WO2018184612A1 - Method and system of facilities for energy conversion using carbon dioxide - Google Patents

Abstract

1. Disclosed are a method and a system of facilities for energy conversion using carbon dioxide. 2.1 In comparison with water, carbon dioxide has a lower thermal capacity. Nevertheless, in the critical energy density range of the carbon dioxide, the materials used must withstand a high pressure and temperature. As a result of its low critical point, carbon dioxide can still be used efficiently for the energy conversion of natural heat into work. 2.2 To achieve this, containers are filled with a large amount of CO2 which is heated by heat, e.g. climatic heat. This establishes the basis for the CO2 expansion in heat engines. Prior to the expansion process, the CO2 pressure fluctuations are smoothed and the CO2 fluids are heated further as they flow to the heat engines. After expansion, the fluids can be condensed by e.g. climatic cold. To obtain climatic cold or heat, local or temporal bridging by a CO2 transport facility or a CO2 storage facility is required. In addition to its storage function, the CO2 storage facility also has heating and cooling functions which are adapted to the output of the heat engines. This solves the problem of slower heat transfer of the heat exchangers in relation to faster operation of the heat engines. The CO2 processes in the containers of the CO2 storage facility, such as the heat transfer process, also do not run continuously but in batches. The CO2 circulation process in the CO2 heat engine facility is therefore a transient flow process. 2.3 The problems of climate change, energy shortages and optionally also desertification can thus be economically and efficiently solved.

Description

 Process and plant system for energy conversion by means of carbon dioxide

The invention relates to a method and a system for the energy conversion of heat in work with carbon dioxide as the working medium. Carbon dioxide can also be used for energy storage, especially near its triple point CO2 has a smaller volume per MWh compared to the compressed air in empty mines or

Pumped water in a store. This avoids the localization of the energy stored by compressed air or pumped water, and the partial load function for electric grids can be exploited almost anywhere with C02-stored energy. It is also known that the energy stored with CO2 can be utilized in a tank for mechanical energy conversion and at the same time for cooling in relation to the power / cooling coupling, in order to increase the efficiency of cooling. In addition, there are, of course, other possibilities for using CO2, and experience has shown that various CO2 deposition techniques are also available for obtaining CO2, for example the cryogenic method with cyclone stages, which can be used, for example, with Biogas can be fractionally liquefied, thereby separating CO2, CH4, water and other substances. In the present invention, a large amount of CO2 of high pressure and temperature is required to remove the C02 process guides such as e.g. the

Heat transfers in the individual containers of the C02 heat engine plant to be designed so that they do not take place continuously, but in a batch manner with some randomity for batch start and duration. The cycle thus formed in the CO2-Wäemekrafrmaschinenanlage is therefore rather a transient C02 flow process.

In comparison with the known state of the art, where the steady-state flow process is usually carried out continuously by means of working medium, the present invention normally operates transiently and batchwise in the C02 low-temperature range. Thus, common measuring devices, machines and materials can be used as needed for the invention. On the other hand, it is also known that intensive efforts are currently being made to find the cost-effective materials for the production of machines and equipment which can withstand high CO 2 pressure and simultaneously high CO 2 temperature. For example, construction of such a model for heat engines, in which carbon dioxide is high Energy density can relax. As you know, in the distance you are striving as you have since

Steam engine invention after constant efficiency improvements through careful machine design and optimized process control. Above all, only a limited amount of the CCh mass is used for the energy conversions. The present invention, however, partly in another direction, namely mass use of the

Carbon dioxide as a working medium and cost-effective use of the natural

Temperature gradient for heating and cooling of carbon dioxide for the

Energy conversion, through an integrative application of current techniques in a transient and batch-wise flow process of CCh fluids. Thus, a large amount of natural heat energy in work can be converted economically efficient. In this case, large-area sites for CCte storage or for CCh transport may be necessary, and the calculated enthalpy gradient of carbon dioxide for the heat engines compared to those of the water is generally also low. With the present invention, however, solving the problems of climate change and lack of energy, if necessary, one also combats the progressive desertification.

 For the detailed formulation of the invention, it is assumed in the following that the air temperature in winter is below minus 30 ° C and in summer over plus 30 ° C, as well as river water or other natural coolant has a maximum temperature of 20 ° C. Under this assumption, the present invention will be described, the working method of which may include four following operations.

 C02 collecting. C02-containing gas, such as purified flue gas from coal-fired power plants or other incinerators, contains some C02 mass fraction, for example 15%. To extract heat from the gas and to further clean it, the

Heat exchangers and sedimentation plants e.g. used in winter time. In addition to the condensed water and other condensates, it also produces a dried gas, in which the CO 2 content has risen to a desirable level.

C02 liquefaction. It is preferably winter cold air used to bring the temperature of the above-mentioned step 1) treated flue gas below minus 30 ° C. Then it is to be compressed by a gas compressor to the CO 2 partial pressure in the flue gas well over 15 bar increase. Thus, carbon dioxide will largely separate from the flue gas liquid. The deposited CO 2 liquid is first used for electricity generation and then sent to a CO 2 liquid tank of the plant system. Each such container should be completely filled with CO 2 liquid. The remainder of the flue gas remaining after CO 2 separation is also led to further use or treatment. Incidentally, it is important to mention that other CO 2 -containing fluids can also be used here as flue gas for CO 2 separation or liquefaction. And the process of CO 2 liquefaction in the heat engine plant will be described in detail in the following explanation of the drawing 7 and it may be combined with the CO 2 liquefaction present here.

