DE19947340A1 - Transport of carbon dioxide - Google Patents

Abstract

An agricultural methane generator reactor vessel has an externally-fitted inlet shaft with sub-surface release of inputs, and a higher-located outlet for spent residues. A biological reactor T4a, T4b generates methane and carbon dioxide by the combined digestion of animal slurry and waste vegetable matter. Animal slurry and vegetable matter is introduced through an vertical side-shaft T3 having a lower inlet F13. Spent wastes are discharged through the shaft upper outlet F12. The vertical side-shaft is mounted especially externally on or near to the reactor outer wall. Both the lower inlet and upper outlet are linked with the reactor chamber.

Description

The invention relates to a method and a plant for the transport of carbon dioxide (CO ₂ ).

Carbon dioxide is used in many chemical processes, such as anaerobic fermentation processes for example in distilleries, in wine production, in breweries and in Combustion processes for energy production produced, but unused in the Release atmosphere.

The invention seeks to remedy this. An object of the invention is carbon dioxide, which is particularly common in industrial processes, is easier to use for recycling do.

This object is achieved in that the carbon dioxide or an accumulating Gaseous or liquid, carbon dioxide-containing product in a fixed installation Pipeline network is transported. This enables a consumer to Carbon dioxide or the carbon dioxide product if required at any time from the Pipeline network can take. The consumer must have their own storage capacity for do not have the carbon dioxide he needs because the carbon dioxide is continuous and is constantly available via the pipeline network. However, it can remove the carbon dioxide from the Cache the pipeline with you, if that is advantageous for him. If in the following only carbon dioxide is mentioned, any gaseous or liquid As long as such a product has a carbon dioxide content of at least Has 40 vol%. Within the scope of the invention, a pipeline network is also a single one  Pipeline from a device for producing the product to a consumer of the Understand carbon dioxide. However, training as branched is particularly preferred Pipeline network to which several devices for generation and / or several Consumers are connected directly or via intermediate storage.

The transport is particularly preferably carried out directly from a device to the Generation of the carbon dioxide or the carbon dioxide-containing product up to immediately the consumer. However, it would also be conceivable to create several devices to connect to each other via a pipeline network and that of these devices Carbon dioxide generated initially stored centrally, then from a central Transport the intermediate storage from further. It would also be conceivable to have several Consumers via the pipeline network to a central buffer for connect the carbon dioxide. Such pipeline networks are also pipeline networks in Purpose of the invention, although the wired transport individually by the Device for generation to the individual consumer is particularly preferred.

Carbon dioxide is generated or collected as a by-product or waste product, enriched, cleaned and transported through pipelines. One or more supply networks connect and network CO ₂ producers and CO ₂ consumers / users. They are used for the area-wide, controlled generation, disposal, recording, supply and release of CO ₂ .

The new utilization possibilities of the pipeline-transported CO ₂ , which are opened up by the invention, also at distant utilization locations lead to an improved economy of the respective production facility and utilization facility, to a better total energy utilization and to better environmental and climate protection.

Until now, it was only possible to collect carbon dioxide at the point of production / production, to fill it under pressure in bottles or tanks and then to transport it in batches to distant recycling sites. It is now possible to pool small, decentralized quantities of processed carbon dioxide by removing one or more bulk buyers and consumers, so that the economy-of-scale effect can be exploited for economic implementation. Smaller plants with CO ₂ -containing gases and / or exhaust gases can also be connected through a decentralized pipeline network to a common processing plant, in which the CO _{2 is} preferably dehumidified and freed of trace substances and solids, so that it fulfills the requirements regarding feed composition and purity before it is fed into the nationwide supply network.

CO ₂ -containing gases and exhaust gases are produced decentrally at any location, but can now be removed and used at a location distant from the introduction by being transported ready for transport from the decentralized production location to a remote utilization location in permanently installed pipelines .

CO ₂ producers are, for example, mineral wells / sources, carbon dioxide plants, lime kilns, plants for gas separation, plants for air liquefaction, plants for exhaust gas purification, fertilizer factories with preferably a steam reformer process, anaerobic microbial fermentative processes, such as those used by a brewery, distillery, in wine production, be carried out in biogas plants, landfills and in pharmaceutical fermentations, furthermore incineration plants, fuel cells and / or power plants. The concentration of CO ₂ in starting gases at the production site is preferably between 5 and 99% by volume. Such a starting gas is processed by means of a device for generating the carbon dioxide to be fed in, so that a product with at least 40 vol% carbon dioxide content results therefrom.

CO ₂ consumers / recyclers are preferably residential areas with household connections, industrial settlements, middlemen, chemical companies, agricultural companies with animal and / or plant production, food and beverage industry, chemical industry, steel industry, storage and storage with preferably controlled atmosphere, transport, Greenhouses, horticultural and landscaping companies with glass growing, aqua and / or aqua algae cultures, restaurants, medical industry, cleaning industry, film, television and video industry, theater industry, show business and / or civil engineering. CO ₂ can also be piped into the deep sea and deposited there. Durable assets made from CO ₂ in the chemical industry and through coal refinement can also be viewed as a CO ₂ sink.

CO ₂ is used, for example, as a chemical raw material and for coal refinement, in oil production, for preservation and asphyxiation, as a carbon and carbonate source as well as to support drying processes, in medicine, in the beverage industry and / or for cleaning. Liquid CO ₂ is preferably used as a fire protection agent , in cooling processes (dry ice) and / or for solvent flooding in the tertiary production of petroleum (enhanced oil recovery). If sufficient CO ₂ can be provided via the networked lines, large consumers such as the chemical industry and coal refining can be supplied. Inferior lignite warehouses, which are no longer suitable for energy production due to high sulfur contents, open up for coal refinement.

Connection to the supply network is particularly preferred, but it also has advantages if concentrated and purified CO ₂ -containing gases and exhaust gases, preferably from the treatment of landfill and / or biogases, are also fed directly to the users. The concentration takes place, for example, using the following methods and devices. At CO ₂ concentrations in the gas and / or waste gas of preferably 8 to 50% by volume, the carbon dioxide is preferably concentrated from biogases, waste gases from anaerobic fermentative processes and / or from processes with cold and / or hot combustion, for example fuel cells and / or Power plants, preferably physical and physical chemical processes applied. In systems with a capacity of preferably 10 to 100 m ³ / h, this is done using physico-chemical commercial processes of pressure washing in aqueous solution with an absorption liquid, preferably monoethylene amine (MEA), e.g. B. with the alternating pressure process, or in larger plants with a capacity of preferably 50 to 2,000 m ³ / h, preferably via physical processes. Selective membranes with continuous gas permeation are preferably used in the lower area and discontinuous PSA systems (pressure swing absorption systems) with molecular sieves or activated carbon are preferably used in the upper area. At CO ₂ concentrations in the gas and / or exhaust gas of preferably 50 to 99%, methods of liquefying CO ₂ are mainly used for concentration and purification in the liquid and / or gaseous phase.

Carbon dioxide is preferably used as a bulk consumer, cooling and refining Freezing processes, medical technology, preservation processes, Fire suppression processes, greenhouses for example in the form of Film tunnels, warehouses, silos, bales, bale-making machines, the chemical industry as chemical raw material, cleaning purposes, the film, television and video industry, the Beverage industry and / or algae production supplied.

When CO _{2 is} used for preservation, the carbon dioxide, preferably from treated biogases, for air displacement to create low-oxygen and suffocating conditions, preferably under an overpressure of 0 to 1 bar, alone, as trailing gas and / or in specially designed pressure vessels (e.g. Pex pressure chamber Carbonic acid BUSE, Carvex pressure chamber CARBO carbonic acid, Guttroff pressure chamber) as supercritical CO ₂ at an overpressure of 10-50 bar at relative humidities of 10 to 95% and / or temperatures of 5 to 50 ° C in concentrations of 5 to 95 vol% preferably initiated over 0.5 to 100 days to increase durability and reduce material losses, storage losses and post-harvest losses in partially or completely closed rooms, storage / silos with a preferably controlled atmosphere. The material thus hygienized, for example straw and / or hay, can be mixed with ammonia gas in order to improve the C / N ratio and / or the digestibility. It is preferably introduced in storage / silos for the ensiling of agricultural products in order to reduce or prevent the ensiling losses, which are usually around 10 to 15%. The residual oxygen content after CO ₂ introduction is 1 to 22 vol%.

