N ₂ 0), the various fluorocarbons, sulfur hexafluoride (SF ₆ ), nitrogen trifluoride (NF ₃ ) and other gases, there is a whole range of climate-relevant greenhouse gases (im Following also GHG) with different climatic effect. Greenhouse gas effects are standardized and quantified using C0 ₂ equivalents. These are usually related to consumed energy units (eg gC0 ₂ -eq / kWh or gC0 ₂ -eq / MJ) or traveled distances (gC0 ₂ -eq / km). While the C0 ₂ values published by the automotive industry indicate the effective stoichiometric C0 ₂ emission from fuel combustion, environmental institutes and authorities additionally calculate the respective energy sources for C0 ₂ emissions over their entire development, ie over the entire lifecycle (Life Cycle Analysis LCA) or over the entire manufacturing path from the source of the energy source to the wheel of the car (well-to-wheel). For example, the LCA consideration of, for example, gasoline also includes the emissions of (fossil) C0 ₂ , which are generated in the process chain by the crude oil tankers, by the pipelines, by the refineries, by the power plants that generate the electricity required in the production line. and be caused by the gas stations.

In accordance with all national and international environmental authorities (such as the Intergovernmental Panel on Climate Change IPCC and the

UNFCCC = United Nations Framework Convention on Climate Change (UNFCCC) and state agencies (including the Federal Ministry for the Environment and the Federal Ministry of Finance), the C0 ₂ emissions of the various energy sources are described below over their entire development ie on the basis of a so-called life cycle analysis (LCA) or well to wheel (WtW).

In the transport sector, sensitivity to greenhouse gas emissions is highest. The respective C0 ₂ emissions per km must be specified in the European Union when selling automobiles. According to the EU decision, the taxation of fuels and vehicles will soon be C0 ₂ -oriented. Precisely because the GHG reduction in the transport sector is so difficult and cost-intensive, a GHG reduction is best rewarded here. Apart from that, GHG-reduced and GHG-free fuels are of course better for the environment than GHG-intensive fossil fuels.

Producers of greenhouse gas-reduced and, in particular, greenhouse gas-free fuels will be able to count on increased market demand in the future. According to EU Directive RED 2009/28 / EC of 23 April 2009, in each member state of the EU, by 2020, approx. 10% of the energy consumed by transport with fuels from renewable sources. Meanwhile, the German Federal Government has reinterpreted this goal in a GHG saving target of 7%. It is expected that the biogenic and synthetic fuels used in transport in 2020 will only reduce the GHG emissions of gasoline and diesel by an average of approx. 58% and not 100%, the share of renewable fuels will reach 12% in 2020 and not just 10%. By 2050, the German government is aiming for largely GHG-free traffic. Thus, the GHG reduction of fuels of all kinds is increasingly gaining (political) importance.

To achieve a largely GHG-free traffic, the fuel used must be GHG-free. In electric mobility, this is the case when GHG-free electricity is used, ie electricity from wind, solar, hydro or nuclear power as well as from geothermal energy (electricity from biomass is not necessarily GHG-free). When purchasing electric vehicles drivers have to accept not only considerable restrictions of comfort (vehicle size, payload, range, battery weight, charging infrastructure), but also high and very high acquisition costs, which will not (yet) be lower in the foreseeable future during the useful life of the electric vehicle Fuel or electricity costs can be compensated. The same is true for hydrogen vehicles, which, while less comfortable to pay, are still more expensive than electric vehicles and have the additional disadvantage that there is still no service station that can offer GHG-free hydrogen. The fossil fuels diesel and gasoline used to date in sophisticated combustion engine drives have the deficit that they are burdened to a significant extent with greenhouse gas emissions. This also applies to natural gas (CNG), liquefied petroleum gas (LPG), kerosene and heavy fuel oil.

Even the biofuels used as substitutes for fossil fuels in internal combustion engines and future synthetic fuels are not per se GHG-free or GHG-neutral energy sources, on the contrary they can be significantly polluted with greenhouse gas emissions. According to the LCA method, the greenhouse gas pollution is calculated as the sum of the greenhouse gas emissions of all energies or of all energy sources that are involved in the cultivation and harvesting of biomass, their storage, their transport, their conversion into marketable energy sources Storage and their distribution are used.

The EU Directive 2009/28 / EC shows how much of these emissions of GHG emissions are affected by a large number of biogenic and synthetic fuels and their various production routes, as well as by the average fossil fuels used in the EU. None of the biofuels listed in the Directive, nor any of the listed synthetic fuels, has an emission of 0 gC0 ₂ -eq / MJ or 0 gC0 ₂ -eq / kWh _H i. The best values are achieved with 10 gC0 ₂ -eq / MJ (36 gC0 ₂ -eq / kWhHi) of biodiesel from vegetable or animal waste oil and with 12 gC0 ₂ -eq / MJ (43.2 gC0 ₂ -eq / kWli _H i ) of biogas produced from dry manure. Of the so-called future fuels, synthetic diesel produced from waste wood by the Fischer-Tropsch process yields 4 gC0 ₂ -eq / MJ (14.4 gC0 ₂ -eq / kWhHi), DME produced from waste wood and methanol produced from waste wood to 5 gC0 ₂ -Äq / MJ (18 gC0 ₂ -eq / kWh _H i), Fischer Tropsch diesel produced from wood pulp to 6 gC0 ₂ -eq / MJ (21.6 gC0 ₂ -eq / kWhHi) and DME produced from timber and from Vegetable wood produced methanol to 7 gC0 ₂ eq / MJ (25.2 gC0 ₂ eq / kWh _H i). Ethanol produced from wheat straw reaches 11 gC0 ₂ eq / MJ (39.6 gC0 ₂ eq / kWl _H i). The EU Directive uses older, but now outdated, IPCC values when comparing these emission values with the GHG emissions of fossil fuels. According to the outdated IPCC values, on average, fossil gasoline and fossil diesel cause a GHG emission of 83.8 gC02 equivalents / MJ, which corresponds to 301.7 gC0 ₂ -eq / kWh _H j. According to recent IPCC figures from 2007, fossil gasoline pollutes the environment with 308.2 gC0 ₂ -eq / kWli _H i while fossil diesel fuel comes to a load of 320.2 gC0 ₂ -eq / kWh _H i. The updated average of gasoline and diesel yields a 4.1% higher THG emission of 314.2 gC0 ₂ -eq / kWh _H j. For fossil natural gas, the IPCC found an updated GHG emission of 244.6 gC0 ₂ -eq / kWh _H i in 2007 and an average GHG pollution of LPG from a mixture of fossil butane and fossil propane approx. 277 gC0 ₂ -eq / kWh _H i-

Although the GHG burden on transport is substantially reduced with the use of biofuels and even more so with the use of synthetic fuels, none of the fuels listed in the EU directive has so far achieved absolute GHG neutrality, ie GHG freedom, ie There is still no usable in internal combustion engines fuel with a GHG load of 0.0 gC0 ₂ -eq / MJ or of 0.0 gC0 ₂ -eq / kWh _H j.

In DE 102009018126 Al, the Center for Solar Energy and Hydrogen Research (ZSW) proposes an energy supply system in which a hydrogen production facility uses electricity from renewable sources, including electricity from biomass power plants for electrolysis in a known electrolysis unit and thus electrical energy from renewable sources chemically binds hydrogen in the energy carrier. This regenerative hydrogen is to be supplied to a conventional methanation reactor. In this Methanisierungsreaktor a C0 ₂ -containing gas is also passed, the C0 ₂ -containing gas among other things, fossil power plants and biogas plants can originate. The regenerative hydrogen and the C0 ₂ are to be synthesized according to the known Sabatier process to methane. Gas service stations can be part of such an energy supply system. DE4332789A1, DE102004030717A1 and DE102009007567 disclose very similar systems. Once realized, such power systems can safely supply the market with renewable and / or regenerative fuel. However, it is not guaranteed that the regenerative fuel is also 100% GHG-free. If, for example, fossil CO _{2 has} entered into the methanol or methane fuel, eg from a coal-fired power plant and / or THG-contaminated electricity, for example from a maize-operated biogas plant, the methane fuel may well be contaminated with greenhouse gas emissions, possibly in considerable extent. Moreover, the published patent applications DE102009018126 A1, DE4332789A1 and DE 102009007567 relate to the property of the renewability of the energy and energy sources produced and not to the property of the GHG reduction power or the GHG emission of these energies and energy carriers. As stated above, these two properties may well fall apart.

There are currently several techniques for extracting fossil C0 ₂ from the flue gases of combustion plants, particularly fossil-fueled or fossil-fueled large power plants, in development. The published specifications US2007 / 0178035A1 (White / Allam), DE102008062497A1 (Linde-KCA-Dresden) and DE 102009043499 Al (Uhde) show this by way of example. A second technique for extracting or separating C0 ₂ from the main process of combustion of the energy sources used (usually fossil coal or fossil natural gas) is the combustion in an oxygen atmosphere (oxyfuel process). The flue gas of this process consists almost exclusively of C0 ₂ and water vapor. The steam is relatively easily removed by condensation from the flue gas, so that highly concentrated C0 ₂ remains. A third technique for the isolation of C0 ₂ is realized with so-called IGCC power plants (Integrated Gasification Combined Cycle), which uses fossil fuels such as coal, but also regenerative energy sources such as biomass or waste by partial gasoline partial oxidation -) Convert gas consisting essentially of hydrogen and CO. By means of suitable catalysts, the CO is allowed to react under high pressure with steam to C0 ₂ and hydrogen. At pressures of up to 70 bar, the CO ₂ can be relatively easily absorbed from the gas mixture by one of the known methods of gas scrubbing (inter alia pressure swing adsorption). tion of amine washing and cryogenic processes. The (fuel) gas is usually emitted, but it can also produce pure hydrogen, methanol, ethanol or synthetic methane, octane, propane and butane. This third technique of C0 ₂ separation is called pre-combustion capture because the C0 ₂ is removed from the process before the (combustion) gas is used.