 C02 -heat. Using warm summer air or by using waste heat or

Geothermal, solar heat and so other natural heat is heated in the containers fully bottled C02 liquid, the e.g. from the o.g. Step 2) can come out and possibly still be relocated before heating. By heating, their temperature rises above the level of 30 ° C, so that their pressure under the isochoric condition reaches a corresponding height of 700 bar or even higher. In addition, the temperature of C02 fluids can be further increased during their flow to the Wämekrafbnaschinen, for example by the heat from the solar thermal systems is used and possibly also the heat from combustion of C02 -neutral fuels in a combustion chamber.

C02 Energieumwandeln. The heated carbon dioxide with the high pressure from the above step 3) can be expanded in heat engines such as piston engines or turbines, for example, to generate the electricity. Before the C02 entry into the heat engines, the strong CO 2 pressure fluctuations are sufficiently smoothed. After the C02 exit from this, the expanded carbon dioxide using the cold from river water, cold air, or other natural coolants to liquefy again, and it may still be to compact. The liquefied carbon dioxide is then filled back into the C02 container. Thus, the process goes to the above-mentioned step 3), and an expanding CO 2 cycle can then be formed if necessary with the CO 2 mass flowing in, which can come continuously from the above-mentioned step 2). In each of four steps above, one tries only to exploit natural cold or heat, but this already indicates that the present invention is only conditionally applicable for achieving above-average economy, namely in the regions where there is a cold or winter or summer. There is a warm air temperature, as in North China or in Egypt. It would be best in one place cold in winter but also hot in summer.

Drawings: As follows, the invention will be further explained with seven drawings.

Explanation to the drawing 1: The first drawing serves the representation of the

System Overview. As the drawing shows, the plant system contains several of the following five components: heat exchanger plant, sedimentation plant, C02 liquefaction plant, C02 thermal energy plant and C02 fluid storage facility. The C02 fluid storage system, called C02 storage facility for short, can in turn consist of two units of the C02 gas storage facility and the C02 fluid storage facility

put together. In front of the heat exchanger is C02-containing gas, eg purified flue gas, which can come from sources such as coal-fired power plants. In order to cool this and to extract heat from it, the heat exchanger system is used, for example, in winter time. This results in cooled flue gas, which is alienated in the subsequent sedimentation by sedimentation and dried by further cooling, if necessary, it is still to filter through a dust filter. Thus, you get a dried and more purified flue gas, which is still largely cooled down and adequately compressed in the subsequent C02-Verfüssigungsanlage to separate carbon dioxide in the form of liquid from the flue gas. This separated CO 2 liquid can first be used to generate electricity and then be stored in the tanks of the CO 2 liquid storage system. The stored CO 2 liquid may need to be relocated in the future. In the coming summer time, it is then to be heated by the air heat, solar heat or other natural heat sources, or to heat them up at an earlier time by applicable heat sources such as waste heat, geothermal, combustion heat, etc., for example, the electricity by their relaxation in the Wämekrafmi machinery with generators to produce. This gaseous carbon dioxide can then be stored in the C02 gas storage facility and reliquefied with the help of cold air in the coming winter, or in an earlier time it is by its cooling with the cold from river water or similar natural coolants again convert into the liquid phase.

 It can easily be seen here that the useful temperature gradients of the air between summer and winter time are to be bridged by the C02 fluid storage system. This is called temporal bridging. Carbon dioxide is condensed and liquefied in winter time and heated and relaxed in summertime. In between, it can be stored in the C02 fluid storage system. In addition, there is still a local bridging between hot and cold places by means of a C02 transport system such as

Transmission pipelines or channels into consideration. This carbon dioxide is liquefied at a cold place and then transported to the warm place, where it is heated and then relaxed in the heat-Krafrniaschinen. After the relaxation, it is transported back to the cold place. In addition, this local bridging may be horizontal or vertical, for example, between the Arctic and the equator it is referred to as a horizontal bridging or between the foot and the summit of the Everest Mountains as a vertical bridging. Of course, the temporal and local

Bridging can also be done in a combined way. Last but not least is the utilization of the temperature gradient between air and river water in one place and in one day.

Explanation to the drawing 2: As is generally known, the flue gas from the

Coal power plants or other incinerators already cleaned and provided with a high temperature. Normally, it is released through a tall chimney into the air atmosphere, but now diverted to a heat exchanger of the plant. It flows in fact via the import of gas (1) in the metal line (5) of the heat exchanger. The pipe in a round or flat shape is placed inside a reinforced concrete tank from top to bottom, for example, in a spiral or rectilinear manner. Of the

Reinforced concrete container itself is partly on its outer wall, for example, with Thermal insulation material thermally insulated. In the line, the flue gas flows from the top down through the export of gas (2) from the plant out. The cold water flows from the top via the import of cold water (3) through a line in the bottom of the container, and then it flows along or cross the pipe outer surface from bottom to top, eventually overflows it as heating water on the export of heating water (4 ) out of the container. Within the line, the water condensed there also flows to the subsequent sedimentation plant. By the way, a heat exchanger system should consist of two such

Heat exchangers exist.