When CO _{2 is} used to reduce the risk of fire, the carbon dioxide, preferably from treated biogases, is introduced into straw and hay storage, into storage and silos or into grinding and / or conveying devices with explosive dusts and gases housed or connected to them, so that dust explosions can be prevented. With a residual oxygen content of 8%, a dust explosion can even be ruled out. In preferably gas-tight / hermetic straw and hay storage facilities, storage facilities and / or silos, it is preferably introduced via lances, perforated hoses, provided air conditioning, ventilation and fumigation systems and / or perforated cover recessed / recessed channels in the floor. The pore volume can be filled in from below with simultaneous displacement of the existing gases or filled from above by the falling gas, preferably if the stored CO ₂ breathing is eliminated. If the CO ₂ atmosphere is lost, a very rapid increase in yeast and mold can be expected. Exhaust gas CO ₂ from the treatment of biogases is introduced into encapsulated grinding and crushing plants and / or transport devices such as screw conveyors and conveyor belts after hot air drying, in preferably pressed and / or preferably wrapped in foils from preferably organic substances such as clothing, textiles, tobacco , Hops, banana fibers, coconut fibers, raw jute fibers, raw sisal fibers, raw rubber, sawdust, hay, straw, crop residues, animal feed, paper, cardboard, waste and / or sorted waste fractions.

Machines such as, for example, collecting presses, round balers, winding presses, large square balers and / or piston presses, the bales of clothing, textiles, tobacco, hops, banana fibers, coconut fibers, raw jute fibers, raw sisal fibers, raw rubber, sawdust, hay, straw, paper crop residues, cardboard, animal feed , Waste and / or sorted out waste fractions and / or wrap bales in foils are equipped with refillable, replaceable CO ₂ pressure bottles, characterized in that the CO ₂ system, consisting of pressure bottle, evaporator, control and regulating valves, pressure reducing valves, Pipes and / or nozzles can be operated by the vehicle driver from the driver's cab or from an otherwise attached control panel and semi-and / or fully automatically injected with CO ₂ during the pressing and / or wrapping process, preferably into the center of the bale.

During the wrapping and pressing process and / or afterwards with Holed lines in the bale are positioned so that a line in the The center of the bale comes to rest, while others are embedded in the periphery become. The central line preferably contains a larger opening in the Center. All lines are accessible from both sides from the outside and with connections, For example, thread or quick connect coupling, so that they, for example  closed with valves, slides, flaps, corks and / or clamps and / or with Connection or extension lines can be provided. Several bales in a camp can be through connectors and / or other lines are interconnected so that gases and / or liquids are uniform and / or at the same time, preferably carbon dioxide, nitrogen, oxygen, ammonia, nutrient solutions, organic acids, mineral acids, bases and / or suspensions, for example from vegetable spores and / or seeds. Alternatively or in addition can between layers of preferably not wrapped bales in film Stacking in the mountain room single and / or double-sided perforated films, Lines, hoses and / or pipes are laid, through which the gases, Liquids and / or suspensions can be supplied. This procedure has the Advantage that the devices are easier to lay and remove, in contrast to the pressed into the ball. Such stacks are preferably covered with a film / tarpaulin covered and sealed at the bottom, in particular to prevent gas loss and gas consumption to reduce. With spores and / or seeds for the production of mushrooms and / or higher Bales enriched with plants become manageable parts weighing 0.5 to 10 kg portioned before they are put on the market. The lines / hoses can be in the portions are left to later add moisture and / or nutrient solutions and thus compensate for losses caused by fungus and / or plant growth were caused.

A further application of the method of using CO ₂ , preferably from treated biogases, is the impregnation of sparkling wines, the introduction alone or in a mixture with other gases into pressurized gas containers, preferably with a simultaneous effect as propellant, for the carbonation of lemonades and soft drinks and / or in steel bombs for beer presses when serving. When introduced into containers, it can be transported to a recycling point at pressures of preferably 1 mbar to 70 bar, containers being thermally insulated. The nature of the CO ₂ is adapted to the requirements, for example by solidifying to carbon dioxide snow, dry ice and / or liquefying to form liquid CO ₂ .

CO ₂ , preferably from treated biogases, is used in particularly preferred uses via devices for fine-pearly gas distribution, preferably in free-growing plant field crops / outdoor crops for establishing a CO ₂ concentration of preferably 0.05 to 0.25% by volume and in aquacultures as CO ₂ - Fertilizer initiated to develop its effect as a carbon source for growth for preferably autotrophic and combined autotrophic / heterotrophic beings.

Exhaust gas CO ₂ is introduced into a greenhouse, which is formed in particular by a mobile, temporary or permanently installed stationary film tunnel covered with plastic films, for example for an outdoor vegetable crop of young plants. The CO ₂ transported in by pipeline is first temporarily stored and then removed from the gas supply, which can be a pressure bottle set up near the film tunnel and / or a film gas storage device. Carbon dioxide is introduced into the film tunnels via a plurality of lances, nozzles, perforated hoses and / or perforated mats laid on the wall side and / or in the middle of the film tunnels, preferably on the floor, to form a gas distribution system. The gas distribution system can be quickly installed and collected again and is mobile and reusable. Several foil tunnels can be supplied from a gas supply by laying pipes and / or hoses to the foil tunnels and connecting them to the gas supply system inside the tunnels. By such a CO ₂ supply the rapid CO ₂ deficiency is counteracted, which otherwise adjusts in foil tunnels rapidly. The use of special films that are perforated to improve the gas exchange and the supply of the rapidly growing young plants with CO ₂ from the ambient air can be reduced or even superfluous.

Carbon dioxide can also be supplied chemically and physically dissolved in the irrigation water, the CO _{2 being contained} in the process water or process water from a physico-chemical process of pressure washing biogases in aqueous solution.

When using CO ₂ for extraction, CO ₂ , preferably from treated biogases, is introduced into plants for the extraction or high-pressure extraction (HDE) of natural substances, preferably with supercritical CO ₂ , preferably of aromatic substances, colorants and / or caffeine from plants or parts thereof , preferably from single and multi-cell algae and / or coal.

The relaxation cooling is used when CO _{2 is} used for cooling. When liquid carbon dioxide, preferably from treated biogases, is depressurized to a pressure of preferably 1 bar at a CO ₂ temperature of preferably -80 ° C., carbonic acid snow is formed which, in presses, has dry density of preferably 1.2 to 1.8 kg / l is solidified. Liquid CO ₂ , carbonic acid snow and / or dry ice can be used in the preferably encapsulated cooling / freeze grinding of organic substances such as composites, tough and elastic materials (e.g. vinyl plastics, polystyrene, acrylic resins, old tires and other rubber waste), oxidation-sensitive substances such as carotenes, A- Vitamins, substances in which loss of aroma are to be feared, such as coffee, spices, hop pellets, also hormones, penicillin and / or other drugs, plastics and / or foods and stimulants, in order to protect the goods against the entry of oxygen and / or to make them brittle and to facilitate the grinding process, to prevent dust explosions, to cool or freeze food, preferably in cooling and freezing tunnels and cabinets, preferably superficially or completely quickly.

Carbon dioxide, preferably from treated biogases, is added by a user in encapsulated inert gas packaging techniques (MA modified atmospheres, CA controlled atmospheres), in bags, trays, glasses, sleeves, capsules, bottles, foils, cups, cans and / or boxes and to cool preferably during the packing process. Cooling can be provided, for example, by cryogenic liquid injection of CO ₂ and / or addition of carbon dioxide snow and / or dry ice, even in heat-developing processing processes such as kneading, mixing or chopping. The cold chain can be maintained during the transport of freshly frozen or chilled goods by adding carbon dioxide snow without further expenditure for a cooling machine.

Liquid bottled CO ₂ , preferably from treated biogases, is used in carbon dioxide snow extinguishers and / or as a coolant for reactors and in refrigeration machines. It is used to freeze / winterize oils and fats to separate the higher melting parts.

The use of CO ₂ for cleaning is based on embrittlement, which is used when using dry ice, preferably from treated biogases, in particle size / pellets in the process of dry ice radiation. The snow is pressed through a die of a pelletizer using, for example, a hydraulically driven punch. Depending on the die, the product is cylindrical dry ice pellets with dimensions of 1 mm to 6 mm in diameter and 5 to 15 mm in length. Dry ice radiation has a similar effect to sandblasting and removes unwanted foreign bodies such as oils and fats, food residues, paints and varnishes, welding residues, adhesives and resins, plastics and rubber, concrete and tar residues, all deposits and dirt from any surface and cleans them. For example, CO ₂ can be used for cleaning replacement engines, stripping paint from aircraft and rail vehicles, removing release agent residues in presses and molds, removing residues from vulcanization processes, removing product residues, cleaning buildings, cleaning and decontaminating nuclear plants, cleaning printing machines without dismantling and Removal of rust protection paints, varnishes, resins, adhesives, oils, greases and / or bitumen can be used. It is therefore also suitable for cleaning circuit boards and printed circuit boards since it is not corrosive.