The extracted according to one of the techniques listed above fossil C0 ₂ is usually fed to a geological disposal (so-called CCS method, Carbon Dioxide Capture and Storage). The additional and additional pollution of the environment with fossil C0 ₂ should be reduced and ideally avoided in the ideal case. Complete collection and disposal of fossil fuels

However, for fossil fuels C0 ₂ s is not possible for technical and economic reasons. This means that even when using the best CCS processes, there is always a C0 ₂ slip, which is between 2% and 20% of C0 ₂ emissions and thus further increases the CO ₂ content in the atmosphere. The CCS techniques that have been designed and planned to date can therefore neither represent absolutely THG-free coal or natural gas flows nor absolutely THG-free fuels such as hydrogen, methanol, ethanol or synthetic methane, butane, octane or propane.

Although in Germany alone over 250 biomass (heating) power plants are operated with renewable energy sources such as woodchips and / or wood pellets that emit not fossil but regenerative C0 ₂ , and although in Germany alone over 50 biogas plants separate renewable C0 ₂ from biogas ( and feed the resulting bio-methane into the national natural gas grid) and some biomass-based IGCC power plants also use biomass as BIGCC plants, it was not until the patent applications DE102010008287.2, DE102010017818.7 and PCT EP2011 / 000748 inventor CCS- Technique designed to recuperate C0 ₂ from regenerative sources (regenerative C0 ₂ ) and to geological final storage (sequestration) or replace it with the recuperated regenerative C0 ₂ fossil C0 ₂ . Also, no methods are known with which the positive environmental effects of the material substitution of fossil C0 ₂ s by regenerative C0 ₂ or the positive environmental effects of the substitution of fossil fuels by GHG-free synthetic fuels or the positive environmental effects of the reduction of the atmospheric C0 ₂ content to (other) GHG-contaminated fuels. In particular, no methods are known in which the transmission is designed so that the GHG balance of these fuels to be relieved reaches a value of <= 0 gC0 ₂ -eq / MJ or <= 0 gC0 ₂ -eq / kWh _H i.

For the first time, DE 102010017818.7 (Feldmann) and PCT / EP2011 / 000748 (Feldmann) describe, among other things, a process and installations for producing greenhouse gas-reduced biogas for its processing into greenhouse gas-negative bio-methane and regenerative CO ₂ for mixing greenhouse-gas-negative bio-methane and natural gas (CNG) to a greenhouse gas-free mixed gas and the use of the greenhouse gas-negative bio methane and / or the greenhouse gas-free mixed gas as greenhouse gas-negative or greenhouse gas-free energy sources, in particular as greenhouse gas-negative or greenhouse gas-free fuels in traffic. However, it does not describe how the GHG emissions of other fuels than the bio-methane produced in the plant could be reduced, in particular the GHG emissions of fossil or foreign biogenic or synthetic fuels.

task

The invention is therefore based on the object to eliminate the lack of GHG pollution as many fuels, especially of fuels that are used in traffic. It is necessary to define a process and systems or systems (plant configurations) that reduce additional GHG emissions due to fuel use, beyond what is possible simply by switching from fossil fuels to biofuels or to synthetic fuels. Preferably, the GHG emission attributable to the use of fuel should be reduced to such an extent that these fuels become at least absolutely GHG-free and the respective GHG load has a value of <= 0 gC0 ₂ -Eq / MJ and thus also < = 0 gC0 ₂ - eq / kWliHi reached. As fuel to be relieved, all fossil, biogenic and synthetic fuels should be considered. solution

 This object is achieved with regard to the method essentially by the invention described in claim 1 and with respect to the system essentially by the invention described in claim 11. The inventions are based on the prior art disclosures DE102010017818.7 and PCT EP2011 / 000748 of the inventor, these writings are not geared to the use of GHG effects for improving the GHG balance of foreign, not generated in the plant fuels. Rather, they relate exclusively to the improvement of the GHG pollution of biogas or bio methane, which is produced by the process described therein or in a plant described therein.

The method disclosed here, which is aimed at improving the GHG balance of fuels of all kinds, in particular the improvement of the GHG balance of foreign fuels, consists of a total of 10 process steps with full utilization of all possibilities of execution and expansion. It comprises in detail process steps 1) "Selection of the energy sources to be used", 2) "Conversion to C0 ₂ - containing gases", 3.) "Separation of the regenerative C0 ₂ s", 4.) "Recuperation of the regenerative C0 ₂ s ", 5.)" liquefaction of the recuperated regenerative C0 ₂ s ", 6.)" interim storage of the recuperated regenerative C0 ₂ s ", 7.)" transport ", 8.)" use of the regenerative C0 ₂ s " , 9.) "Balancing the meta-system" environment "and 10.)" Use of the relieved fuels in traffic "or" Use of the relieved fuels for heat or power generation ".

The process steps "Recuperation of the regenerative C0 ₂ s", "Use of the regenerative C0 ₂ s", "Balancing the meta-system" environment "and" Use of the relieved fuels in traffic "- as will be explained below - central elements of the invention represents.

Process step 1. "Selection of the energy sources to be used": The selection of non-fossil energy sources for use in conversion processes, which are aimed at the generation of marketable energy sources, is not new: every biomass (heating) power plant and every biogas plant geared to the emission fossil C0 ₂ s to avoid. The inventory of atmospheric C0 ₂ in the meta-system "environment" should not be increased any further.In the core process of chemical, stoichiometric conversion, this always succeeds when the raw materials used are of non-fossil nature, eg consisting of biomass or waste . Both the C0 produced as biogas fraction in the Vergä- tion ₂ and the C0 ₂ that is produced during the subsequent use of to BioMethan treated biogas, as well as the resulting from the combustion of biomass C0 ₂ is in terms of its effects on the climate completely harmless it was still in the atmosphere 1 to 40 years ago and thus in the meta-system "environment" before it was taken up by the plants via the photosynthesis process.

For the regenerative C0 ₂ used in process step 8.) to be able to achieve its positive THG effect, it is imperative for the entire process that such primary energy carriers and other harmless starting materials harmless for the meta-system "environment" be used (cf. Claim 1)., Process step 2.) "Conversion to CCb-containing gases": The usual conversion methods of combustion, fermentation and gasification of non-fossil fuels do not have the production of C0 ₂ to the main goal, they are usually rather the conversion of non or Low-energy energy sources (eg corn, grass and solid manure) into marketable energy sources (eg bio-methane) and / or the direct conversion of energy sources that are not marketable or less marketable (wood residues, woodchips) into marketable electrical or thermal energy. C0 ₂ thereby falls only as by-value or worthless waste product. Therefore, C0 ₂ resulting from incineration, fermentation and gasification is usually simply emitted into the meta-system "environment." If C0 _{2 is} required in bulk for industrial use, it is usually recovered as a by-product of other industrial processes a) in the industrial combustion of coke with (excess) air, b) in the industrial gasification of coal, c) in industrial ammonia synthesis, d) in industrial methanol production and e) in industrial lime burning. The fact that the required carbon comes from fossil sources is obvious in the production processes a) and b). But also in the production of ammonia C0 ₂ has fossil origins: while for the running under high pressure and high temperature reaction N ₂ + 3 H ₂ »> 2 NH ₃ nitrogen is separated by cryogenic technology by air liquefaction or air separation is the hydrogen required by steam reforming is also produced from natural gas or from coal or from the petroleum fraction naphtha. C0 _{2 is produced} in synthesis gas production as a product of the water-gas shift reaction. For use in ammonia synthesis, the C0 _{2 is} previously washed out of the process gas, for example by the Rectisol process. C0 ₂ is therefore available in relatively large amounts in relatively pure form (after separation of the C0 ₂ s, the hydrogen is mixed in the required ratio with nitrogen and synthesized to ammonia). Due to the use of the fossil feedstocks natural gas, coal or petroleum, the CO _2, which is a by-product of ammonia synthesis, also has fossil origins. The industrial production of methanol (CH ₄ O) occurs almost exclusively with catalysts under high pressure and high temperatures from syngas, a mixture of carbon monoxide and hydrogen (in the ratio of about 1: 2). Reaction formula: CO + 2 H ₂ »> CH ₃ OH. As described above, the synthesis gas required for methanol synthesis can be produced from fossil feedstocks such as coal, petroleum fractions and peat, but also from renewable raw materials such as wood, straw and other biomass, as well as from biogas, waste or sewage sludge. However, steam reforming and partial oxidation of natural gas are common. Coal and natural gas are the major sources of synthesis gas in the industrial production of methanol worldwide. In Germany, about 2 million tons of methanol were produced in 2000, of which about 1.4 million tons or approx. 70% from fossil residual oils. The resulting in the syngas production C0 ₂ is washed out as in the ammonia synthesis before synthesis from the process gas. Thus, C0 ₂ , which is produced in relatively large amounts as a by-product of methanol synthesis and is available in relatively pure form, usually has fossil origins. Lime burning is the decomposition of calcium carbonate to calcium oxide and C0 ₂ . The reaction CaC0 ₃ »> C0 ₂ + CaO takes place at a temperature between 900 and 1,300 ° C. In industrial production, CaC0 ₃ is supplied in the form of fossil limestones from a limestone quarry and heated to about 900-1300 ° C in vertically operating ring or shaft furnaces or in rotary kilns or in eddy current furnaces. The ovens are charged with a mixture of 90% limestone and 10% coke. Both feedstocks originate from fossil deposits. Thus, C0 ₂ , which is a byproduct of lime burning, has fossil origins.

All for the industrial production of C0 ₂ used method so use fossil fuels or substances, that is, the material used in industrial C0 ₂ is usually of fossil nature. With fossil C0 ₂ , no positive GHG effects can be achieved, so you can not replace other fossil C0 ₂ with positive environmental effects material. The commonly used methods are therefore not suitable for generating large amounts of unloaded C0 ₂ quantities. What is needed is a process that uses non-fossil feedstocks and energy sources as described in process step 1.). These conditions are met only by the anaerobic digestion of biomass and possibly also of organic waste, the combustion of biomass and possibly also of organic waste and the gasification of biomass and possibly also of organic waste. Therefore, besides the appropriate selection of the starting materials, the process necessarily includes the selection of these conversion methods listed here (see claim 1).