Explanation to drawing 3: Import of gas (6) is connected to the export shown in drawing 2 from the gas (2). The height of their position is lower than that of the export of gas (2), so that the condensates from the flue gas into a reinforced concrete tank the

Inlet the sedimentation system slightly. They are selectively extracted by the double valve (7) separately, that is, the condensed water with some foreign matter is discharged after the

Sedimentation derived to a water system, not shown in drawing 3, all solid sediments are also adequately treated after their removal via the double valve (7). The heat exchanger (10) serves here for the further cooling of the flue gas, e.g. using the winter cold air. As a result, it is largely dried and then flows through the check valve (9) on the export of gas (8) out to the subsequent C02 liquefaction plant. If necessary, it can also be installed by a yet to be installed

Gas fan can be fed out of the container, and in front of the check valve (9), if necessary, install a dust filter to filter large and light particles from the flue gas. Incidentally, a sedimentation plant should consist of two such reinforced concrete tanks.

Explanation to drawing 4: Here the CO2-liquefaction process is described on the basis of the dried flue gas from the sedimentation plant. Instead, it is also possible to use other CO 2 -containing gases in an analogous way to CO 2 liquefaction. The dried flue gas from the sedimentation plant is here at a pressure level of over 300 compressed by a multi-stage gas compression plant with

Intermediate cooling thanks to winter air cold. This can generate a lot of heat of compression above 100 ° C, which is dissipated in two heat streams A and B to the heat exchangers 1 and 2. After compression and cooling, the flue gas is at a thermodynamic state of over 300 bar and below -30 ° C, which is sufficient for CO 2 liquefaction. The compressed flue gas then flows further into a previously evacuated container, and there, with possibly further cooling it separates into two parts: C02 liquid and other, called as residual gas. The two parts are discharged separately from the container in each case by the CO 2 flow D and the residual gas flow C, their

Temperatures are then each raised via heat exchanger 1 or 2 to a height of about 100 ° C. The necessary heat comes just from the o.g. multistage

Gas compression plant or from the heating water or other usable heat obtained in the heat exchanger system. After that they will each have one or more

Heat engines with electric generators, e.g. Piston engine or turbine, relaxed to the lowest possible pressure. The CO 2 fluid is depressurized, for example, to a pressure of 15 bar and then passed into a container of the CO 2 liquid storage system and stored there. The residual gas is analogous, e.g. to relax it to 1 bar. The relaxed residual gas can then be released into the air atmosphere, or used for other uses, e.g. half of the cold created by relaxation and by the appropriate techniques, e.g. Linde method to separate the oxygen and nitrogen from the residual gas.

It is thus promising and desirable to realize a full use of the purified flue gas economically, with some important and new forms of substances may arise, for example, liquid carbon dioxide and heating water. For this purpose, however, electrical energy is spent, for example, for driving the gas compression systems. By using the compression and heating water heat but electric energy is also generated in large quantities, so that after balance nor a surplus of electrical energy can be reported. However, to do so will require the provision of a large volume of containers for storing the CO 2 liquid, which consequently represents a massive investment in their construction requests. However, she is involved in further electrical power generation

Heat recovery machines bring back by the relaxation of previously stored in the containers and still to be heated C02 liquid in the coming

Summer time, or in a previous time in a warm place or by exploiting the usable waste heat, geothermal and so on.

Explanation to the drawing 5: CO 2 liquid flows through the import for CO 2 liquid (11) through the check valve (13) into the previously evacuated container, which may be an externally insulated heat-insulated reinforced concrete container. It is, if necessary, pumped by pump (12), otherwise it flows through a not shown in the drawing switchable bypass next to the pump (12) to the check valve (13). The container can be internally equipped with a heat exchanger (16) for heat transfer to the outside and has an export for CO 2 liquid (14) with check valve (15), and has at least one Sicherheitsexit not shown in the drawing. It automatically lets C02 liquid flow out of the container if its pressure in the container exceeds a certain level, for example, 70 bar.

 There may be several such CO 2 liquid containers that can be connected to each other via valves and all of them together form the CO 2 liquid storage system. The heat exchanger (16) of such containers can be implemented with different levels of heat transfer performance. For example, the heat exchangers of those vessels require very high heat transfer performance, from which CO 2 fluid is delivered directly to CO 2 flow to the heat engines. The other heat exchangers can be provided with low heat transfer performance, especially if their heat transfer is for a long time, e.g. for several months from winter to summer.