When using CO ₂ as a chemical raw material, CO ₂ , preferably from treated biogases, is used in a wide variety of industrial processes. It is used in urea synthesis, the production of ammonium carbonate, as a fertilizer, for the synthesis of preferably methanol or cyclic carbonates of the ethylene carbonate type from simple oxiranes such as ethylene oxide (for solvents such as propylene carbonate and hydroxy compounds), in the plastics industry by esterification, polymerisation , Polyaddition and / or polycondensation, preferably by forming aryl and / or alkyl esters, for example mono- or poly-ethylated and / or mono- or poly-methylated carbonates, polycarbonates or polyester polycarbonates, for the production of salicylic acid, for example in the Kolbe-Schmitt process as well as for soda production, for the production of lead white, barium carbonate, chalcocarbonic acid, etc., for the neutralization of alkaline waste water and / or process water from the processing industries, for the acidification of process water, preferably thallus oil, in the paper industry, as an inert gas in chemical processes s, in baking powders, effervescent powders, in CO ₂ lasers and / or in gas chromatography.

It is advantageous to generate CO ₂ nitrogen-free carbon oxide CO by allothermal and / or authothermal generator gas reaction with all non-baking coals, for example lignite, for coal gasification. Instead of the generator gas reaction, an allothermic and / or authothermal synthesis or water gas reaction can also be used, for example in the Lurgi pressure gasification process with fixed bed reactors (in which briquettes or coal bulk material of 10-30 mm grain size are used in countercurrent) in Fluid bed process / fluid bed / dust flow process in Winkler generators (with fine-grained coal of 1-10 mm grain size in cocurrent), with the Koppers-Totzek process, (with coal dust of <0.1 mm grain size in cocurrent together with the gasifying agents horizontally is blown into the center of the reactor (entrained flow carburetor). Carbon oxide can also be produced from carbon dioxide during cleavage at high temperatures and / or in continuous operation, preferably by the Calcor process.

Coal gasification will be the coal refining process that will be the largest in the future Will have importance for the provision of organic basic chemicals. Out Synthetic methanol can be used to manufacture adhesives. Carbon dioxide becomes a synthesis of carboxylic acids and esters by carbonylation, preferably oxo synthesis, Koch's carboxylic acid synthesis and / or hydroformylation, e.g. B. from ants or Acetic acid, phosgene, formates, formamides, acrylates, isocyanates, for the synthesis of aromatic aldehydes, for the production of the purest metals, preferably via the Metal carbonyls, used by catalysts preferably over carbonyl complexes.

In the steel industry as a user, CO ₂ , preferably from treated biogases, is used preferably for cleaning forging molds and for producing casting molds.

In the use of CO ₂ in medicine, CO ₂ , preferably from treated biogases, is used in the form of natural and artificial baths against cardiac and circulatory disorders; The CO ₂ penetrating through the skin in carbon dioxide baths (water-soluble mixtures of hydrogen carbonates and organic acids, e.g. fruit acids) for dermatological purposes also stimulates the circulation and causes a strong blood circulation and reddening of the skin. Percutaneous exposure to CO ₂ concentrations in the range between preferably 45-90% lead to a slowing of the pulse and an increase in blood pressure, thus influencing the cardiovascular system in the sense of vagotonia, also as a component of the Kissinger salt, which is used as a therapeutic agent against gastric, Bowel and metabolic disorders are used.

When using CO ₂ in the photo, film, television, theater, concert and video industries, the high temperature difference between dry ice and / or carbon dioxide snow from liquid CO ₂ , preferably from treated biogases, becomes its environment used, wherein CO ₂ sublimes in contact with the air and / or liquids of preferably 0 to 90 ° C, begins to boil and / or forms slime. These phenomena can be used to create or simulate slime, steam, mist, evaporation and / or cooking effects and provide the required mood. Effects are preferably created in connection with fog machines.

The filtered and / or settled culture water taken from uncontrolled extensive and / or controlled intensive, artificially illuminated aquacultures or aqua-algae cultures can be bypassed in the culture for pressure washing of CO ₂ -containing gases and exhaust gases, preferably biogases in the corresponding commercial physico-chemical alternating pressure systems used and loaded with the chemically and physically dissolved CO ₂ back into the culture, so that a water cycle is formed. As a result, the water can replace the commercial solution for CO ₂ absorption, for example monoethylene amine, which is otherwise used in pressure washing in a first washing stage. Likewise, the algae culture water can replace commercial liquids in membrane technology, preferably in liquid-flowed hydrophobic membranes, which are flown with biogas from the outside. The commercial pressure washing system / alternating pressure system can also be preceded by a gas scrubbing operating at constant pressure. Such a gas scrubber can preferably be a tube scrubber, which is characterized in that it has vertical, preferably vertical tubes. The tubes are preferably 3 to 10 m long and have a diameter of preferably 5 to 50 cm. Biogases are introduced from below in counterflow to aqua / algae culture water with a blower or compressor in fine bubbles. Internals for gas and liquid deflections for better mixing of the phases and gas exchange can be contained in the tubes, preferably packing elements, deflection projections, sieve trays, boiling trays and / or distillation trays. The hydraulically predetermined pressure in the biogas which is largely free of CO _{2 and} flows out at the top is preferably increased to 1 to 50 bar. This is done, for example, via a reducing valve and / or a booster pump. The gas is returned to the pipe gas scrubber with the booster pump. This further reduces the residual CO ₂ content in the washed biogas. The daily cycle of CO ₂ requirements is taken into account by the pressure level, the amount of biogas washed and / or intermediate buffers for CO ₂ and methane. The washed biogas is then fed either via an intermediate buffer or directly to the commercial pressure change system, continuous gas permeation and / or discontinuous PSA systems (pressure change absorption systems) with molecular sieves or activated carbon for post-purification, while the water removed from the bottom, enriched with CO _2, is preferred is returned to the deeper layers of the culture in such a way that it is evenly distributed and the CO ₂ dissolves in the water body of the aqua or aqua algae cultures during relaxation. The CO ₂ enrichment in the bypass has the advantage that the necessary back pressure is achieved through the pipe length. The construction of such depressions of about 10 m in ponds is expensive. There is also a fear of silting up the depressions. The separately installed gas scrubber enables easy access.

For deodorization, the exhaust gas can preferably be treated in activated carbon filters. This avoids the effects of taste and smell during recycling. CO ₂ itself is tasteless and odorless, non-toxic and suffocating.

Carbon dioxide is transported at pressures of preferably 1 mbar to 70 bar, temperatures of preferably 1 to 80 ° C. and relative humidity of preferably 0.01 to 80% in pressure, CO ₂ and corrosion-resistant pipeline supply networks.

Measuring probes are permanently installed, preferably at inlet and tapping points, CO ₂ stores, branches and interfaces to measure physical parameters, pressures, temperatures, humidity, flow rates, fill levels, conditions and / or activities of work machines and actuators and safety elements. The measured values are registered and forwarded to central computers, so that an MSR chain is made possible and maintained. Measured values about preferably performance and activity states are preferably also recorded and forwarded by all devices, machines, motors, apparatus, shut-off, actuating and safety elements that perform work and are part of the MSR chain. Pressures are generated with compressors, preferably pumps, compressors such as reciprocating compressors, screw compressors, and / or blowers, and pressure drops are overcome. Pressure differences serve to promote carbon dioxide. In overhead lines which connect decentralized networks with one another, CO _{2 is} preferably transported in liquid form, in order to reduce the volume preferably by 90 to 99.5%, while in decentralized supply networks to which producers and / or consumers are preferably connected in high density and are connected at a short distance, the gas is fed, transported and extracted in gaseous or liquid form, depending on the local conditions. Branches and interfaces of networks with gaseous and liquid CO ₂ are preferably provided with complete liquefaction and / or evaporator stations in order to change the state of aggregation. Released heat and / or cooling capacity is used by heat exchangers and is available for general purposes. It is particularly advisable to use heat in combined condensing / evaporating stations to supply energy for evaporation and cold for cooling during liquefaction.

For the temporary storage of liquid CO ₂ , above / and / or underground tanks / storage facilities are installed in connection with preferably flexible gas buffers, in particular in the vicinity of production and consumption points, which have a capacity of 50 to 500 times the hourly capacity to compensate for weekly, monthly and / or seasonal fluctuations in demand and / or production.

In the production sites, trace components such as preferred are added before the feed Oxygen, nitrogen, non-condensable gases, nitrogen oxides, methane, alcohols, Carbonyls, esters, ethers, solids, acrylates, cresols, phenols, aerosols, benzene, benzene, Hydrogen sulfide, sulfides and / or moisture by concentration and / or Purification process removed to values of preferably 5 ppb v / v to 100 ppm v / v. As  Cleaning processes are preferably molecular sieves, absorption, adsorption, Oxidation, reduction, stripping, distillation and / or rectification are used.