Step 3) "Separation of the regenerative CO2S".. In the conversion processes of gasification, the extraction of the resulting C0 ₂ is s need to be limited by the requirement -free the subsequent process, C0 _2, necessarily Vergasungsanla- gene without C0 ₂ are -Separation If a non-fossil primary energy source such as biomass is used as a raw material, the separated C0 ₂ fulfills the precondition of regenerative origin and it is in the desired concentrated form after separation, the more concentrated the C0 ₂ is Less technical and energetic effort must be made in the subsequent liquefaction or solidification steps, since the gas mass flow to be cooled will then be smaller, which is why Advantage, if the C0 ₂ supplying gasification plant uses non-fossil primary energy sources as raw material and if the regenerative C0 _{2 is} supplied in the highest possible concentration.

For the separation of C0 ₂ from the process gas, several known methods can be used, for example the membrane permeation process, the pressure-swing adsorption process (with PSA plants), the absorption process (with MEA plants) and cryogenic processes , Each method has its specific advantages and disadvantages.

In the conversion process of anaerobic digestion biomass is converted by the activity of various bacterial strains substantially into C0 ₂ and methane. Since anaerobic fermentation always uses non-fossil organic feedstocks as fermentation substrates, the CO ₂ produced by the bacteria is regenerative. Extraction of the regenerative C0 ₂ s produced in the bacterial process is only necessary if the C0 ₂ -containing biogas is to be treated as BioMethan and fed into a natural gas grid. However, around 98% of German biogas plants currently use the produced C0 ₂ -containing biogas directly as fuel for electricity generation in generator sets (CHP) without C0 ₂ separation.

For the separation of C0 ₂ from the biogas, the known methods can be used, for example the membrane / permeation process, the pressure-swing adsorption process (with PSA plants), the absorption process (with MEA plants) and cryogenic digestion. drive.

The regenerative C0 ₂ contained in the biogas can be extracted from the biogas before it is converted into electricity. However, this is associated with significant additional overhead, since power plants (CHP) can also be operated with biogas and biogas plants usually have only low capacity and it is not worthwhile to provide gas scrubbing equipment for small plants. In addition, the "production" of regenerative C0 ₂ part of the process of the invention would. In order to keep the inventive method as lean and effective, it is advantageous to avoid this possible. As a supplier of renewable C0 ₂ s are therefore preferably the biogas plants selected anyway the biogas already prepare to To get bio methane. These are all biogas plants that feed into the natural gas grid and biogas plants that supply liquid bio methane or pressurized bio methane with suitable means of transport (pipeline, mobile pressurized gas containers, mobile liquid gas tanks). The technical and energy costs of the separation can be omitted in the inclusion anyway already preparing biogas plants, which is beneficial for the users of the method described here. However, it should be expressly pointed out that the inclusion of the "production" of the regenerative C0 ₂ s should be protected in the process of the invention.

In the conversion process of combustion, the extraction of C0 _{2 is} so far uncommon, especially if the raw materials used are regenerative nature. For example, in contrast to coal and gas power plants, biomass cogeneration plants are considered to be particularly environmentally friendly because they only emit regenerative C0 _{2, which is} harmless to the meta-system "environment." C0 ₂ separation, which involves considerable additional investment, additional costs and efficiency losses, is therefore indeed for coal-fired power plants The separation of renewable C0 ₂ would have to be decidedly performed, it would be part of the process, which is technically possible, but only secondarily, the significant additional technical effort and additional cost of a stand-alone C0 ₂ - Separation should preferably be avoided, the process step of the separation being characterized, inter alia, by the fact that it is preferably carried out by the suppliers of the regenerative C0 ₂ s (cf claim 2) The known processes are used for the separation of CO ₂ from the flue gas Question, eg the membrane / permeation process, the pressure-swing adsorption process (with PSA plants), the absorption process (with MEA plants), cryogenic processes and the oxy-fuel process.

Process Step 4.) "Recuperation of the regenerative CCbs": So far, it is common in almost all biomass utilizing incineration, gasification and fermentation plants to discharge the separated (regenerative) C0 ₂ into the atmosphere - which, as stated above, not harmful to the meta system is "environment". This applies in particular to the operators of biogas plants feeding into the natural gas grid, which separated them C0 ₂ usually considered worthless waste. The special feature of the method disclosed here is the recognition that this (regenerative) C0 ₂ can certainly be of value, namely, when used as shown here.

The separated in the plants regenerative C0 ₂ is therefore not, as is customary today, released into the atmosphere and thus returned to the (short-term) C0 ₂ cycle, but collected (recuperated) and possibly stored. The C0 ₂ precipitation and the C0 ₂ recuperation can be combined in one plant. The recuperation regenerative C0 ₂ s is therefore a novelty, especially in combination with the other process steps. Process step 5) "Liquefaction of the recuperated regenerative CC s": In order to be able to better store and transport the recuperated regenerative C0 ₂ it is advantageous to liquefy it The apparatus complexity and the costs of a gaseous handling would be significantly higher However, the process step is not absolutely necessary, it can also be skipped, for example if the use is relatively close to the location of the CO ₂ production or separation and in this case the means of transport "gas pipeline" is more cost-effective.

Process step 6.) "Interim storage of the recuperated regenerative CQ? S": The recuperated C0 ₂ gas volume flow will generally fluctuate and therefore not coincide with the decrease It is therefore advantageous, but not absolutely necessary, between the separation and the transport to provide a buffering in the form of at least one temporary storage (see claims 1 and 11).

Process step 7) "Transport": The recuperated regenerative CO ₂ is physically transported from the place of recuperation or intermediate storage to the place of use, which can be transported by truck and / or by ship and / or by rail and / or by pipeline.

Process step 8) "Use of the regenerative CO ₂ s": The use of the regenerative CO ₂ s determines which GHG effect is achieved in the meta-system "environment". In order to achieve a positive GHG effect, 3 usage options are provided. see: A) sequestration of the regenerative C0 ₂ s, B) Substitution of fossil C0 ₂ s, C) use of the regenerative C0 ₂ s for the production of synthetic fuels.

During the sequestration of the regenerative CO, the C0 _{2 is} geologically demolished (sequestered) and thus removed from the meta-system "environment." The segregation removes regenerative C0 ₂ from the short-term C0 ₂ cycle, which is significantly more is considered to be a mere avoidance of further additional GHG emissions into the meta-system "environment" as the C0 ₂ level of the atmosphere is actively lowered. If this reduction in the atmospheric CO ₂ level of a small amount of fuel is taken into account (see process step 9), this can be relieved to such an extent that its GHG burden is not only reduced or brought to zero, but even negative. This is of particular advantage when it comes to the dual use of fuel. In the case of dual-fuel concepts, for example, it is possible to use methane as gas and / or methane as liquid on the one hand and diesel or biodiesel on the other hand in dual-fuel trucks. If the methane has a negative GHG balance, it can compensate for the positive GHG balance of diesel or biodiesel so that the trucks are ultimately GHG-free despite the use of polluted fuels.

Would at the material substitution replaces regenerative and innocuous C0 ₂ fossil and thus harmful C0 _2, which would otherwise enter the meta-system "environment" and increase the C0 ₂ backlog the atmosphere and thus would have harmful effects. The fossil C0 ₂ must no longer be generated for industrial application, an additional burden on the meta-system "environment" is avoided. Although this does not lower the atmospheric CC ^ level, at least there is no further increase in this stock. When using the regenerative CC s for the production of synthetic fuels, the regenerative C0 _{2 is introduced} into one of the conventional reforming processes, in which it is treated to a regenerative synthetic fuel, preferably according to the known Sabatier process to synthetic methane (CH ₄ ) or according to the other known methods (eg steam reforming, Bertau / Pätzold / Singliar method) to synthetic methanol (CH ₃ OH), ethanol or to synthetic Me- than, octane, butane or propane. It is an advantage if the required hydrogen is obtained by electrolysis from GHG-free electricity, so that it leads to minimal GHG emissions and does not cancel out the GHG effects generated by the use of regenerative C0 ₂ s by using fossil energy be made (see DE 102004030717A1, DE102009 018126A1 and DE4332789A1).

When the C0 ₂ reforming or the Sabatier process releases synthetic fuels, these synthetic fuels replace fossil fuels, which avoids the additional emission of additional additional GHG into the atmosphere and thus into the meta-system "environment", which (additional) GHG Emission is then almost zero Step 9.) Balancing the Meta-System "Environment": As with the sale of BioMethan feeds into the natural gas grid and from green electricity feeds into the grid, no physical transfers of exactly the same gas or electricity from the sellers (feeders) to the buyers (feeders / users), but only virtual-statistical offsetting of the corresponding energy quantities, the achieved reductions of the physically indefinable atmospheric C0 ₂ stock of the meta-system "environment" and / or the reductions achieved in additional GHG emissions in this process according to the invention virtually statistically offset against the GHG emissions of the fuels to be relieved. This balance of the meta-system "environment" is fuel-specific according to the following inventive algorithm (see claims 10 and 20):

MK "= (RC0 ₂ ./. ECC- _2- egg · /. EC0 _2-th ./ EC0 _2-otherwise ) / (C0 ₂ -kn. /. C0 ₂ -ZB _K ") where

MK _n maximum energy quantity of fuel n, measured in kWh _H j

or MJ, which can be brought to the target load C0 ₂ -ZBKn;

RC0 ₂ Recuperated amount of regenerative C0 ₂ , measured in t C0 ₂ -eq,

C0 ₂ emissions, measured in t C0 ₂ -eq, which arise after the recuperation of the regenerative C0 ₂ s through the use of electrical energy;

EC0 _2-th C0 ₂ emissions, measured in t C0 ₂ -eq, which arise after the recuperation of the regenerative C0 ₂ s through the use of thermal energy; EC0 ₂ . _S onst ⁼ other C0 ₂ emissions, measured in t C0 ₂ -eq, which arise after the regeneration of the regenerative C0 ₂ s;

C0 _2- Kn ⁼ LCA-THG load of the fuel to be discharged n, measured before the discharge in gC0 ₂ -eq / kWh _H i or in gC0 ₂ -eq / MJ;

C0 ₂ -ZBi n ⁼ GHG target load of the fuel to be discharged n, measured after the discharge in gC0 ₂ -eq / kWh _H i or in gC0 ₂ -eq / MJ;

If, for example, from a biogas plant operated with conventional fermentation substrates (maize, grass, manure, cereal crop cut) in step 4.) "Recuperation" 5,600 1 regenerative C0 ₂ s recuperated and in the following process steps 5.) to 8.) C0 ₂ emissions, eg through the use of 56,000 kWhei of electricity from the German electricity mix for the control of the liquefaction plant and through the consumption of 2,240,000 kWha, heat from natural gas for the liquefaction of the recuperated regenerative C0 _2s and through the use of 593,000 kWhHi diesel fuel for the transport of the liquefied C0 ₂ s by truck, then the chargeable C0 ₂ quantity is reduced to 4,827.3 t / a.