Explanation to drawing 6: C02 gas flows via the import of C02 gas (17) through check valve (19) into the previously evacuated container, which is eg a heat-insulated reinforced concrete container on the outside and built in combination with C02 liquid containers can be. It is, if necessary, required by the fan (18), otherwise it flows via a not shown in the drawing switchable bypass next to the fan (18) to the check valve (19). The container may be equipped with a heat exchanger (22) for heat transfer to the outside and has an export of C02 gas (20) with check valve (21), and has at least one Sicherheitsexit not shown in the drawing. It automatically lets C02 gas flow out of the tank if its pressure in the tank exceeds a certain pressure level of, for example, 5 bar.

 There may be several such CO 2 gas tanks that can be connected to each other via valves and all of them together form the CO 2 gas storage facility. Of the

Heat exchanger (22), if installed, should have little heat transfer performance if its heat transfer takes place for a long time, e.g. for several months from

Summer to winter.

Explanation to the drawing 7: The

has a

Wärmelaafm Aschmengruppe, from the piston engines or turbines with

consists of electric generators. To the left and right of this is in each case connected to a heat exchanger to which an operating tank L or R is connected. Of the

Operating tank L or R links a container group of L 1, L2, ... Ln or Rl, R2, ..., Rm via their switches. The containers of the two groups of containers are each connected to the heat and cooling source systems also via their but other switches. Also connected are the two operating vessels L and R and the two connected to the heat exchanger with the heat and cooling source systems, but for clarity, the connecting lines and the corresponding switches are not shown in the drawing. All containers are e.g. thermally insulated with thermal insulation material from the outside, inside they are each equipped with heat exchangers for heat transfer to the outside. The service tanks are different from other vessels in that their heat transfer performance is higher and their strength is greater than the others.

As starting conditions of the plant it is assumed without restriction of generality: the right-sided containers are evacuated, but the left side filled with C02-fluid, the has a high pressure and a certain high temperature. These two

State variables of pressure and temperature are referred to below as operating pressure and operating temperature, respectively. The strained C02 fluid in the service tank L flows to the heat engines of the group via the left heat exchanger, where it is reheated. In the heat engines, it relaxes for energy conversion to a lower pressure with an associated lower temperature. These two quantities are referred to below as relaxation pressure or relaxation temperature. The expanded carbon dioxide is cooled to the right via the heat exchanger, and flows on to the right-side operating tank R.

 The containers LI, L2, ..., Ln will sequentially supply their C02 fluids to the service vessel L, during their delivery time the C02 fluids in the vessels are each heated via their own heat exchangers. This heating process is called as a process of heating to be filled or heated to relax (See claim 1). After each C02 delivery end, which is marked with a certain C02 pressure level in the container in question, the container in question is closed, and after its switching is switched its heat exchanger, namely locking the

Heat source and then release the source of cooling to cool the remaining carbon dioxide in the container. This cooling process ends when it reaches the temperature of a preselected coolant. And it is called a process or process of cooling for filling. (See claim 1). This process of cooling for filling occurs at certain intervals sooner or later for each left side container of LI, L2, Ln.

First, for the right-side containers, the right-side operating container R receives the expanded carbon dioxide with a cooling process through its heat exchanger. The cooled carbon dioxide then flows further into the tanks R1, R2, ..., Rm in succession or in parallel, where it is further cooled by them for its liquefaction via the respective heat exchanger. The necessary cold comes from the connected cooling sources. After the end of the C02 full filling in the respective container of Rl, R2, Rm by the flowing carbon dioxide from the operating tank R of the container in question is closed and after its closing its heat exchanger is switched, namely locking the Cooling source, and then releasing the heat source to heat carbon dioxide in the dedicated container isochorously to the initial left-side operating temperature, and thus the carbon dioxide will regain the initial 4-second operating pressure in the container. These operations occur for each right-side tank of Rl, R2, Rm. And so sooner or later all their C02 fluids reach the thermodynamic state when the system is started. In this case, the cooling process as a process or process of cooling to

Liquefied called (see claim 1), and the heating process or after the closing of the container as heating for pressure rise (see claim 1).

Subsequently or shortly before, CO 2 fluid then flows in the reverse direction, namely from the right side to the left side containers. The CO 2 delivery processes on the right then take place analogously to the previous delivery processes on the left. The left-side containers L, LI, L2, Ln still have residual carbon dioxide, which after cooling already has a lower pressure than the expansion pressure. Because of this, the processes of C02 fillings, cooling and heating take place analogously to the previous processes in the containers on the right. Sooner or later C02 fluids reach the thermodynamic state at the start of the plant.

In the drawing, the structure to the left and right of the Wännel Afteiaschinengruppe looks similar. In the process described above, the C02 flow direction alternates at certain intervals constantly left to right and vice versa. Likewise, the processes of C02 heating and cooling or C02 deliveries and fillings alternate in the mutual CO 2 containers, which accordingly have to change between two states of open and closed. In addition, these processes do not proceed continuously in the individual containers, but in a batch manner with some randomness for batch start and duration. Therefore, the C02 process is not a stationary flow process, but is a transient ping-pong flow process between the left and right sides of the thermal force group. In the following implementation example, this process will be described in detail with concrete numerical values. Furthermore, it should be noted that due to the flexible design of the heating, cooling and storage functions of the C02 container the problem of discrepancy of the slow heat transfer from heat exchangers over the fast operation of heat engines is resolved.