The uses disclosed as such and also in connection with the further details of the respective uses or a combination of several of the disclosed uses are advantageous uses also for carbon dioxide which is not transported through a pipeline network but in batches. This applies in particular to the use of CO ₂ for preservation in storage facilities / silos, closed rooms, for laying pipe and / or hose systems in storage facilities / silos with a CO ₂ connection and the addition of other substances, to reduce the risk of fire in storage facilities , Silos, grinding and / or conveying devices, round and square bales, in mountain rooms for storing bales, for use in baling machines, in the beverage industry, as a carbon source in greenhouses and / or film tunnels, in aqua and aqua algae cultures using the bypass process pipe washing and replacement of conventional CO ₂ absorption liquids, in cooling and freezing processes, in protective gas packaging techniques, in cleaning techniques, in the chemical industry as a chemical raw material, in the steel industry, in medical technology, in the photo, film, TV and video industry. A separate protection can be directed at this, which is not limited to the origin of the gas from a pipeline network. The installation of CO ₂ systems on balers and bale wrapping machines, the pressing of lines in bales and the loose laying of lines in bale stores as well as the bypass process in aqua and aqua algae cultures of tube washing and the replacement of conventional CO ₂ absorption liquids is new. The applicant reserves the right to provide separate protection, which can be independent of the origin of the CO ₂ .

Preferred exemplary embodiments of the invention are described below with reference to figures explained. Show it:

Fig. 1 connects an inventive pipeline network, the producer and consumer of carbon dioxide with each other,

Fig. 2 generators in which carbon dioxide is produced as exhaust gas and preferred uses of carbon dioxide,

Fig. 3 is a horizontal silo,

Fig. 4 is a biogas reactor having two reactor tanks and a separate preliminary tank as premixing,

Fig. 5 shows a reactor vessel with a built-side shaft as premixing,

Fig. 6 the side slot of Fig. 5 in a different section,

Fig. 7 is a series circuit of a horizontal and a stationary reactor vessel,

Fig. 8 is a biogas storage and biogas separation

Fig. 9 the memory for desulphurised biogas according to FIG. 8 and

Fig. 10 is a gas separation device.

In Fig. 1, a series of carbon dioxide generators and carbon dioxide sources are shown together with potential users in a carbon dioxide-line composite of example.

That which is generated or otherwise incurred on the part of the producers or the sources Carbon dioxide is processed as a product in such a purity that it is arbitrary Can be offered to consumers as a carbon dioxide product. Preferably still on site a device for producing the carbon dioxide product, for example one Biogas plant, the carbon dioxide product is converted into a fixed gas or liquid Piping system initiated specifically for the carbon dioxide product. A first one Piping system for the transport of gaseous carbon dioxide product and a second piping system for the transport of liquid carbon dioxide product by means of one or more stations for the liquefaction and / or evaporation of the Carbon dioxide product linked together.

In the exemplary embodiment, there are two fixed, local piping systems, one for one gaseous carbon dioxide product and the other for a liquid carbon dioxide product a first station for the liquefaction and / or evaporation of the two Carbon dioxide products linked together. Form these two piping systems overall a common, local first piping system. Another one Piping system for gaseous carbon dioxide product and another Pipe system for liquid carbon dioxide product form a common, local second piping system. In the exemplary embodiment there are local second ones Piping system only consumers connected. It could be the second local  Piping system, however, also additional producers from the local area of the second local piping system.

The first local piping system and the second local piping system are over one only landline interconnected. For transportation through the landline becomes the gaseous carbon dioxide product from the local first pipeline network liquefied and partly through the station for the second local piping system Liquefaction and / or evaporation of this local second piping system evaporates. Since the two connection stations are preferably used as condensers and evaporators are designed, these two stations can also be used as exchange stations for gaseous and liquid carbon dioxide product within their respective local piping systems be used.

A variety of local piping systems can be used in the manner shown Overland lines to be connected to an overall network. Within the local Pipeline systems and also in the overland pipeline are compressors and storage or Accumulators arranged. As a result, the uniform supply with the Carbon dioxide product ensured and a desired line pressure set and be maintained.

Fig. 2 shows as preferred carbon dioxide generator landfills and biogas plants. In landfills and biogas plants, carbon dioxide is usually generated as exhaust gas when methane is extracted. However, instead of flaring the carbon dioxide off-gas or simply releasing it into the atmosphere, as is currently the case, a methane product and the carbon dioxide product are obtained from a biogas generated in the biogas plant or a landfill gas. The methane product and the carbon dioxide product are transported to the respective consumers in separate piping systems. Preferred uses of the carbon dioxide product are given by way of example in FIG. 2.

In the following figures, a particularly preferred method and a particularly preferred device for generating the carbon dioxide product and Methane product described.  

Fig. 3 shows a driving silo T1 in a cross section and below in a view. Energy plants, preferably silage maize, rapeseed, wheat, rye, millet, alfalfa, fodder beet, sugar beet, potatoes and / or grass, are preferably chopped as whole plants with forage harvesters, transported to the silo T1 and ensiled there. The ensiling process comprises the addition of ensiling aids, such as molasses and / or seed cultures, preferably compacting the loose bed to a bulk density of preferably 300 to 600 kg / m ³ and covering with silage film M1. The driving silo T1 is equipped with a horizontal pipe R1, preferably laid along the upper edge of the silo, preferably 1/2 to 3 inches in diameter, with vertical branches, preferably at a distance of 2 to 4 m, to the silo floor. The vertical branches have connections Fl1 at the ends. From these connections, perforated lines, preferably hoses R2, are laid on the silo bottom and on the compacted plants, via which a quantity of carbon dioxide, preferably 1 to 3 times the pore volume, is added via directly connected pressure cylinders T15 or via a blower K5 both after compacting and after covering with foil M1 at the beginning of the ensiling process to displace the oxygen and to reduce the ensiling losses. The hoses R2 laid on the floor advantageously lie in recesses or depressions. With T2 a septic tank is designated.

Fig. 4 shows a Biogasreator T4 with an upstream, separate premixing device in the form of a preliminary tank T3. The biogas reactor T4 is formed by two reactor tanks T4a and T4b, which can be operated individually, in parallel or in series. The reactor vessels T4a and T4b are referred to below as reactor T4 or as partial reactors.

The finished silage is removed from silo T1 using a wheel loader and / or a gripping device removed, filled into a tipping hanger or on a conveyor belt, to the pre-pit T3 transported and dumped into this. The tipping trailer is transported on the Road or rail. There can be ensiling in a silo but also at the location of the Biogas plant be available.  

There is preferably some fresh manure and / or in the pre-pit T3 beforehand Bedding and / or solid manure. The pre-pit T3 is filled with manure after the silage has been tipped over and / or digestion water and the mixture is fixed in the pre-pit T3 Agitator Rü1, preferably a cutting agitator, homogenized and preferably crushed until a dry matter content of preferably 10 to 30% is obtained.

In the pre-pit T3 organic waste and / or liquid manure are placed, which previously were preferably heated. A WT2 heat exchanger from the system is used for this. The in Heat exchangers WT2 are heated in a holding tank T7, preferably with an additional heating is provided, preferably at 70 to 75 ° C for preferably 30 to 60 min thermally hygienized. You can via a pump P6 via a line R3 in the Pre-pit T3 and / or pumped from a line R4 into the biogas reactor T4.

The mixture in the preliminary pit T3 is fed with a thick matter pump P1 via the line R4 either via a valve V8 or a valve V9 or both valves in one of the standing Sub-reactors T4a or T4b or transported to both sub-reactors.

Fig. 5 shows a standing T4 biogas reactor with an integrated premixing T3. FIG. 6 shows the side shaft T3 in a section perpendicular to FIG. 5. The premixing device T3 is formed directly on the biogas reactor T4 as a side shaft. The side shaft is also labeled T3 because of the same function as the pre-pit. The two partial reactors T4a and T4b in the exemplary embodiment in FIG. 4 can be designed like the reactor T4 in FIGS. 3 and 4, in particular each be provided with a side shaft T3. A separate pre-pit is preferably omitted in this case. The pump P1 and parts of the pipeline R4 can be omitted or used differently.

The ensiled, solid, pourable materials, manure and / or organic waste are in the Side slot T3 filled. When designing the biogas reactor T4 in the form of several Sub-reactors with integrated side shafts T3 are these materials when operated in parallel filled each of the side shafts T3. The light vegetable substances tend to Bridge formation and are difficult to move down. The function of the Side shaft T3 is improved by devices according to the invention. Preferably  contains such a side shaft T3 a lid, which is preferably opened as Tilt wall for solid materials. The cover closes the side shaft T3 preferably odor and splash proof. In the side shaft T3 is preferably a Cutting agitator designed Rü1 attached, which the substances together mixed and preferably crushed. The standing vessel of the reactor T4 points in Side shaft T3 preferably two openings Fl2 and Fl3 at different heights on. The two openings Fl2 and Fl3 are preferably diagonally one above the other, so that a horizontal flow in the side shaft T3 also arises.