The German power mix is burdened with 624 gC0 ₂ -eq / kWhei, the consumption of 56,000 kWhei from the power grid pollutes the environment with consequently 34.9 tC0 ₂ . With an LCA load of natural gas of 244.6 gC0 ₂ / kWliHi, the heat input of 2,240,000 kWh _th results in a further load of 547.9 tC0 ₂ . When using 593,000 _H i kWh on diesel fuel, which is loaded with 320.2 GC0 ₂ / kWh _Hi, further 189.9 TC0 ₂ arise. Of the originally recuperated C0 ₂ amount of 5,600 1 remain according to the above formula still approx. 4,827.3 t C0 ₂ chargeable (5,600 tC0 ₂ ./. 34.9 tC0 ₂ ./. 547.9 tC0 ₂ ./. 189.9 tC0 ₂ = 4,827.3 tC0 ₂ ).

The fuel to be relieved is fossil natural gas and the target load is 0.0 gC0 ₂ / kWh _H i- According to the algorithm part (C0 _{2- n} ./. C0 ₂ -ZBi n) 244.6 gC0 ₂ / kWh _Hi ./. 0.0 gC0 ₂ / kWh _H i = 244.6 gC0 ₂ / kWh _H i needed for a corresponding GHG discharge of the natural gas. With the qualifying C0 ₂ amount of 4,827.3 t C0 ₂ ie up to 19,735,487 kWhni fossil natural gas is converted to an absolute GHG-free fuel. Accordingly, the GHG burden of all fossil, biogenic and synthetic fuels whose LCA-GG load is known can be reduced, preferably to zero, and more preferably to <zero. The maximum loadable fuel quantities result from the algorithm according to the invention.

According to the method of the invention, it is possible to convert any fuel into an absolutely THG-free fuel. It is thus possible to offer absolutely C0 ₂ -free gasoline, absolutely C0 ₂ -free diesel fuel, absolutely THG-free kerosene, absolutely C0 ₂ -free natural gas, absolutely C0 ₂ -free liquefied petroleum gas, absolutely GHG-free heavy oil and also absolutely C0 ₂ -free biofuels and absolutely THG-free synthetic fuels. The respectively available GHG-reduced fuel quantity is greater, the lower the initial LCA-GHG load of the fuel to be relieved and vice versa. With an anticipated C0 ₂ amount of 4,827.3 t, due to its higher initial LCA-THG load of 308.2 gC0 ₂ / kWh _H i, only 15,662,881 kWli _H i of gasoline can be relieved to absolute GHG-free gasoline yields. By contrast, with the allowable tonnage of 4,827.3 t C0 ₂ , an amount of up to 121,901,515 kWh of Fischer-Tropsch diesel produced from timber could be converted into a zero-emission fuel, ie a factor of 7 , 8 larger fuel quantity.

On balance, this method either does not further increase the effective C0 ₂ level of the meta-system "environment" or further reduce the emission of additional fossil C0 _2. Step lO.a) "Use of Released Fuels in Transport": As has been shown above, apart from absolutely THG-free bio-methane (from DE 102010 017818.7 and PCT / EP2011 / 000748), no other fuels are known which have the property of absolute GHG-freedom. With the method according to the invention, it becomes possible for the first time to make every fuel an extremely environmentally friendly zero-emission fuel. When such zero-emission fuel is used in transport, zero-emission mobility is provided, without changing the established propulsion technologies or replacing them with other propulsion technologies (electric or hydrogen propulsion) and without the need to build new gas station infrastructures. A particular advantage of this method step is that the positive environmental effects are immediately effective over the entire vehicle stock can and should not be waited to full effectiveness on the complete replacement of the old vehicle stock by new vehicles.

Of all the process steps and measures, the sequestration of regenerative C0 _{2 has} the greatest effect on the GHG balances of the process or on the energy products obtained by the process. This is not a computational assignment, the C0 ₂ is rather physically stored in deep geological formations. The effective C0 ₂ reduction (final removal of C0 ₂ from the atmospheric C0 ₂ cycle of the meta-system "environment") is attributed to any fuel and not only GHG-free fuels with a GHG reduction of 100% but also by this method by 0.01% to 99.99% GHG-reduced fuels and fuels whose GHG emission was reduced by> 100%.

Process lO.b) "Other uses of the relieved fuels": The GHG-relieved fuel or fuels can not only be used in traffic, but also as GHG-reduced or as GHG-free heating fuels and for the production of GHG-reduced or THG-free electricity.

The inventive method includes the control and regulation of the respective sub-processes and the overall process. These are implemented in the usual way as system or system control and are therefore not explained in detail.

Achieved benefits

If implemented with all steps, fuel can be provided and used with the method disclosed here without increasing the (atmospheric) CO ₂ inventory of the meta-system "environment." Alternatively, the emission of fossil C0 ₂ into the meta system "environment" by the emission of regenerative C0 ₂ . These fuels can be used in traffic. Without having to significantly change or further develop automotive technology (ie neither the product nor the production plants), the use of absolutely THG-free fuels makes zero-emission mobility possible, possibly even GHG-negative mobility. The international automotive industry can still build cars with internal combustion engines, without having to change the technology, the GHG freedom of mobility is achieved through fuel.

The disadvantages of possibly also CO ₂ -free electromobility such as short range, long charging times, high battery weight, very high additional acquisition costs, problematic heating in winter and problematic air conditioning in summer, investment in new production lines, high R & D expenditure etc. etc Do not occur in this case. Neither has the sophisticated combustion engine technology to be switched to an electric motor technology, nor high-performance batteries must be developed, produced and paid. GHG emissions caused thereby can be avoided.

Also against. hydrogen technology currently considered as a last resort, the method and use described herein have advantages; since the acquisition cost of hydrogen cars today compared. comparable gasoline vehicles at 50,000 euros and more and these amount to electric cars to 10,000 to 40,000 euros, can hardly compensate for a car with these new drives during its usual useful life, this cost disadvantage by cost advantages in fuel consumption. With CNG drives, the additional purchase costs only amount to between € 0 and € 4,000 per car and the break-ment points are already reached after a journey of between 0 and 30,000 km.

The "production" of THG-reduced or THG-free fuels is thus of advantage for the automotive industry, its employees, car buyers and users and last but not least for the environment.

Detailed description

For a better understanding of the present invention, reference will be made below to exemplary embodiments which are described on the basis of subject-specific terminology. It should be noted, however, that the scope of the inventions is not intended to be limited by the specification of exemplary embodiments, since changes and modifications to the disclosed method and to the disclosed system and to its variants and further applications of the inventions and other uses of the recuperated regenerative CO2S are considered as current current or future expertise of a person skilled in the art ,

Figures 1 to 5 show exemplary embodiments of the method according to the invention, wherein the rectangles represent substances and products and rectangles with cut corners processes or process steps.

 FIG. 1 shows a schematic block diagram of the method steps for improving the GHG balance of any fuels in all possible variants

FIG. 2 shows an alternative embodiment of the method in which the intermediate storage of the recuperated regenerative C0 ₂ s is dispensed with.

FIG. 3 shows a further embodiment variant of the method illustrated in FIG. 1, in which the regenerative CO _{2 is obtained} exclusively by the conversion method of anaerobic fermentation and in which the unused process options are no longer shown.

FIG. 4 shows an embodiment variant of the method illustrated in FIG. 1, in which the regenerative CO _{2 is obtained} exclusively by the gasification conversion method.

FIG. 5 shows an alternative embodiment of the method illustrated in FIG. 1, in which the regenerative CO _{2 is obtained} exclusively by the combustion conversion method.

FIGS. 6 to 10 show exemplary embodiments of the possible system configuration. In the figures 6 to 10 plants or devices are shown as a rectangle with cut off corners and fabrics or products as a rectangle.

FIG. 6 shows a general schematic block diagram of the plant components which are or may be required for carrying out the method according to the invention. FIG. 7 shows an alternative embodiment of the system from FIG. 6, in which the temporary storage of the recuperated regenerative C0 ₂ s is dispensed with.

FIG. 8 shows an embodiment variant of the plant from FIG. 6, in which the conversion of the starting materials and the recovery of the regenerative C0 ₂ s take place in a fermentation plant; the unused plant components are no longer displayed.

FIG. 9 shows an embodiment variant of the installation from FIG. 6, in which the conversion of the starting materials and the recovery of the regenerative C0 ₂ s take place in a firing plant.

FIG. 10 shows a variant embodiment of the plant from FIG. 6, in which the conversion of the starting materials and the recovery of the regenerative C0 ₂ s take place in a gasification plant.

In Figure 1, the rectangles 1 to 9 represent the usual starting materials for the production of C0 ₂ , both the fossil feedstocks and the regenerative feedstocks. The rectangle with the reference numeral 1 is propane, the reference numeral 2 refers to butane, 3 to petroleum fractions such as Naphta, 4 to natural gas, 5 to fossil coal, 6 to biomass, 7 to hydrocarbon waste, 8 to organic waste and 9 on farmyard manure (see list of references).