Implementation Example: In the present invention, the standard techniques and equipments are usually used integratingly.

 Heat engines: Piston engines or turbines with electric generators are used in different C02 operating pressure ranges with an upper limit of 700 bar and in the C02 temperature range between minus 70 ° C and plus 150 ° C. The upper limit of 700 bar is determined by the strength of the C02 containers, here C02 liquid can reach a much higher pressure than 700 bar when heated up to 150 ° C in a fully filled container, such as 2000 bar. Therefore, if necessary, it is possible to build an operating tank with harder materials, which can withstand, for example, a higher CO 2 pressure of 1327 bar and at the same time the CO 2 temperature of 80 ° C. The CO 2 depressurization pressure is based on the ambient temperature, e.g. River water temperature, or after the objective for the production of refrigeration or electricity. It is also affected by the ratio of C02 densities before and after CO 2 relaxation. The lower temperature limit after CO 2 expansion in heat engines, in addition to the influence of the CO 2 depressurization pressure, is limited by the CO 2 triple point temperature and the other factors such as the entropy height and the strength of the materials used. The upper limit of C02 temperature before C02 expansion in the

Heat engines are used in the temperature range between 20 and 150 degrees Celsius so that if possible no fossil fuels need to be used for CO 2 heating and at the same time still a large amount of natural heat energy can be converted into work economically efficient.

Gas compression systems for flue gas or C02 gas compressions usually operate in the pressure range with an upper limit of 400 bar or 20 bar, which does not challenge the current technological state of gas compression systems. In addition, if the processes of membrane gas separation (MGS) or pressure swing adsorption (PSA) or other processes are used before the compression of the flue gas to increase its CO 2 content, then the upper limit of 400 bar can be much reduced. Whether one of the Both methods or other methods used or not, depends solely on the consideration of the economy.

 Measuring instruments for pressure, temperature, mass flow, etc. are normal devices that do not usually require high precision, i.e. fault tolerance can well be in the range of tenths of units of bar, degrees, cubic meters per minute and so forth. lie.

Current heat transfer technology is considered technically mature for the applicable

Heat exchanger in the system. See the various company products and the corresponding textbooks mentioned in the literature of the invention description.

In the case of C02 long-distance transport, a reinforced concrete channel can be used for C02 gas transport, which has to withstand a pressure of up to 5 bar. Inside the canal, or directly next to it or elsewhere, a C02 fluid pipeline can be built to withstand C02 pressures up to 30 bar. These requirements for the C02 transport systems can be satisfied with current channel and tube technologies. See the corresponding listed specialist literature in the description.

The site selection for implementation is somewhat limited by the climatic conditions in that no C02 transport system is used between the hot and cold locations. A good location as an example is Haerbin City, the provincial capital of Helongjiang VR. China. There, the air temperature in winter reaches minus 35 ° C, and in summer it exceeds plus 30 ° C. In addition, it would be good if the construction sites of the plants could be close to C02 sources such as coal-fired power plants. However, if there is no suitable land near it, carbon dioxide can be separated from flue gas on-site and then transported through a CO 2 liquid pipeline to a remote CO 2 liquid storage facility. The C02 storage facility should be built where possible, where there is little, for example, in the deserts. Because the C02 storage facility requires large areas or volumes, the construction of such storage facilities, for example in the form of reinforced concrete tanks, can also combat the progressing desertification. In addition, the C02 storage facility can be built in modules, from small to large, to a system size that can meet the local energy needs, provided that there is a sufficiently large amount of C02 available stands. In the example of the city of Haerbin, one can now expect a newly available quantity of C02 of approximately 2.58 million tons per year. This requires about 3.30 million cubic meters of the total volume of reinforced concrete tanks for storing C02 fluid, which has a density of 782.6 kilograms per cubic meter. With 17500 cubic meters per container you have to build 189 containers. For safety reasons, 380 pieces of such containers are built, so in drawing 7, 190 containers are designed respectively for the left and right sides of the heat engine group: 1 operating container and 189 other containers. It also sets an average C02 mass flow of 2000 kilograms per second for the domestic group, so 2.58 million tonnes of C02 mass sufficient for about 10 days, while the duration of the C02 mass flow from one to the other side of the heat-generating group flows before it changes the direction of flow.