The upper opening Fl2, which is preferably 2 to 100 cm below the side slot cover lies and in several, preferably over 20 to 100% of the circumference of the container Seen width of the side shaft T3 is divided partial openings preferably closable from the outside and / or from the inside. For this there is a closure V3 Flap with preferably non-return effect, a valve or a slide or Quick closing slide inserted. A is preferably at the bottom of the side shaft T3 promotional submersible mixer or a pump P2 parallel or perpendicular to the reactor T4 installed. When P2 is actuated, it flows through the preferably simultaneously opened closure V3 digested liquid from the standing reactor T4 in the Side shaft T3 and rinses the fresh fabrics, especially the solid, floating plant parts, directly in P2. The rinsing effect can be increased by the closure V3 only at a differential pressure of preferably 10 to 200 cm Water column suddenly opens. Digestion water preferably sprays into the side shaft T3.

P2 preferably conveys the substances into the reactor T4 in such a way that short-circuit currents to the or the upper openings Fl2 are excluded. The submersible mixer or the pump P2 can be arranged such that the conveying direction of P2 is perpendicular or parallel to the container wall through the opening Fl3. With the conveying direction pointing parallel to the vessel wall of the reactor T4, as shown in FIG. 6, the corner of the shaft T3 into which the agitator or the pump P2 is conveyed is preferably rounded off in order to reduce the frictional resistance and at the same time the direction of the flow in the Specify the reactor T4 tank. The radius of the rounding is preferably 1 to 8 times the cross section of the lower opening Fl3. An extension T3.1 of T3, which preferably extends into the interior along the vessel wall and has a cross section of 0.2 to 2 times Fl2 and a length which corresponds to at most half the circumference of the vessel of the reactor T4, prevents a short-circuit flow. P2 promotes the side shaft T3 preferably empty after the loading process. The lower opening F12 is then preferably closed from the outside and / or from the inside with a closure V3.1. The opening Fl2 can be made at the same height as P2 or 2 to 100 cm above P2, which would have the advantage that P2 cannot run dry.

The biogas reactor T4 can be divided into several, preferably at most 4 sub-reactors or Reactor vessel be divided. It is particularly preferred in two reactor vessels T4a and T4b divided, T4a preferably a standing or lying cylindrical Container is. Container T4b is preferably a standing cylindrical container. The Tanks of the biogas reactor T4 are preferably on the gas side and hydraulically with one another in connection. On the gas side, they are connected in series via a gas line R9 and directly with connected to a gas storage T8.

FIGS. 4 and 8 together show a complete biogas plant with biogas production, storage and separation.

If, as is preferred and shown in FIG. 4, the reactor consists of two standing tanks T4a and T4b, the tanks are preferably fed in parallel or in series by actuating the valves V8, V9, V10, V11 and V12. The containers are emptied through overflow lines R6 directly into a secondary fermentation tank T6, which is shown in FIG. 8, and / or by pumping. For pumping down, a pump P4 is connected on the suction side to the drain line R7 of the respective container by actuating the valves V10, V11 and V12.

A pipeline in which the valve V10 is located is indicated by a dashed line. By means of this connection and corresponding switching of the valves V10 to V12, the two sub-reactors T4a and T4b either in parallel or in series one behind the other operate.

The vertical cylindrical sub-container T4a and / or T4b preferably has a ratio of height to diameter of 0.2 to 4 to 1, is gas-tight and gas-side preferably at the highest point in a head space T5 or in a manhole Fl5 in the head space via the pipeline R9 connected to a biogas store T8 for raw biogas ( Fig. 8). The biogas storage tank T8 is advantageously integrated in the secondary fermentation tank T6. The headspace T5 of the biogas reactor T4 is under a gas pressure of preferably 1 to 100 mbar and preferably has a height of 30 to 200 cm. When pumping out digested liquid from the reactor T4, biogas flows into it from T8 and when the fresh substances are pumped into T8 to ensure pressure equalization in the headspace T5 of the reactor T4. In addition, the biogas reactor T4 is equipped with frost-proof, preferably hydraulic and / or as a bursting membrane, overpressure and underpressure protection devices, which are preferably attached to ports Fl6 and Fl7 at manhole Fl5. The overpressure safety device responds preferably at 50 to 150 mbar, the negative pressure device at preferably -2 to -10 mbar to the atmospheric pressure.

The standing cylindrical sub-container T4a and / or T4b preferably contains one slow-running agitator Rü2, which comes from an outside of the reaction space arranged direction of rotation variable motor Mo2 is driven. The agitator Rü3 has preferably a central, vertical shaft, preferably two Stirring blades are attached: Rübl1 preferably at the upper end of the stirring shaft below of the liquid level and Rübl2 preferably at the lower end of the stirring shaft in the Near the bottom of the container. The two stirring blades destroy Floating and sinking layers and homogenize the content. The stirrer Rü3 is preferably stopped at predetermined time intervals and otherwise preferably runs constantly. It is a completely mixed reactor, i. H. a CSTR. The agitator Rü3 can be formed by one or two submersible agitators preferably 20 to 200 cm below the surface and preferably 20 to 200 cm above are attached to the floor, which also applies to the stirring blades Rübl1 and Rübl2.

In the standing subtank T4a or T4a and T4b there are no openings for the agitator Rü3 and the overpressure and underpressure protection further openings for the manhole Fl5 in the Headspace T5, for a sight glass at the boundary between liquid level and headspace, for Pipes for pumping in and pumping out the liquid Fl10 and Fl9, for temperature and Pressure measurements Fl11 and Fl12 as well as a nozzle Fl13 for adding chemicals intended. The opening Fl10 for pumping in fresh substances is preferably 50 to  200 cm above the lower edge of the reactor. The opening Fl9 for pumping goes from the middle of the preferably conical or horizontal container bottom or preferably from the side of the container wall with the container bottom level.

The reactor T4 is thermally insulated all around with thermal insulation Iso 1 to ensure a k-value of ≦ 5 W / m ² K. A floor heating system WT1 with a heating output of 4 to 8 watts / (m ² K) is preferably installed in the base plate. The underfloor heating WT1 preferably acts in addition to the heat exchanger WT2 and is preferably fed with hot water via a heating pump. With the underfloor heating, small temperature differences to the reactor temperature of preferably <5 ° C are used. The reactor is preferably also heated when, for example, the supply of biomass is interrupted for a few days and / or the heat exchanger WT2 is not in operation.

The biogas reactor is preferably heated to 26 to 36 ° C. preferably via the external countercurrent and / or cross-flow heat exchanger WT2, preferably a tube bundle heat exchanger, plate heat exchanger, spiral heat exchanger and / or slurry-slurry heat exchanger, which is thermally insulated with Iso 2 , preferably to ensure a k value of ≦ 3 W / (m ² K). The heat output of the heat exchanger WT2 is dimensioned such that preferably the entire material flow of the biomass, preferably in connection with the heat exchanger WT2 and the holding tanks / sanitation tanks T7.1 and T7.2, preferably to ≦ 40 ° C or preferably only partial flows such as liquid manure and / or organic waste can be heated up to preferably 75 ° C. and preferably with this energy the reactor can be brought to the desired temperature of preferably 26 to 36 ° C. The energy is preferably supplied with hot water and / or steam of preferably ≦ 130 ° C. from an energy station T10 at the location of the system. It is particularly advantageous if waste heat from the encapsulated compressors used in the system for the gases biogas, methane and carbon dioxide for heating T4, T4a, T4b, T7, T7.1, T 7.2 and in WT2, WT3 and / or WT4 is used. As is well known, only about a third of the electrical connected load is converted into compression work, but about 2 thirds into waste heat. If necessary, a partial liquid stream preferably heated to 75 ° C. or the entire stream in preferably two to four, preferably alternately charged, hygiene tanks T7, 1 and T7.2 can be kept at this temperature, preferably for 30 to 60 minutes. The ≦ 75 ° C hot hygienized substances are pumped with the pump P6 into the counterflow heat exchanger WT2, particularly preferably a liquid manure-liquid manure heat exchanger, and / or into the biogas reactor T4 and / or the premixing device T3.