From those possible starting materials in step 1 (reference numeral 10) those starting materials are selected with which regenerative C0 ₂ can be produced, namely at least THG-reduced, preferably GHG-free biomass (1 1) and / or at least THG-reduced, preferably GHG -free waste (12) and / or at least THG-reduced, preferably GHG-free farm fertilizer (13) and / or at least THG-reduced, preferably GHG-free organic waste (14).

In method step 2 (reference numerals 15, 16 and 17), the selected ingredients are converted into C0 ₂ -containing mixed gases. Gasification (15), anaerobic digestion (16) and incineration (17) are the possible conversion methods. When using the conversion process of the gasification (15) is formed as a mixed gas pyrolysis gas (19), which is composed of regenerative C0 ₂ and synthesis gas. Using the conversion process of anaerobic digestion (16) produces the Mixed gas Biogas (20), which consists of regenerative C0 ₂ , methane and associated gases. When using the conversion process of the combustion (17), the mixed gas flue gas (21), which consists essentially of regenerative C0 ₂ , CO, NO _x , 0 ₂ , N and other associated gases. In process step 3 (22), mixed gas-specific technology is used to concentrate or extract the regenerative CO ₂ contained in all of the mixed gases listed and to make it available for further use. The aim is to recover concentrated regenerative C0 ₂ (23 and 24) and separate them from the associated gases (18). To extract the C0 ₂ from the mixed gas "pyrolysis", one of the conventional gas cleaning or Gasextrahierungsverfahren is such as the Recti- used sol method or pressure washing with water or the pressure-amine scrubbing or a cryogenic methods. To the C0 ₂ from the Extracting mixed gas "biogas" is also one of the usual gas treatment processes used (see above). In order to separate the C0 ₂ from the mixed gas "flue gas", one of the suitable gas extraction process is used, in addition to those already mentioned possibly also the oxyfuel process (not shown), in which before the combustion of the feedstock an air separation takes place and for the combustion of the feedstock is largely used oxygen, so that the flue gas is largely nitrogen-free and the C0 ₂ concentration in the flue gas high or even very high with the further consequence that the cost of C0 ₂ extraction is relatively low.

The greatest possible part of the regenerative C0 ₂ s is supplied to process step 4 (recuperation, reference numeral 25). The proportion of regenerative C0 ₂ s to be recuperated results from the desired cost / benefit ratio in the separation, because the additional equipment required in each case increases with increasing degree of extraction (increasing marginal expenditure).

The recuperated regenerative C0 ₂ (26) is liquefied in step 5 (27, 28) or converted into the solid state or initially left in the gaseous state. The liquefaction of C0 ₂ s is carried out according to the prior art with cryogenic processes in suitable equipment. To solidify the C0 ₂ , the liquefied C0 ₂ is further cooled. The liquefaction and solidification are beneficial because themselves The C0 ₂ in liquid and solid state (not shown) better store and transport.

The gaseous and / or liquefied and / or solidified regenerative C0 ₂ (not shown) is intermediately stored in process step 6 (29) in pressure tanks or in liquefied gas tanks or in isolated cold stores until they are transported to the place of use or to the site of sequestration. Intermediate storage is required because the fluctuating volume flow of C0 ₂ generation usually does not correspond to the fluctuating volume flow of the use. In this respect, the intermediate storage performs the function of a buffer. In step 7 (30), the recuperated regenerative C0 ₂ (not shown) is transported by appropriate means to the site of use or sequestration. Preferably, GHG-reduced fuel is used, particularly preferably GHG-free fuel and in particular GHG-negative fuel. The use of these fuels prevents the GHG balance of the transported C0 ₂ s from deteriorating.

Process 8 (31, 32, 33) involves the use of the recuperated regenerative C0 ₂ s. The options include sequestration (31), material substitution of fossil C0s (32) and use as feedstock for the production of synthetic fuels such as synthetic methane, synthetic octane, synthetic butane and synthetic propane or synthetic methanol and synthetic ethanol , In all options, the atmospheric inventory of C0 _{2 is} reduced or at least not further increased: the sequestration regenerative C0 ₂ s decreases the atmospheric C0 ₂ inventory, the material substitution forces back the use of fossil C0 ₂ s and synthetic fuels produced from regenerative C0 ₂ Substitute fossil fuels, which also results in a reduction in the emission of fossil C0 ₂ s or corresponding greenhouse gases.

In process step 9 (34), the reduction of the atmospheric CO ₂ level (not shown) and / or the reduction of fossil CO ₂ emissions (or corresponding greenhouse gases) (not shown) with the CO ₂ emissions (or the THG -Emis- ions) of the selected fuels, resulting in a virtual statistical GHG relief (not shown) of the at least one selected fuel (35). The maximum amount of fuel that can be relieved is given by the formula given above. In method step 10 (36, 37) it is determined how the unloaded fuel (35) is used. Since the GHG reduction is the most difficult to achieve for all sectors in the transport sector (see various statements by the EU and the German Federal Government), a solution to this problem is best rewarded here. It is therefore advantageous to use the relieved fuel (35) in traffic (36), preferably in traffic and particularly preferably in air traffic. Alternatively, the GHG-relieved fuel (35) may be used as fuel or exhaled (37).

The inventive method includes the control and regulation of the respective sub-processes and the overall process. These are implemented in the usual way as system or system control and are therefore not explained in detail.

FIG. 2 shows an embodiment variant of the method according to the invention in which intermediate storage of the recuperated regenerative C0 ₂ s is dispensed with. Instead, it is transported to the place of use without intermediate storage.

FIG. 3 shows a variant of the method generally described in FIG. 1, in which the unused method steps are no longer shown. From the possible feedstocks (1 - 9), biomass (11) and manure (13) were selected in process step 1 (10). The conversion process used in process step 2 is anaerobic digestion (16). This produces the mixed gas biogas (20). The regenerative C0 ₂ contained in the biogas (20) in the process step 3 (22) by one of the suitable gas scrubbing (eg Rectisol-, pressurized water, non-pressurized amine scrubbing, Kryo-V experienced) of the accompanying gases (18) of C0 ₂ s (below the energy carrier methane) and as completely as possible recuperated in process step 4 (25). The recuperated C0 ₂ (26) is liquefied (27) in process step 5, stored temporarily in cryogenic tanks (not shown) (29) and thereafter transported by truck (not shown) to the place of use (not shown) (30). The regenerative C0 ₂ (not shown) transported to the place of use is used there to substitute material for fossil C0 ₂ (not shown) (32). The resulting GHG credits (not shown) are used in the replacement of the Meta-System "Environment" (34) to relieve the GHG balance of fossil natural gas (35) and fossil diesel fuel (35), which are GHG-relieved fuels be used in road traffic (36).

FIG. 4 shows a variant of the method generally described in FIG. 1, in which the unused method steps are no longer shown. From the possible starting materials (1-9), the biomass (11) was selected in process step 1 (10). The conversion process used in process step 2 is thermochemical gasification (15). In this case, the mixed gas pyrolysis gas (19). The regenerative C0 ₂ contained in the pyrolysis gas (19) is separated from the associated gases (18) of the C0 ₂ s in process step 3 (22) using one of the suitable gas scrubbing processes (eg Rectisol process, pressurized water scrubbing, pressureless amine scrubbing, cryogenic processes) and Step 4 (25) recirculates as completely as possible. The recuperated gaseous C0 ₂ (26) is transported to the point of use (not shown) by means of a pipeline (not shown) without intermediate storage (30). The regenerative C0 ₂ (not shown) transported to the place of use is used there as feedstock for the production of synthetic fuels (33). The resulting GHG credits (not shown) are used in the balancing of the MetaSystem "environment" (34) to relieve the GHG balance of a fossil fuels (eg natural gas, reference numeral 35), which this GHG-relieved fuel in appropriate heating systems (not 5 shows a variant of the method generally described in FIG. 1. Biomass (11) and waste (12) were selected from the possible starting materials (1 - 9) in method step 1 (10) The conversion process used is combustion (17) in method step 2. The mixed gas flue gas (21) is produced in this case. The regenerative CO ₂ contained in flue gas (21) is treated in process step 3 (22) with one of the suitable gas scrubbing methods (eg Oxy-fuel process, rectisol process, pressurized water wash, pressureless amine wash, cryo process) of the accompanying gases (18) of C0 ₂ s separated and as completely as possible recuperated in step 4 (25). Part of the recuperated CO ₂ s (26) is liquefied (27) in process step 5, stored temporarily in cryogenic tanks (29) and then transported by truck (not shown) to the place of use (geological repository, not shown). transported (30). The other part is stored in a gaseous state in pressurized gas tanks or caverns (not shown) and then transported to the place of use (plant for the production of synthetic fuels, not shown). The regenerative C0 ₂ (not shown) transported to the geological repository is sequestered there (31). The C0 ₂ transported to the synthesis plant is used there as feedstock for the synthesis of fuels (33).

The resulting GHG credits (not shown) will be used in offsetting the Meta Environmental System (34) to relieve the GHG balance of a range of fuels (35), including fossil, biogenic and synthetic fuels Fuels (35) are used both in (road) traffic (36) and for power generation and heating purposes (37).

FIG. 6 shows a general system configuration which converts the feedstocks (1 1, 12, 13, 14) selected according to the method into mixed gases (19, 20, 21), namely pyrolysis gas (19) with one of the conventional gasification plants (51) generates biogas (20) with one of the usual biogas plants (52) and flue gas (21) with one of the conventional combustion plants (53).

The pyrolysis gas (19) is fed to a conventional separation plant (54). The regenerative C0 ₂ (24) contained in the pyrolysis gas (19) is separated from the pyrolysis gas by means of the customary separation plant (54). However, the regenerative C0 ₂ (24) is not discharged into the atmosphere as usual, but is collected as completely as possible according to the invention by means of a recuperation device (57). The associated gases (18) are used in other plants for the production of synthetic fuels or for energy recovery. The recuperated, originating from pyrolysis regenerative C0 ₂ (60) is either stored in a gaseous state in pressure tanks or pressure tanks (64) or a liquefaction plant (63) supplied to the recuperated regenerative C0 ₂ (60) by cooling in the liquid state brings (65) or into a solidification plant (64), which converts the recuperated regenerative C0 ₂ (60) by further cooling in the solid state and thus converts it into so-called dry ice (66).