In terms of cost-effectiveness, the investment for this system size is still low. For explanation, it is assumed that the city of Haerbin needs as an example about a total electric power of 2 GW from coal power plants for civilian use. There they consume about 6.41 million tonnes of standard coal per year, producing about 20.61 million tonnes of carbon dioxide. With a C02 deposition rate of 75% from the flue gas, approximately 1.46 million tonnes of pure carbon dioxide could be produced each year, but within two months of winter, with the air temperature below minus 30 ° C, only 2.58 million tonnes could be liquefied there. After CO 2 liquefaction, the city of Haerbin must route the C02 fluid to a remote and low-level C02 fluid storage facility. So for the plant system there is a total investment of about 900 million yuan Renminbi excluding the two costs for the land and the construction of C02 transmission lines. The biggest part of the cost here is the construction of C02 storage facility, which contains 380 pieces of the above mentioned containers. In summertime, in addition to hot air, solar thermal systems and salt storages for heat storage can also be used for C02 heating, possibly also a combustion chamber for combustion of CO 2 -neutral fuels in other times, with a C02 operating temperature of 80 ° C before entry to reach the heat engines. The relaxation pressure is around 60 bar and depends on the Ambient temperature, eg of river water at 20 ° C. For the heat transformations of heat, it is assumed that the efficiency of the heat engines is 70%, with the CO 2 enthalpy difference between before and after CO 2 expansion there being an average value of 21 kJ / kg. Under more favorable conditions, a higher value of approximately 118 kJ / kg can be achieved. However, the electricity quantity calculation is carried out below with the value of 21 kJ / kg, and thus obtains an electrical power of about 28 MW. It follows: a) production of electricity of 244 million kWh in the first year of production; b) generation of cold in summer. Currently in China, the eco-electricity has a price of about 0.5 Yuan Renminbi per kWh. The generated electricity alone will then have a value of 122 million Yuan Renminbi, which is economically very efficient compared to the estimated investment of 900 million Yuan Renminbi.

As follows, the operation process for the C02 heat engine plant will be described in detail with reference to the drawing 7 with city Haerbin as an example. First, without loss of generality, the following starting conditions were assumed: The right-hand containers of Figure 7 were evacuated and the left-hand but filled with C02 fluid, its thermodynamic state 342 bar and 80 ° C, from which its density follows 782.6 kilograms per cubic meter ; the coolant is river water whose temperature does not exceed 20 ° C; the total heat transfer capacity of all the heat exchangers from the plant would be equivalent to 28 MW of electrical power, requiring approximately 215 MW of heat transfer capacity for CO 2 heating and 270 MW for CO 2 cooling. When assuming here is to mention that the pressure level of 342 bar for a

Reinforced concrete tank is very high. And in the following 9 comments, especially the 4th note explains how to reduce this pressure level without reducing the electrical power.

At the beginning of the process, the strained C02 fluid flows from the left operating tank L via the left heat exchanger, where it is reheated, and then on to the heat engines of the group, where it relaxes to a pressure of 60 bar. The expanded CO 2 fluid is cooled via the right heat exchanger, and then flows into the right operating tank R. During the CO 2 delivery period from the operating tank L, carbon dioxide in the L will receive the heat via its heat exchanger from the heat source plant so that the C02 temperature in the L can rise above the level of 80 ° C. At the same time as the C02 outflow from L, the C02 operating pressure drops there. With the sinking to near 70 bar C02 fluid is then supplied to him from the container LI. During the C02 delivery time from tank LI, carbon dioxide in the LI will receive the heat through its heat exchanger from the heat source plant to keep CO 2 temperature there as high as possible at 80 ° C. With the CO 2 pressure sinking to near 70 bar in tank LI, LI is closed and shortly before tank L2 begins to supply C02 fluid to holding tank L, carbon dioxide in L2 being heat-exchanged from its heat source plant to CO 2. Temperature there as possible to 80 ° C to hold. With the C02 pressure sinking to close to 70 bar in L2, L2 is also closed. This CO 2 delivery process through the left-side containers is repeated until carbon dioxide in the last container Ln reaches the pressure of 70 bar. In addition, a left side C02 cooling process starts in each case in the containers LI, L2, ..., Ln successively or in parallel, as soon as they are each closed and then the respective heat exchangers are switched from heating to cooling. The C02 cooling process in each left side tank ends when the residual carbon dioxide there reaches the coolant temperature, eg 20 ° C. The cold comes here via the respective heat exchanger of the container from the cold source system.

Above the link-side process is described, now the right-sided process is shown. The service tank R receives the expanded C02 fluid through a cooling process using its heat exchanger. Subsequently, the cooled CO 2 fluid flows to the container R 1, which begins to receive it also by a cooling process with the aid of its heat exchanger. When carbon dioxide in the Rl reaches the depressurizing pressure of 60 bar due to C02 filling of R, Rl is automatically closed with a check valve for Rl not shown in the drawing, and thus, at the same time or just before, it begins to fill R2 with carbon dioxide from R. And so continuing, it runs to the last right-side tank Rm. During the time of CO2 filling in the tank R2 or another right-sided tank in the group with number greater than 2, carbon dioxide in the Rl passes through its heat exchanger cooled further until it reaches the temperature of the coolant of 20 ° C. It also applies that whenever C02 pressure in Rl is slightly lower than 60 bar, Rl is automatically topped up with carbon dioxide from R until carbon dioxide reaches the depressurization pressure of 60 bar. This Rl replenishment is repeated in certain periods of time until carbon dioxide in it has a stable thermodynamic state of 60 bar and 20 ° C. This results in a CO 2 density of 782.6 kilograms per cubic meter in Rl. Then Rl is closed and then its heat exchanger is switched from cooling to heating. It then begins to heat carbon dioxide in RI isochorically via its heat exchanger until carbon dioxide reaches the operating temperature of 80 ° C there. This results in a CO 2 pressure of 342 bar in the Rl. These cooling, filling and heating operations for carbon dioxide in RI are repeated in the analogous manner for each other tank of the right-side tank group successively or in parallel. As a stretched C02 fluid in the last left-side container Ln reaches the pressure 70 bar, ie all strained left side C02 fluids for the CO 2 relaxation in the