The homogenized mixture is from the premixing device T3 by means of the Thickness pump P1 distributed at once or preferably in up to 3 throughout the day Batches through line R4, with appropriate control of valves V6 and V7 via the external heat exchanger WT2, into the biogas reactor T4 or in the latter Pumped T4a and / or T4b. Before in T4 or container T4a and / or T4b is pumped, preferably the same amount is pumped out of the biogas reactor, if not switched to overflow. The pumped volume is selected so that in the biogas reactor or in all sub-reactors of T4 without T6 taken together preferably an average hydraulic residence time of 15 to 80 days is guaranteed.

FIG. 7 shows a particularly preferred embodiment alternative to the standing part containers of FIG. 4 with a lying part container T4a and a standing part container T4b connected in series therewith. If the reactor T4, as preferred and shown in FIG. 7, consists of a horizontal and a vertical tank, the tanks are hydraulically connected in series so that the horizontal tank T4a is first fed via the pump P1. The overflow flows into T4b without further pumping work.

The lying cylindrical container T4a with a circular cross-section is set up on supports which are preferably 2-4 m apart. It has a volume of 100 to 200 m ³ and contains a continuous horizontal agitator Rü3, the agitator-carrying shaft of which is mounted at the two ends and additionally at intervals of preferably 2-4 m. The reactor ends are preferably designed as dished heads. The container T4a contains a manhole Fl5 at each end. Preferably, the first third of the container is enclosed on the underside with a WT4 heating jacket. The connector Fl 13 is used to add chemicals and preferably protrudes 10 to 20 cm into the container. Stirrer arms are attached to the stirrer shaft at intervals of preferably 0.5 to 2 m. Each stirring arm is offset from the neighboring one by an angle of 18 ° to 36 ° on the shaft. The mixed substances with preferably 5 to 40% dry matter are pumped into the horizontal fermenter T4a with the pump P1 via the pipeline R4 and valve V5, which is preferably a non-return flap, pass through the fermenter in preferably 4 to 10 days and preferably come together the formed gas through a pipe R5 and a check valve V15 into the standing fermenter T4b. As a result of this procedure, the horizontal fermenter T4a is constantly filled, is under the pressure specified by the liquid column in the vertical reactor T4b and does not require a gas dome. Accumulations of deposited substances are preferably occasionally drawn off via a screw (not shown) attached at the end. The delivery through the container T4a is preferably carried out by the pump P1 and not by the agitator Rü3.

Fig. 8 shows the storage and separation of the biogas.

The biogas storage tank T8 is preferably a low-pressure gas storage tank which, when installed separately, is accommodated in a preferably fire-retardant casing. T8 is advantageously integrated in the secondary fermentation tank T6 as a cover. The post-fermentation tank T6 is equipped with a Rü 4 agitator, which is driven by a Mo4 motor and is attached to the side. The memory T8 is sealed off from the air by a membrane M2, in particular a film. The post-fermentation tank T6 forms part of the reactor T4.

In the previous biogas storage facilities, a gas space above a closing membrane is exposed to the air, deliberately ventilated and / or pressurized to give the biogas a pressure under the membrane. On the other hand, according to the invention, contact with air and in particular oxygen is prevented for the production of marketable, natural gas-like biomethane and carbon dioxide. The purity of carbon dioxide is subject to particularly high requirements. Therefore, a very low permeability for air at 0 to 30 ° C of preferably at most 150 cm ³ / (m ² bar24 h) is required for the membrane M2. In the case of inexpensive membranes with permeabilities in the upper range which is still permissible according to the invention, a protective space M3.1 is preferably formed in order to improve the insulation. This protective space M3.1 is preferably flushed with process gases, preferably with biogas and / or carbon dioxide, instead of with air. The protective area M3.1 can be divided several times and / or in particular can be formed by a plurality of protective areas M3.1 one above the other. Prefabricated shelters can be attached to gas stores, which are preferably designed as sacks and / or pillows. After passing through the shelter M3.1, biogas is preferably used to generate process energy in an energy station integrated in the system. Passed carbon dioxide is preferably used as fertilizer in greenhouses and / or for disinfestation of camps where the oxygen content does not interfere.

An overall very low passage of air is preferably ensured by a stainless steel membrane, a metal-coated plastic film and / or at least one two-layer membrane M2. Two layers are preferably formed by flexible Plastic films or through a gas-tight, rigid container cover with an underlying one flexible film, the protection area M3.1 preferably with raw biogas, desulphurized biogas or carbon dioxide and preferably flows through it After leaving the shelter M3.1, biogas preferably in the energy station is consumed. The protection area M3.1 has a constant or variable volume. On constant volume of the protective space M3.1 is preferred for gas bags and Gas cushion achieved by the two preferably flexible and / or stretchable films are separated by spacers. Due to the shape of the spacers, a controlled gas flow are supported to prevent short circuit flows. The Spacers can be gas-tight or porous with a pore volume of up to 99.9% his. The shelter M3.1 can be divided into several rooms, preferably each have their own gas inlet and gas outlet. The gas storage T8 can, like the others Gas storage of the plant also, several layers of Protection rooms included to improve insulation against air entry.

A shelter M3.1 with a variable shelter volume turns up at the Combination membrane / rigid plate, for example between one in a rigid Container attached flexible membrane and the side walls and roof of the container, because the flexible and / or stretchable membrane, in particular film, the degree of filling adjusts. This leads to the protective space becoming larger when the gas storage volume gets smaller and vice versa. The total amount of gas in the shelter M3.1 and in Memory T8 remains the same.  

The invention preferably provides air access to the stored raw and / or desulphurized biogas prevented. In addition, an overpressure of preferably 1 to 100 mbar is generated in the protective room M3.1 and in the stored biogas variable protective space volume supports the work of a blower K1 and / or K2.

In addition to the storage T8 serving as raw gas storage, the biogas storage a separate clean gas storage tank T11. Desulfurized is in the clean gas storage T11 Biogas stored. Above the clean gas storage T11, the Practice for oxygen-impermeable membrane M3 again a protective volume M3.1 formed, which is constantly connected to the protective volume M3.1 of the raw gas storage T8 or can be connected if necessary.

With regard to the clean gas store T11 and its intermediate volume M3.1, reference is also always made to FIG. 9. The clean gas storage device T11 is designed as a double-walled gas storage cushion or bag with an internal storage device T11, surrounding flexible intermediate space M3, 1 and a fire-retardant covering T9 surrounding the same. With regard to the double-layer membrane M3 and the protective volume M3.1 formed by the membrane M3, the same applies to the membrane M2 and its protective volume M3.1. All gas stores of the system can be designed like the clean gas store T11.

Preferably, a partial flow of the raw gas blower K1 driven by a motor and / or the clean gas blower K2 driven by a motor and / or the CO ₂ blower K5 driven by a motor Mo10 is fed into the spaces M3, 1 between M2 and / or M3 in the gas storage T8 and / or T11 directed in series or in parallel. The gas storage device T8 is preferably connected to a torch which can flare off sudden excesses of biogas. If the gas storage device T8 were set up separately, a valve, such as valve 16 of the storage device 11 , via which condensate is drawn off, would preferably be attached at the lowest point. The flexible casing M3 of the gas storage device T11 is preferably connected to a device which indicates the fill level. The blower K1 connected on the suction side to the gas space of the biogas store T8 provides the necessary admission pressure in the raw gas for a preferred forwarding of at least one partial flow into the intermediate space M3.1 from M3 and / or to the energy station and / or to a gas separation device T12.

The H2S concentration in the raw biogas is preferably reduced to 1 to 500 ppm, by preferably iron-III in T4a and / or T4b via a metering pump P3 preferably proportional to the sulfur content of the fresh substance mixture supplied and / or biogas volume flow is added. The addition can advantageously also directly into the premixing device T3.

Advantageously, this desulfurization forms a preliminary stage and the complete one Desulphurization of the biogas takes place in a first separation stage of the gas separation device T12. The desulfurized biogas (clean gas) is preferably in the separate Pumped gas storage T11 and from there is the gas separation device T12 and / or preferably after passing through the spaces M3, 1 of the membranes M2 and / or M3 of the energy station available.