The biogas (20) is fed to one of the usual gas scrubbers (55), eg a Rectisol system or a system for pressurized water scrubbing, or a plant which operates on the principle of pressureless amine scrubbing or a plant which operates according to a ryo process. The regenerative C0 ₂ contained in the biogas (20) is extracted from the biogas (20) by means of these gas scrubbers (55). However, the separated regenerative C0 ₂ (24) is not released into the atmosphere as usual, but collected by means of a recuperation device (58). The associated gases (18), including the high-energy bio methane, are used for energy purposes or fed into the natural gas grid after further treatment. The recuperated, biogas-derived regenerative C0 ₂ (61) is either temporarily stored in a gaseous state in pressure tanks or pressure tanks (67) or a liquefaction plant (63), which brings the recuperated regenerative C0 ₂ (61) by cooling in the liquid state (65) or in a solidification plant (64), which converts the recuperated regenerative C0 ₂ (61) by even lower cooling than in the liquefaction in the solid state and thus converts it into so-called dry ice (66).

The flue gas (21) is fed to one of the abovementioned customary gas purification systems (56), which extracts the regenerative CO ₂ (24) from the flue gas (21) by one of the customary methods. Also possible is the upstream connection of an air separation plant (not shown), whereby almost exclusively the recovered oxygen is used in the furnace and thus no nitrogen in the air. This creates a flue gas with high and very high C0 ₂ concentrations (24). However, the separated from the flue gas regenerative C0 ₂ (24) is not discharged as usual in the atmosphere, but collected by means of a Rekuperationsvorrichtung (58). The accompanying gases (18) of the regenerative C0 ₂ s (24) are released into the atmosphere after any cleaning that may have to be carried out. The recuperated, flue-gas regenerative C0 ₂ (61) is either temporarily stored in a gaseous state in pressure tanks (67) or fed to a liquefaction plant (63) which cools the recuperated regenerative C0 ₂ (61) to a liquid state brings (65) or into a solidification plant (64), which converts the recuperated regenerative C0 ₂ (61) by even lower cooling than in the liquefaction in the solid state and thus converts it into so-called dry ice (66).

When the recuperated regenerative CO ₂ (60, 61, 62) is left in gaseous form, it is stored in at least one pressure tank (67) until it is transported to the point of use. Liquefied regenerative C0 ₂ (65) is temporarily stored in at least one cryogenic tank (68) and solidified C0 ₂ (dry ice; 66) in at least one insulated and optionally refrigerated room or container (69) until it is removed.

The recuperated regenerative C0 ₂ is transported to the place of use by means of suitable means of transport (eg truck, ship, railroad, pipeline). When in the gaseous state (70), there are pressure tanks available

(73), in liquid state (71) isolated and possibly cooled liquid gas tanks

(74) and in solid state (72) insulated and possibly cooled containers / containers

(75). The regenerative C0 ₂ (76, 77, 78) spent at the point of use is fed either to a geological repository (79) where it is sequestered or to an (possibly industrial) site (80) where it substitutes for fossil C0 ₂ (not shown) is used (eg a plant of the food industry), or a plant for the production of at least one synthetic fuel (81). In the production of synthetic fuels, the synthesis device (81) is fuel-specifically designed so that the supplied regenerative C0 ₂ optimally reacts with the supplied hydrogen. The production of synthetic methane takes place, for example, according to the Saabier reaction 4 H ₂ + C0 ₂ >CH ₄ + 2 H ₂ O, where Δ H _R = -165 kJ / mol. This reaction is connected via the retro-shift reaction H ₂ + C0 ₂ »> CO + H ₂ 0 (ΔH _R = + 42 kJ / mol) to the reaction 3 H ₂ + CO»> CR »+ H ₂ 0 where ΔH _R = -206 kJ / mol. The synthesis of fuels from C0 ₂ and H ₂ existing input materials requires a fuel-specific design of the synthesis device and corresponding control and regulating devices. With the incorporation into the geological repository (79), the regenerative C0 ₂ (76, 77, 78) disappears permanently from the atmosphere and with the substitution of fossil C0 ₂ s (not shown) by regenerative C0 ₂ (not shown) is the use fossil C0 ₂ s pushed back or avoided. The use of the regenerative C0 ₂ s as a feedstock for the production of largely GHG-reduced synthetic fuel, the use of fossil fuels (gasoline, CNG, diesel, LPG, kerosene, heavy oil) is pushed back, which also reduces fossil C0 ₂ emissions in the Atmosphere results.

The positive GHG effects (82, 83, 84) associated with the respective use of regenerative C0 ₂ s for the meta-system "environment" become statistically virtual with the

GHG emissions (85, 86, 87) of the selected at least one fossil or biogenic or synthetic fuel (88, 89, 90) are billed or balanced. Positive GHG effects thus compensate for negative GHG effects and overall GHG neutrality is created. The fuel quantity (88, 89, 90) whose GHG emission can be reduced or neutralized or overcompensated is calculated according to the formula given in claim 20.

The GHG-relieved fuel quantity (88, 89, 90) can be used in traffic vehicles (91), e.g. in road vehicles, rail vehicles, aircraft and ships, or in heating installations (92) or in electricity generation plants (93). The system configuration according to the invention includes the control and regulation of the respective systems and the overall configuration. These are implemented in the usual way as system or system control and are therefore not explained in detail.

FIG. 7 shows a variant embodiment of the system configuration according to the invention, in which intermediate storage of the recuperated regenerative C0 ₂ s is dispensed with. Instead, it is transported to the place of use without the use of storage technology. FIG. 8 shows an embodiment variant of the system configuration of FIG. 06 which converts the feedstocks biomass (11) and farmyard manure (13) selected in accordance with the method according to the invention into the mixed gas biogas (20) with a conventional biogas plant (52). The unused system components are no longer displayed. The regenerative C0 ₂ contained in the biogas (20) with one of the appropriate gas scrubbing plants (eg Rectisol plant, pressurized water wash plant, with the pressureless amine scrubbing plant, ryo plant) of the associated gases (18) of C0 ₂ s (including the Energy source methane) separated. The associated gases (18), including the high-energy bio methane, are used for energy purposes or, after further processing, fed into the natural gas grid.

The extracted regenerative C0 ₂ (24) is recuperated as completely as possible by means of a recuperation device (58). The recuperated regenerative CO ₂ (61) is fed to a liquefaction plant (63) which brings the recuperated regenerative CO ₂ (61) into the liquid state by cooling (65). The liquefied regenerative CO ₂ (65) is stored in cryogenic tanks (68) and then transported by truck (74) to the point of use (not shown).

The regenerative C0 ₂ (77) transported to the place of use is fed to one or more industrial plants (80) which use it in place of fossil C0 _2s (not shown), eg for the production of carbonated drinks. With the substitution of fossil C0 ₂ s by regenerative C0 ₂ (77), the use of fossil C0 ₂ s is suppressed or avoided. The resulting GHG credits (83), when offsetting the meta-system "Environment", are compared to the GHG pollution (86) of fossil natural gas (35) and fossil diesel fuel (35) .These two fuels are used in road traffic 6 shows an embodiment variant of the plant configuration of FIG. 06, which converts the biomass input material (11) into the mixed gas flue gas (21) by means of a conventional furnace 53. The unused plant components of FIG. The regenerative C0 ₂ contained in the flue gas (21) is mixed with one of the suitable gas scrubbers (eg a Rectisol plant, a pressurized water scrubber). Plant, a plant operating with the pressureless amine scrubber, a cryogenic plant; Reference numeral 56) from the accompanying gases (18) of C0 ₂ s (including 0 ₂ , CO, NO _x , N) separated. The accompanying gases (18) are discharged as worthless waste product into the atmosphere. The extracted regenerative C0 ₂ (24) is recuperated as completely as possible by means of a Rekuperationsvomchtung (59). The recuperated regenerative CO ₂ (62) is stored in gaseous form in pressure tanks (67) and then transported by suitable means of transport (73) to the place of use (not shown).

The regenerative C0 ₂ fractions (76, 78) transported in gaseous and solid state to the place of use are fed in part to at least one geological disposal site (79) and to the other part of one or more fuel synthesis facilities (81) use fossil C0 ₂ s (not shown). With the removal of regenerative C0 ₂ s from the atmosphere and with the substitution of fossil C0 ₂ s (not shown) by regenerative C0 ₂ (76, 78), the use of fossil C0 ₂ s is suppressed or avoided. The resulting GHG credits (82, 84) will be offset against the GHG pollution (85, 87) of fossil fuels (88) and biogenic fuels (89) when balancing the meta-system "Environment." The at least two fuels will be FIG. 10 shows an alternative embodiment of the system configuration of FIG. 06, which uses the biomass feedstock (11) selected according to the inventive method by means of a gasification / pyrolysis system (51) in FIG The unused system components of Figure 06 are not shown The regenerative C0 ₂ contained in the pyrolysis gas (19) with one of the appropriate gas scrubbing systems (eg a Rectisol system, a Druckwasserwäsche-, one with the pressureless amine-washing plant, a cryogenic plant; 54) from the accompanying gases (18) of the C0 ₂ s (below 0 ₂ , CO, NO _x , N, H ₂ , But on, propane) separated. The associated gases (18) are used in the main process of the gasification plant as a high-energy synthesis gas and converted into synthetic fuels. The extracted regenerative C0 ₂ (24) is recuperated as completely as possible by means of a recuperation device (57). The recuperated regenerative C0 ₂ (60) is temporarily stored in gaseous form in at least one pressure tank (67) and liquefied to the other part in a liquefaction plant (63) and intermediately stored in at least one liquefied gas tank. Thereafter, the gaseous C0 ₂ (70) and the liquid C0 ₂ (71) are transported by suitable transport means (73, 74) to the place of use (not shown).