Heat engines have been expended, carbon dioxide in the last right-side container Rm or a previous container in the right-side container group is already on the stable thermodynamic state of 342 bar and 80 ° C. Now, the entire process will reverse in its CO 2 flow direction, from the right side to the left side CO 2 containers. The C02 delivery processes on the right are then analogous to the previous C02 delivery processes, the stressed C02 fluid now flows from the service tank R via the right side heat exchanger, where it is reheated, and then on to the heat engines of the group where it relaxes to 60 bar. The relaxed carbon dioxide then cools on the left side

Heat exchanger from, and then flows readily into the operating tank L, because the residual carbon dioxide in the left-side containers after previous cooling already on the thermodynamic state of 20 ° C and the density 134.1 kilograms per

Cubic meter, which means that the CO 2 pressure there is about 48 bar, it is less than the expansion pressure 60 bar. Therefore, the previous right side CO 2 processes are now repeated in the left side group containers, namely, fill, cool, heat and so on. Thus, CO 2 fluids there are the thermodynamic state of 80 ° C and 342 at certain intervals sooner or later.

 So the C02 delivery process is first from left to right and then from right to left, and now it starts again from left to right. So, in this cycle, a ping-pong flow process between the two sides of the family of cremation groups is going on continuously. However, one will ask oneself a question, whether the heat engines would interrupt their course in between, because the reversal process in the two

Operating containers L and R between supply and receive or heating and cooling could not be completed so quickly. An answer for that will be in subsequent ones

To find annotations, for the time being it can be imagined that an operating tank consists of two sub-tanks, one for heating and delivery, another for cooling and receiving. The analogous applies to the heat engine group and the two heat exchangers next to it.

Remarks:

 1) For a better understanding of the structure of the C02-Wäimekrafbnaschinenanlage is drawn almost symmetrical. However, it is sufficient to set up a control program for the plant, which is based on the states of their containers or heat exchangers with the corresponding CO 2 processes or heat transfer modes. They are to or open, and the C02 operations are heating, cooling, holding, delivering, refilling, refilling, shutting and opening for the containers, as well as the

 Heat transfer modes On, off and switching of heat or

Refrigeration source systems for the heat exchangers. All containers L, LI, L2, ..., Ln and R, Rl, R2, ..., Rm are then under the same control and control of the program. Thus, in each case an operating container fixed for C02 deliveries or C02-receiving be recognized, and analogously, this applies to the two heat exchangers next to them for C02 cooling or C02 heating. On the whole, a heat exchanger fixedly attached to CO 2 cooling can also be combined with the receiving operating tank. In addition, this may cause a container, except for the service vessels, to be stopped during its CO 2 delivery process from supplying it with further CO 2 fluids for the CO 2 delivering service vessel, if its heat exchanger is the CO 2 supply Heat to maintain certain C02 temperature level in it, eg 80 ° C in

 Implementation example, can not deliver on time. In this case, CO 2 fluid is instead supplied from another CO 2 container with appropriate CO 2 temperature and C02 pressure for the CO 2 delivering operation vessel, in the

 Implementation example means that C02 temperature there is higher or equal to 80 ° C and at the same time CO 2 pressure higher than 70 bar. As a result, a single CO 2 tank need not necessarily have sufficient heat transfer capacity for CO 2 heating and CO 2 cooling in the tank except for the service tanks. However, it is important to note that the entire

 Heat transfer capacity of the plant for C02 heating and CO 2 cooling just the rated electrical power must comply. In the example of the city of Haerbin, the electric power of 28 MW, accordingly, the total heating and cooling capacities are also as stated above. Therefore, due to this control and

 Control functions of the program, regardless of how it is implemented and in particular with which programming language and with what hardware, the said number of containers of 380 pieces with the given volume in the implementation example can be much smaller, and thus the sink

 appropriate investments. Incidentally, it is clear from the above-mentioned achievements that the overall efficiency of this system with regard to the heating power or the total heat transfer capacity is approximately 13% or 6%. This efficiency is similar to that of ORC systems in the low temperature range.

) The implementation example of the city of Haerbin has, as stated above, a C02 mass amount which is sufficient for a 10-day single-sided CO 2 delivery for relaxation in the heat treatment machines. One can shorten this duration somewhat, for example to 5 days, doubling the C02 mass flow to 4000 kilograms per second. As a result, there is approximately a loss of electric power, provided, however, that the heat transfer capacity and the electrical capacity of the equipment are also increased accordingly. All shortest duration would be 24 hours, then usually there is at least one early morning with the lowest ambient temperature in one day for the purpose of CO2 cooling. Here is the memory function of

 Recognizable containers, which results in a temporal bridging, namely a time shift thereby realized for the purpose of CO 2 cooling from the CO 2 reception time in the operating vessel at a later time in another C02 container, such. here the coming early morning. One can realize such time shifts for CO 2 cooling not only by one or more days, but also by several months, for example between summer and winter time. If this time difference is actually achieved by bridging the time between summer and winter, then the C02 depressurization pressure can be set much lower than 60 bar in the example to produce more electricity but also to produce more cold in summer. However, you also have to build more C02 storage capacity. On the other hand, while maintaining the electrical power level of 28 MW in the example can be significantly reduced by reducing the duration of the C02 storage capacity, ie here the number of containers 380 with said volume. As a result, the investment sum of 900 million Yuan Renminbi for the plant system can be drastically reduced.