According to the invention, the energy station T10 extracts raw and / or desulfurized biogas via the blower K1 from the biogas store T8 for raw biogas, via gas line R11 the space M3.1 from T8, from the space M3.1 of the gas reservoir T11 for desulphurized biogas and / or directly from T11 via the blower K2 and gas line R 10th

The energy station T10 preferably consists of a combined heat and power plant (CHP) Type petrol engine or pilot heater, which has a temperature spread of preferably works at 70 to 130 ° C, a fuel cell and / or Absorption refrigeration pump and / or a boiler. That in the energy station accommodated CHP and / or the fuel cell's job is to put so much energy on To generate electricity, heat and / or cold from biogas that preferably the Energy requirements of the biogas plant and the gas separation device for electricity, cooling and / or Heat is covered. If it is economical, agricultural can also be used Companies are supplied with electricity, heat and / or cold. Additionally or alternatively to the CHP is preferably an absorption heat / cold pump and / or a boiler set up, which preferably generates the required heat and / or cold from biogas. It is  also advantageous if the energy station only needs process heat and Process cold covers and the process electricity needs from the public grid becomes. With preferably simultaneous use of heat, for example for heating of substances in the heat exchangers, and cold, for example in the condensation of Humidity and with the CO2 compression from the absorption heat / cooling pump is the Efficiency 1.1 to 1.9 times better than that of a condensing boiler. Electricity will preferably obtained from the network if no cogeneration is installed. The Energy station is housed in a container, preferably runs fully automatically via its own EI&C and PLC system and the level of the biogas storage, the gas volume flow, the methane content and / or the energy requirement of the biogas plant preferably controls electricity, heat and / or cold. The CHP is preferred heat-controlled to the temperature in the biogas reactor, in the external heat exchanger, during the sanitation and / or in the gas separation facility and the To provide energy.

The biogas separation device T12 preferably takes biogas from the gas storage T8 for raw biogas via the blower K1. In a desulfurization stage T12a, the one Cold trap for condensate removal follows, H2S is removed. The desulfurization in the Gas separation device T12 is preferably used in addition to a desulfurization Chemical addition carried out in the biogas reactor T4, for example that described Iron III addition. In this case, desulfurization takes place in two stages. In the Gas separation device T12, the sulfur content of the biogas to 5 ppm or less diminished. Desulphurization to preferably 5 to 500 takes place in the reactor T4 ppm. The desulfurization in the gas separation device can be done after another preferred embodiment may also be the only type of desulfurization. Also in this Trap, the sulfur content in the desulfurized biogas is reduced to 5 ppm or less. Preferably, the entire biogas is desulfurized and not just the part that is not in the Energy station is used. The biogas desulphurised in the desulphurization stage can the separate gas storage unit T11 for desulphurized biogas. The desulfurized biogas is either either right after the desulfurization step a subsequent CH4-CO2 separation stage T12b or the clean gas storage T11 Intermediate storage supplied or two partial streams are formed, one for  Separation stage T12b and one to T11. From T11 it becomes the clean gas blower K2 and Gas line R10 removed with valve V18 open for CH4-CO2 separation.

The gas separation device T12 is preferably controlled completely automatically and controlled, preferably by an EMSR and PLC system. The Gas separation device T12 preferably consists of with changing pressure working PSA modules, in particular molecular sieves and / or absorbent Liquids, for the enrichment of methane or the separation of carbon dioxide. The PSA modules are preferably preceded by activated carbon filters Adsorption of hydrogen sulfide and odorants and molecular sieves for halogenated components. In place of the PSA modules with constant and Low overpressure working membrane modules occur that are selective from the biogas Remove hydrogen sulfide and / or carbon dioxide. They preferably consist of hydrophobic, liquid-flowed membranes, which are preferred with the biogas flow in cross or counterflow. The gases diffuse through the membrane into the liquid, preferably in the first separation stage hydrogen sulfide and in the second separation stage carbon dioxide from that for this purpose, respectively selected liquid are preferably selectively absorbed.

The gases biomethane and carbon dioxide emerging from the gas separation device T12 have a purity of preferably at least 95.0% by volume. The methane loss is preferably less than 5%. Biomethane, which is the same as natural gas, is preferably odorized with tetrahydrothiophene (THT) in a concentration of preferably more than 10 mg / m ³ in an oding station (not shown) and either compressed to preferably 250 bar and preferably via a Mo8-driven, preferably two to three-stage compressor K3 Bottled pressure cylinders T14 and / or compressed via a compressor K4 driven by the motor Mo9 to a pressure above atmospheric pressure, preferably to a pressure in the range from 100 mbar to 100 bar, and fed via a volume flow measurement through a pipeline R14 into a natural gas network. The guide variable for feeding into the natural gas network and thus for controlling the gas separation device is preferably the CH ₄ content and / or the methane number and / or the Wobbe index of the biomethane to be fed. The Wobbe index is preferably between 10 and 15 kWh / m ³ . If the predetermined value for the guide variable is not reached, the biomethane is returned to the gas separation device T12 or preferably to the gas storage device T8.

Carbon dioxide is preferably passed through an air-permeable low pressure accumulator T13 as an intermediate buffer. From the store T13, the carbon dioxide is filled with a motor-driven compressor K6 as liquid CO ₂ into pressure tank T15, for example pressure bottles or tankers, and / or introduced into pipes for liquid CO ₂ and / or as gas from the gas store T13 via the blower K5 emitted in pipelines for transportation of gaseous CO ₂ . The blower K5 preferably directs a partial flow into the intermediate space M3.1 of the preferably double-layer membrane M3 via a valve V19 in order to generate a stable excess pressure of preferably 1 to 100 mbar in the intermediate space M3.1. Excess CO ₂ is released into the environment. A membrane M4 is of multi-walled design, in the exemplary embodiment double-walled, and forms an intermediate space filled with CO2. The same applies to the membranes M2 and M3 for the membrane M4.

Fig. 10 shows a gas separation device T12 and the supply and discharge lines. The gas separation device T12 of FIG. 10 is expanded by a second methane-CO2 separation stage T12c compared to the gas separation device T12 of FIG. 8. The gas separation device T12 of FIG. 10 can be used in all embodiments of the invention as an alternative to the simplified embodiment of FIG. 8. What has been said above regarding the gas separation device T12 therefore also applies equally to the gas separation device T12 of FIG. 10. In particular, the embedding in the overall system is the same as in FIG .

Overall, the gas separation device T12 of FIG. 10 has three separation stages T12a, T12b and T12c connected in series. T12a forms the desulfurization stage and the two separation stages T12b and T12c are methane-CO2 separation stages, to which the above explanations for such separation stages T12a and T12b apply. Each of the two separation stages T12b and T12c is formed by several PSA columns, each filled with molecular sieves or liquid, which selectively absorb carbon dioxide and allow methane to flow through. The several PSA columns in each of the separation stages T12b and T12c are operated in batches, with an equalization in the product stream being achieved by parallel connection and staggered loading of the several columns in the respective separation stage.

In the PSA columns of the first methane-CO2 separation stage T12b, the methane-rich Partial stream M and a carbon dioxide-rich partial stream C in a manner known per se in one Get PSA procedures. The methane-rich partial stream M is, as already described, in T14 stored, or fed directly into a fixed methane pipeline network.

The carbon dioxide-rich partial stream C is formed in the PSA columns of the first methane-CO2 separation stage T12b during the desorption and subsequent evacuation. In the PSA process, carbon dioxide is absorbed at a pressure of 6 to 8 bar and desorbed when the pressure is subsequently reduced. At the end of the desorption, a slight negative pressure is applied, so that it is evacuated. At the beginning of the desorption, the carbon dioxide-rich partial stream C contains most of the methane in a relatively high concentration of 5 to 10% by volume. Furthermore, the partial stream C also contains other accompanying substances contained in the biogas, which have been retained in the respective prefilters of the columns of the first methane-CO2 separation stage T12b or in the separation stage T12b themselves and are likewise desorbed during the desorption. The concentration of these accompanying substances, for example volatile fatty acids, aldehydes, ketones, silanes, alcohols etc., is closely related to the composition of the input substances and the digestion conditions in the T4 bioreactor. Even the digestion of, for example, orange peel, frying fat, animal fat, cosmetics etc. can lead to volatile high and low molecular weight, slightly to difficultly condensable trace substances in the biogas. The additional or sole digestion of such substances, especially in combination with a high space load of over 5 kg of organic dry matter per m ^{3 of} reactor volume and day, results in more accompanying substances in the biogas than the digestion of pure manure and pure energy plants. As desorption progresses, the methane content in the carbon dioxide-rich partial stream C and also the content of accompanying substances decrease, ie the purity of the carbon dioxide increases.

In a line connecting the two separation stages T12b and T12c, a branch 20 is provided, through which the carbon dioxide-rich partial stream C can optionally be returned to the downstream separation stage T12c, directly to the carbon dioxide store T13 or to an earlier process stage. The valves shown in the respective connecting lines are switched accordingly. In the connecting line between the separation stages T12b and T12c, a measuring device is arranged in front of the branch 20 , with which the residual content of methane in the carbon dioxide-rich partial stream C is determined.