The regenerative C0 ₂ (76) transported in the gaseous state to the point of use is fed to one or more fuel synthesis plants (81) which use it in place of fossil C0 _2s to produce synthetic fuel (not shown). The regenerative C0 ₂ (77) transported in the liquid state of aggregation to the place of use is fed to at least one final geological deposit (79).

With the removal of regenerative C0 ₂ s from the atmosphere and with the substitution of fossil C0 ₂ s (not shown) by regenerative C0 ₂ (76, 77), the use of fos- sil C0 ₂ s is suppressed or avoided. The resulting GHG credits (82, 84) are offset against the GHG pollution (85, 87) of fossil fuels (88) and synthetic fuels (90) when balancing the meta-system "Environment." The at least two fuels are used both in Used in traffic vehicles (91) as well as in power plants (93).

List of Reference Propane

butane

petroleum fractions

natural gas

coal

Biomass (GHG reduced)

Hydrocarbon waste (GHG-reduced)

Organic waste as a special form of biomass (GHG-reduced)

Organic fertilizer as a special form of biomass (GHG-reduced)

Process step 1: Selection of the starting materials

Biomass (GHG reduced)

Waste (GHG reduced)

Organic fertilizer as a special form of biomass (GHG-reduced)

Organic waste as a special form of biomass (GHG-reduced)

Process Step 2a: Conversion by Gasification (Pyrolysis)

Process 2b: conversion by anaerobic digestion

Process step 2c: Conversion by combustion (oxidation)

Carrier gases

Mixed gas Pyrolysis gas, consisting of at least GHG-reduced C0 ₂ and synthesis gas

Mixed gas Biogas, consisting of at least GHG-reduced C0 ₂ , CH4 and associated gases

Mixed gas flue gas, consisting of at least GHG-reduced C0 ₂ , CH ₄ and associated gases

Process step 3: Separation of regenerative C0 ₂ s from mixed gases

Separated, but not recuperated, regenerative or GHG-reduced C0 ₂ The recuperation zxigeführtes, regenerative or GHG-reduced C0 ₂ Process step 4: recuperation regenerative or GHG-reduced C0 ₂ s Recuperated regenerative or GHG-reduced C0 ₂

Process step 5a: liquefaction of the recuperated C0 ₂ s

Process step 5b: solidification of the recuperated regenerative C0 ₂ s Process step 6: intermediate storage of the recuperated regenerative C0 ₂ s Process step 7: Transport of the recuperated regenerative C0 ₂ s

Process step 8a: Sequestration of the recuperated C0 ₂ s

Process step 8b: Material substitution of fossil C0 ₂ s by the recuperated regenerative C0 ₂

Process step 8c: Use of the regenerative C0 ₂ s for the production of synthetic fuels

Process Step 9: Balancing the Meta-System "Environment"

Fuel relieved by virtual statistical offsetting of GHG emissions

Process step 10a: Use of the relieved fuel in traffic Process step 10b: Use of the relieved fuel as fuel or for power generation gasification pyrolysis plant

Of fermentation ZBiogasanlage

furnace

Plant for the separation of C0 ₂ from pyrolysis gas

Plant for the separation of C0 ₂ from biogas

Plant for the separation of C0 ₂ from flue gas

Device for recuperation of C0 ₂ from pyrolysis gas

Device for recuperation of C0 ₂ from biogas

Device for recuperation of C0 ₂ from flue gas

Pyrolysis gas recuperated regenerative C0 ₂

Biogas recuperated regenerative C0 ₂

Recuperative C0 ₂ recuperated from flue gas

Plant for the liquefaction of gases

Plant for the production of solid C0 ₂ (dry ice)

Liquefied regenerative C0 ₂ Solid regenerative C0 ₂ (dry ice)

At least 1 pressurized gas tank

At least 1 LPG tank

At least 1 isolated cold room

Expelled regenerative C0 ₂ in gaseous state

Exploded regenerative C0 ₂ in liquid state

Exploded regenerative C0 ₂ in solid state

Suitable means of transport for the transport of gases (truck, ship, rail, pipeline)

Suitable means of transport for liquefied gas transport (truck, ship, rail, pipeline)

Suitable means of transport for the transport of dry ice (truck, ship, rail)

At the place of use spent regenerative C0 ₂ in gaseous state

At the place of use spent regenerative C0 ₂ in liquid state

Regenerative C0 ₂ spent at the place of use in a fixed state of aggregation Geological repository

C0 ₂ using (industrial) plant

Plant for the production of synthetic fuels or components Quantified GG effect of sequestration of regenerative C0 ₂

Quantified THG effect of the material substitution of fossil C0 ₂ s by regenerative co ₂

Quantified GHG effect of recycling regenerative C0 ₂ s in the production of synthetic fuels and heating fuels

GHG effect transferred to fuels to be relieved of GHG loads (GHG credit or GHG certificate)

GHG effect transferred to fuels to be relieved of GHG loads (GHG credit or GHG certificate)

GHG effect transferred to fuels to be relieved of GHG loads (GHG credit or GHG certificate) 88 At least 1 fossil fuel

 89 At least 1 biogenic fuel

 90 At least 1 synthetic fuel

 91 At least 1 vehicle of traffic (road, rail, water, air)

 92 At least 1 heating system

 93 At least 1 power plant (internal combustion engine with generator, fuel cell)

Claims

claims

1. A process for the production of renewable C0 ₂ s by means of the conversion process of combustion or gasification or anaerobic digestion in suitable plants, especially in combustion plants or gasification plants or in biogas plants, from non-fossil fuels, preferably from biomass, particularly preferably from greenhouse gas-free biomass and in particular from lignocellulosic biomass, characterized in that the at least one combustion plant with concentrated oxygen operates according to the oxyfuel process, in which the flue gas is not diluted with atmospheric nitrogen and C0 _{2 is obtained} in concentrated form, or the at least one combustion plant with a system for Separation of C0 _{2 is connected} from the flue gas or the at least one furnace is integrated into an IGCC combined cycle power plant, in which C0 _{2 is produced} by gasification and after the pre-combustion capture method before combustion is removed from the fuel gas, od the at least one combustion plant is integrated into a plant for the production of methanol, hydrogen or synthetic methane, in which C0 ₂ is obtained as a by-product, and the feedstocks of the at least one gasification plant are partially sub stoichiometrically converted with water to a (combustion) gas in partial oxidation be substantially consisting of hydrogen and CO, wherein the CO is converted by means of suitable catalysts under high pressure with steam to C0 ₂ and hydrogen, which is connected to at least one biogas plant with a plant for the separation of C0 ₂ from biogas or such a plant supplied with biogas, regenerative energy sources and / or organic residues and / or organic waste are used as fuel in the at least one firing plant, preferably culture wood and / or waste wood and / or waste wood and / or forest residue wood and / or bark and / or landscape care wood and / or fiber slurry and / or or black liquor and / or straw and / or paper and / or cardboard and / or organic waste and / or residual organic waste, in which at least one gasification plant regenerative energy sources and / or organic residues and / or organic waste are used as feedstock, preferably cultivated wood and / or or waste wood and / or waste wood and / or forest residue wood and / or bark and / or landscape care wood and / or fiber sludge and / or black liquor and / or straw and / or paper and / or cardboard and / or organic waste and / or residual waste, in the at least one Biogas plant renewable energy sources and / or organic residues and / or organic waste as fermentation substrates ei preferably corn and / or cereal grains and / or cereal crop cut and / or grass and / or manure (manure, solid manure, manure, dry manure) and / or potatoes and / or beets and / or vinasse from bioethanol production and / or straw and / or organic waste and / or organic waste, which is deposited in the at least one plant resulting regenerative C0 ₂ to at least 5%, preferably at least 20%, more preferably at least 50% and in particular at least 85% from the exhaust gas consisting of mixed gases in which at least 5%, preferably at least 20%, particularly preferably at least 50% and in particular at least 85% of the precipitated regenerative C0 _{2 are passed} into a "C0 ₂ -recuperation" process step and are collected there (recuperated), the recuperated regenerative C0 ₂ in gaseous state in at least one non-pressurized container or in at least one pressure vessel or in liquid For m in min. at least one liquefied gas tank or in solid form in at least one thermally insulated container or room is temporarily stored or the recuperated regenerative C0 _{2 is} fed with or without caching in a gas or liquid gas line or for generating liquid or solid regenerative C0 ₂ in a cooling system, of which recuperated regenerative C0 ₂ in the following use at least 5%, preferably at least 20%, more preferably at least 60% and in particular at least 95% sequestered (geologically stored) or according to the Sabatier process preferably with the addition of electricity from sources free of greenhouse gases or hydrogen atomized by atomic flow into synthetic methane or reformed to methanol or ethanol or to synthetic methane, octane, butane or propane according to one of the known and conventional methods, or to substitute fossil C0 ₂ , the result forming savings on greenhouse gas emissions and / or the resulting impairment of atmospheric C0 ₂ inventory over are counted towards the greenhouse gas emissions of at least one fuel, preferably to the greenhouse gas emissions of fossil fuels, gasoline, diesel fuel, kerosene, natural gas, LPG and heavy fuel oil, more preferably on greenhouse gas emissions bio-fuels BioDiesel, bioethanol, hydrogenated oils, bio-methane (biogas), ETBE and TAEE not produced in the plant, and in particular greenhouse gas emissions of so-called future fuels Fischer-Tropsch-Diesel from lignocellulose (wood and / or straw), ethanol from lignocellulose, DME from biomass, methanol from biomass and MTBE from biomass, the LCA greenhouse gas load on the at least one fuel is at least 5%, preferably at least 50%, more preferably at least 85% and in particular at least 100% relieved.

2. The method of claim 1, wherein the deposition of the regenerative C0 ₂ s is a secondary process and the main purpose of C0 ₂ deposition is the concentration of at least one of the gases that accompany the C0 ₂ .

3. The method of claim 1, wherein the at least one fuel is used in traffic, preferably in traffic.

4. The method of claim 1, wherein the at least one fuel is used as fuel or used for power generation.

5. The method of claim 1, wherein the current used in the process from greenhouse gas reduced, preferably derived from greenhouse gases sources and / or in which the thermal energy used in the process from greenhouse gas reduced, preferably from greenhouse gases sources.

6. The method of claim 1, wherein both for the deposition and for the liquefaction of the regenerative C0 ₂ s a cryogenic process is used or the deposition is carried out by a condensation of water or the regenerative C0 ₂ physically from a high pressure C0 ₂ - / hydrogen mixed gas is absorbed or chemically washed out under supply of thermal energy.

7. The method of claim 1, wherein the transport of the recuperated regenerative C0 ₂ s to the place of use is at least partially by truck and / or by ship and / or rail and / or pipeline and thereby preferably greenhouse gas reduced fuels are used, particularly preferably Domestic gas-free fuels.

The method of claim 1, wherein at least 35%, preferably at least 50%, more preferably at least 60%, and most preferably at least 70% of the resulting greenhouse gas emission savings and / or the resulting C0 ₂ emissions reductions do not affect the greenhouse gas emissions of the greenhouse gas emissions be counted at least one fuel.

9. The method of claim 1, is recuperated with the C0 ₂ from a plant, which is used for the production of fuels.

10. The method of claim 1, wherein the maximum unloadable fuel amount is calculated according to the following algorithm:

MK _n = (RC0 ₂ / ECC-2-ei / EC0 _2-th / EC0 ₂ -so "st) / (C0 ₂ -kn. / CC / -ZB ^), where

MK _n ⁼ maximum energy quantity of the fuel n, measured in kWTi _H i or MJ, which can be brought to the target load C0 ₂ -ZBj n;

RC0 ₂ = recuperative amount of regenerative C0 ₂ , measured in t C0 ₂ -eq,

EC0 _2- ei = C0 ₂ -emissions, measured in t C0 ₂ -eq, which arise after the recuperation of the regenerative C0 ₂ s by the use of electrical energy;

EC0 _2- th ⁼ C0 ₂ -emissions, measured in t C0 ₂ -eq, which arise after the recuperation of the regenerative C0 ₂ s by the use of thermal energy;

EC0 ₂ - otherwise - other C0 ₂ emissions, measured in t C0 ₂ -eq, which arise after recuperation of the regenerative C0 ₂ s;

C0 _2- Kn ⁼ LCA-THG load of the fuel to be relieved n, measured in gC0 ₂ -eq / kWh _H i or in gC0 ₂ -eq / MJ;

C0 ₂ -ZB _I , ⁼ GHG target load of the fuel to be relieved n, measured in gC0 ₂ -eq / kWh _H i or in gC0 ₂ -eq / MJ.

11. Plant for generating regenerative C0 ₂ s from non-fossil fuels, preferably from biomass, particularly preferably from greenhouse gas-free biomass and in particular from lignocellulosic biomass in which the conversion process of the combustion or the conversion process of the gasification or the conversion process of anaerobic digestion is used , characterized in that the plant operates as a furnace with concentrated oxygen according to the oxyfuel process, in which the flue gas is not diluted with atmospheric nitrogen and C0 _{2 is obtained} in concentrated form, or as a firing plant with a plant for separation C0 _{2 is connected} from the flue gas or is integrated as a combustion plant in an IGCC ombikraftwerk in which C0 _{2 is produced} by a gasification and is removed from the fuel gas prior to combustion by the pre-combustion capture method, or as a furnace is integrated into a plant for the production of methanol, hydrogen or synthetic methane, in which the by-product C0 ₂ is obtained, the plant as a gasification plant substoichiometrically converted the feedstocks in partial oxidation with water to a (fuel) gas, which essentially consists of Hydrogen and CO, wherein the CO is converted by means of suitable catalysts under high pressure with steam to C0 ₂ and hydrogen, the plant is connected as a biogas plant with a plant for the separation of C0 ₂ from biogas or such plant is supplied with biogas, in the plant as a combustion plant regenerative energy sources and / or organic residues and / or organic waste ll be used as a fuel, preferably culture wood and / or waste wood and / or waste wood and / or forest residue wood and / or bark and / or landscape wood and / or fiber sludge and / or black liquor and / or straw and / or paper and / or cardboard and / or organic waste and / or residual waste, in the at least one gasification plant regenerative energy sources and / or organic residues and / or organic waste are used as feedstock, preferably cultural wood and / or waste wood and / or waste wood and / or forest residue wood and / or bark and / or Landscape wood and / or fiber sludge and / or black liquor and / or straw and / or paper and / or cardboard and / or organic waste and / or residual waste, used in the at least one biogas plant regenerative energy sources and / or organic residues and / or organic waste as fermentation substrates preferably corn and / or cereal grains and / or cereal crop cut and / or grass and / or farm dung (manure, solid manure, dung, dry manure) and / or potatoes and / or beet and / or vinasse from bioethanol production and / or straw and / or organic waste and / or industrial waste, the regenerative C0 ₂ produced in the plant at least 5%, preferably at least 20%, particularly preferably at least 50% and in particular at least 85% is separated from the exhaust gas consisting of mixed gases, from the deposited regenerative C0 ₂ at least 5%, preferably at least 20%, particularly preferably at least 50% and in particular at least 85% in a plant part "C0 ₂ -Rekuperation" out and there are collected (recuperated), the recuperated regenerative C0 ₂ in the gaseous state in at least one unpressurized container or in at least one pressure vessel or in liquid form in at least one liquefied gas tank or in solid form in at least one thermally insulated container or room is temporarily stored or recuperated Regenerative C0 ₂ with or without caching in one Gas or liquid gas line or for the production of liquid or solid regenerative C0 _{2 is} fed into a cooling system, the at least one pressureless container and / or the at least one pressure vessel and / or the at least one liquefied gas tank by means of a line with the plant part "C0 ₂ -Rekuperation at least 5%, preferably at least 20%, particularly preferably at least 60% and in particular at least 95% of the recuperated regenerative C0 _{2 are} sequestered (geologically stored) or, according to the sabatizing process, preferably with the addition of electricity be converted from greenhouse gas-free sources or atomic stream electrolytically generated hydrogen into synthetic methane or reformed according to one of the known and customary methods to methanol or ethanol or synthetic methane, octane, propane or butane or substitute fossil C0 ₂ material, the resulting savings in greenhouse gas emissions and / or the resulting reductions in atmospheric C0 ₂ emissions being credited to the greenhouse gas emissions of at least one fuel, preferably the greenhouse gas emissions of the fossil fuels gasoline, diesel fuel, kerosene, natural gas, liquefied petroleum gas and heavy fuel oil Greenhouse gas emissions of biofuels BioDiesel, BioEthanol, Hydrogenated oils, BioMethane (biogas), ETBE and TAEE not produced by the plant, and in particular greenhouse gas emissions from so-called future fuels Fischer-Tropsch diesel from lignocellulose (wood and / or straw) , Ethanol from lignocellulose, DME from biomass, methanol from biomass and MTBE from biomass, the LCA greenhouse gas load on the at least one fuel by at least 5%, preferably at least 50%, more preferably at least 85% and in particular at least 100% relieved ,

12. Plant according to claim 11, wherein the deposition of the regenerative C0 ₂ s represents a secondary process and the main purpose of the C0 ₂ - deposition in the concentration of at least one of the gases that accompany the C0 ₂ .

13. Plant according to claim 11, wherein the at least one fuel is used in traffic, preferably in traffic.

14. Plant according to claim 11, wherein the at least one fuel is used as fuel or used for power generation.

15. Plant according to claim 11, in which the electricity used in the plant is derived from greenhouse gas-reduced sources, preferably from sources free of greenhouse gases, and / or from which the thermal energy used in the plant originates from reduced greenhouse gas emissions, preferably from greenhouse gas-free sources.

16. Plant according to claim 11, wherein at least one cooling system is used both for the deposition and for the liquefaction of the regenerative C0 ₂ s or in which the deposition takes place by condensation of water or in which the regenerative C0 ₂ physically from a high Pressurized C0 ₂ - hydrogen mixed gas absorbed or chemically washed out under pressure with the supply of thermal energy.

17. Plant according to claim 11, wherein the transport of the recuperated regenerative C0 ₂ s to the place of use is at least partially by truck and / or by ship and / or by rail and / or pipeline and thereby preferably greenhouse gas reduced fuels are used, especially preferably propellant-free gas fuels.

The plant of claim 11, wherein at least 35%, preferably at least 50%, more preferably at least 60%, and most preferably at least 70% of the resulting greenhouse gas emission savings and / or the resulting C0 ₂ atmospheric emissions reductions do not affect the greenhouse gas emissions of the greenhouse gas emissions at least one fuel counted.

19. Plant according to claim 11, in which C0 _{2 is} recuperated from a plant which serves for the production of fuels.

20. An installation according to claim 11, wherein the maximum loadable amount of fuel is calculated according to the following algorithm:

MK "= (RCO2 ./. EC0 _2-e i V. EC0 _2-th ./ EC0 ₂ -sons t) / (C0 _2-K " ./. C0 ₂ where

MK "maximum energy quantity of the fuel n, measured in kWli _H i or MJ, which can be brought to the target load C0 ₂ -ZB | Cn;

RC0 ₂ Recuperative amount of regenerative C0 ₂ , measured in t C0 ₂ -eq, EC0 _2-e , C0 ₂ -emissions, measured in t C0 ₂ -eq, resulting from the use of electrical energy after recuperation of the regenerative C0 ₂ s ; EC0 _2-th = C0 ₂ -emissions, measured in t C0 ₂ -eq, which arise after the recuperation of the regenerative C0 ₂ s by the use of thermal energy;

EC0 ₂ - other C0 ₂ emissions, measured in t C0 ₂ -eq, arising after recuperation of regenerative C0 ₂ s;

C0 _2-K "= LCA-THG load of the fuel to be relieved n, measured in gC0 ₂ -eq / kWh _H> or in gC0 ₂ -eq / MJ;

C0 ₂ -ZBKn = GHG target load of the fuel to be relieved n, measured in gC0 ₂ -eq / kWh _Hi or in gC0 ₂ -eq / MJ.