At the beginning and in the initial course of the desorption, the residual methane content in the Partial stream C usually so large that the carbon dioxide-rich partial stream C into one or more of the earlier stages of the process. Accordingly, the two are Valves in the lines to the separation stage T12c and to the carbon dioxide storage T13 closed. The residual content decreases in the course of the desorption and evacuation phase Methane in partial flow C. If the value falls below a specified residual level, preferably 1 Vol.% Residual methane content, the valve is switched accordingly Partial stream C rich in carbon dioxide is fed to the second methane-CO2 separation stage T12c. In In this separation stage T12c, the carbon dioxide contained in partial stream C is concentrated. The stream with the concentrated carbon dioxide then becomes T12c Carbon dioxide storage T13 directed. Should the carbon dioxide purity in partial stream C already be so high that the partial stream C as carbon dioxide gas or, after liquefaction, as Liquid CO2 can be sold by switching the valves accordingly Partial stream C passed directly to the carbon dioxide storage T13.

If the carbon dioxide-rich partial stream C from the second methane-CO2 separation stage T12b is still highly loaded with methane and / or other trace substances, in particular at the beginning of the desorption, the valves in the lines to the separation stage T12c and to the carbon dioxide store T13 are closed, and it there is a return to an earlier process stage. Such a recirculation can also greatly reduce methane loss. Furthermore, any organic accompanying substances can be separated off, for example by anaerobic degradation or physically chemical reactions, in order to prevent their accumulation. Whether the concentration of an accompanying substance can be determined naturally depends on the design of the measuring device in front of the branch 20 . The presence and concentration of organic substances can alternatively be estimated on the basis of experience. Basically, this also applies to the residual methane content. A measurement of a residual concentration is therefore not absolutely necessary, but only advantageous. The recycling takes place in particular with high residual methane contents, preferably with residual methane contents of at least 1% by volume, since in such a case the methane extraction is also worthwhile. However, the recirculation also takes place if an accompanying substance with such a high content is contained in the partial stream C that sufficient enrichment of carbon dioxide in the downstream separation stage T12c is not possible or is not desirable.

If, for example, only a high residual methane content is determined, the partial flow becomes C preferably returned to the first methane-CO2 separation stage T12b. Becomes a specified content of another organic accompanying substance is exceeded, so takes place instead, preferably the return to an organic filter for filtering out such Accompanying substances. Is the organic filter upstream of the desulfurization stage T12a, like this Usually the case, the return takes place by admixing to the gas stream in line R8 from gas storage T8 for raw biogas. Especially in the event that the content of one or more other accompanying substances exceeds the predetermined value, is also preferably carried out instead or as a partial flow a return to one or more containers of the T4 bioreactor or to one or several fixed bed reactors T4c. The latter are preferably vertical Fixed bed reactors, in particular designed as packed columns. When returning to The partial flow C into the rotting liquid becomes a container of the bioreactor T4 blown in. Is a fixed bed reactor T4c or there are several fixed bed reactors T4c provided, so digested liquid from such a fixed bed reactor T4c Overflow of the bioreactor T4 fed via line R6. The partial stream C is divided into one Floor area of the fixed bed reactor T4c guided. The rising partial stream C trickles in the fixed bed reactor T4c or in the fixed bed reactors T4c the digested liquid from towards the top. Since the fixed bed reactor or the several fixed bed reactors T4c at very low space and digested sludge pollution works or work, the organic Accompanying substances in partial stream C are greatly reduced. The partial stream C cleaned in this way becomes the Gas storage T8 supplied.

If, as a result of digestion in the T4 bioreactor, the presence of accompanying substances in the biogas is likely, the raw biogas can also be used directly, either before or after  Gas storage T8 can be passed through such a fixed bed reactor T4c. One of R9 branching line R9a through which the biogas from the biogas reactor T4 in the same How the carbon dioxide-rich partial stream C is passed through the fixed bed reactor T4c.

For the purity of the carbon dioxide, it is particularly advantageous if after passing through the second methane-CO2 separation stage T12c and before being fed to the carbon dioxide storage T13 or a direct feed into a line network a further concentration preferably in the liquid state by distillation, stripping and / or activated carbon filter he follows.

Finally, it should also be pointed out that the gas separation device T12 described with reference to FIG. 10 and the separation process operated in connection with FIG. 10 can be used advantageously not only with a gas separation device operated in a PSA process, but also, for example, in connection with membrane process for gas separation.

The arrangement of a side shaft directly on a biogas reactor with the filling Reactor from the side shaft and with a preferred outflow of liquid from the reactor into the side shaft is in itself advantageous even without the invention. This also applies to the formation of one or more biogas storage facilities airtight storage and also for the desulphurization of biogas without air or Addition of oxygen. Also the introduction of biomethane made from a biogas and / or carbon dioxide in a fixed pipeline network can stand alone or in Combination with disclosed features can be used to advantage. These others Inventions are preferably used in combination with the claimed invention Commitment. You can advantageously but without the wired transport, at a another type of biogas production, production from other raw materials or without the separation described can be used. After all, there is also a silo with an inside Silo installed pipeline network for introducing CO2 into a bed to be ensiled alone usable for a silage.

Claims (21)

1. A method of transporting carbon dioxide, characterized in that the carbon dioxide is transported through a fixed pipeline network. 2. The method according to claim 1, characterized in that the carbon dioxide directly from a plant for the production of carbon dioxide to immediately a consumer is transported through the pipeline network. 3. The method according to any one of the preceding claims, characterized in that the content of carbon dioxide in a gas or liquid caused by the Pipeline network is transported, at least 40 vol%, preferably at least 99 vol%. 4. The method according to any one of the preceding claims, characterized in that carbon dioxide is used for the line transport, which comes from one or more of the following sources:

• - Carbon dioxide-containing by-product from the treatment of biogases,
• - Carbon dioxide-containing by-product from the treatment of landfill gases,
• - carbon dioxide in the preparation from wine production,
• - carbon dioxide from distilleries,
• - carbon dioxide from anaerobic fermentation,
• - carbon dioxide from a cold electrochemical combustion process,
• - carbon dioxide from a hot combustion process,
• - carbon dioxide from a mine gas,
• - carbon dioxide from air separation,
• - carbon dioxide from a fertilizer production,
• - carbon dioxide from the chemical industry,
• - Carbon dioxide from a mineral well.

5. The method according to any one of the preceding claims, characterized in that the carbon dioxide in the pipeline network at a temperature out of the range from 1 to 80 ° C, a relative humidity in the range from 0.01 to 80% and an overpressure in the range of 1 mbar to 70 bar compared to the atmospheric pressure is transported. 6. The method according to any one of the preceding claims, characterized in that the carbon dioxide from the pipeline network is supplied to one or more of the following uses:

• - for refrigeration,
• - in cold / freeze grinding processes for cooling and embrittlement,
• - for cleaning purposes,
• - for high pressure extraction.

7. The method according to any one of the preceding claims, characterized in that the carbon dioxide from the pipeline network for a coal refinement of preferably low-quality coal is used. 8. The method according to the preceding claim, characterized in that the Coal refinement via coal gasification with synthesis or water gas reaction and / or generator gas reaction is carried out. 9. The method according to any one of the preceding claims, characterized in that the carbon dioxide is used as a chemical raw material.   10. The method according to the preceding claim, characterized in that the Carbon dioxide for the production of a fertilizer, a cyclic carbonate from Methanol, salicylic acid, a polycarbonate, ethylene carbonate and / or Methylene carbonate is used. 11. The method according to any one of the preceding claims, characterized in that the carbon dioxide taken from the pipeline network into a bale or is injected between bales. 12. The method according to the preceding claim, characterized in that the or the bales are compressed and are preferably wrapped in film and textiles, fibers, waste, sorted waste fractions and / or perforated Lines included. 13. The method according to any one of the preceding claims, characterized in that the carbon dioxide for the operation of an aquaculture or aqua-algae culture is used. 14. The method according to the preceding claim, characterized in that the Carbon dioxide with culture water in a bypass in pipes, preferably are upright, is washed out. 15. Plant for the transport of carbon dioxide, characterized in that the device is formed by a fixed pipeline network. 16. Plant according to one of the preceding claims, characterized in that gaseous in some parts of the system and liquid in other parts Carbon dioxide located. 17. Plant according to one of the preceding claims, characterized in that Measuring sensors are installed, also for quantity measurements, that the measured values  be registered and forwarded and to regulate and control the transport serve. 18. Plant according to one of the preceding claims, characterized in that the system permanently installed compressors, storage tanks and intermediate storage for Has carbon dioxide. 19. Plant according to one of the preceding claims, characterized in that Liquid connection points of the system through built-in evaporator stations Carbon dioxide evaporates and gaseous through built-in compressor stations Carbon dioxide is liquefied. 20. Plant according to the preceding claim, characterized in that about Heat exchanger released cold for liquefaction and / or heat for Evaporation is used. 21. Plant according to one of the preceding claims, characterized in that the carbon dioxide with culture water from an aqua or aqua algae culture in the bypass in vertical pipes is washed out.