Analogous to the temporal bridging between the high and low temperatures in the different times, a local bridging of the temperature difference between hot and cold places can be achieved by a C02 transport system such as e.g.

 Transmission pipelines or channels can be realized. Thus, more takes place

 Generating electricity by substituting the CO 2 depressurization pressure for the

 Heat engines or by increasing the operating temperature for it. But you have to cope with the construction costs for the C02 transport system. And, of course, it is of course also possible to use the temporal bridging combined here.

) If the required heat transfer capacity is concentrated on a few C02 containers, then all other containers, with the exception of the operating containers, no longer need to install heat exchangers in them, they therefore have mainly one

Storage function and a possible outside heat insulation. Your Strength requirement can therefore be significantly reduced, for example, to reduce CO 2 pressure in it to 70 bar or 1 bar for CO 2 liquid container or CO 2 gas container. Thus, the construction and operating costs of C02 containers can be reduced even further.) If the objective is refrigeration rather than electricity generation, so taking into account the entropy heights of the relaxation pressure for some

 WärmelaaftmascWnen be reduced in the group about 1 bar. This creates in the relaxed CO 2 gas, the cold, which is targeted to dissipate. After

 Cold transfer, the C02 gas is either stored and later liquefied, or adequately compressed by a driven with the generated electricity gas compressor and at the same time with the cold from river water or similar natural coolants again converted into the liquid phase. The resulting

 Compaction heat can be reused for CO 2 heating for electricity generation.

If it were to use excess electricity from the power grid at night, reduce as much as possible during the day the CO 2 expansion pressure for the heat engines, taking into account the corresponding entropy heights, to generate more electricity as well as more cold. The gas expanded carbon dioxide is then at night by a gas driven with said surplus electricity gas compressor to compress and at the same time liquefy through its cooling, with the help of the previously produced during the day cold and / or cold from river water, cold air or other natural coolants. The next day, the liquefied carbon dioxide will be available again for electricity generation, whereby the heat of compression that occurred earlier in the night can also be used for CO2 heating. The efficiency of this whole process is remarkably high, especially as the part-load functions of the C02-powered thermal machines in the

 Compared to steam power plants are much more flexible.

) If the operating pressures, for example between 342 and 70 bar, are to be homogenized in the implementation example, ie to smooth the operating pressure fluctuations between them, then for the different CO 2 streams with different CO 2 pressure levels before the CO 2 Entering the Waste Machine Group to set up a C02 mixing apparatus consisting mainly of nozzles and diffusers. Or another method for this should be to first adequately divide a large operating pressure range into a plurality of smaller operating pressure ranges, and then use different thermal power machines for these different smaller operating pressure ranges accordingly. Of course it is also possible to use these two methods combined. However, a very different possible method is the use of a backpressure turbine with multi-pressure flows, if the C02 density before the C02 entry into the

 Heat engines in a suitable subcritical area, e.g. less than 60 bar and higher than 80 ° C.

The operating temperature of 80 ° C assumed in the implementation example results in that heat of the lower temperature for heating C02 can be used as the first heating stage. For example, the hot ambient air in summer heats carbon dioxide to 30 ° C or even higher. Is however the

 Operating temperature 80 ° C unattainable, then is with a lower

 Enthalpy gradient and consequent smaller electrical power to be expected if the relaxation temperature can not be reduced accordingly. But if the relaxation temperature is also lowered, it will, despite the lower

 Operating temperature even possible to increase the enthalpy gradient. For example, for the operating temperature 30 ° C and the coolant temperature minus 30 ° C, which at the beginning of the formulation of the present invention just assumed

 Air temperature in summer or winter, a corresponding

 Enthalpy gradient of about 36 kJ / kg can be achieved. This is much higher than 21 kJ / kg in the example, but it would have to accomplish a temporal or local bridging between plus 30 ° C and minus 30 ° C. In addition, one should use the heat from solar thermal systems, it is sufficient to achieve the

Operating temperature 80 ° C in any case in the summer time. In addition, the C02 temperature of 80 ° C is easily surpassed by the transfer of heat resulting from the combustion of CO 2 -neutral fuels such as lumber and straw. If your combustion flue gas is also collected as it is from coal-fired power plants, then this type of combustion can even reduce the C02 greenhouse effect.

 9) Are the enthalpy slopes, e.g. 21 kJ / kg in the implementation example, too low for the drive of the heat engines, then the tensioned C02 mass can only be taken from the specific upper part of the usable operating pressure range. In the implementation example, if the strained carbon dioxide was only used from the interval [100, 342] bar instead of [70, 342] bar, the enthalpy gradient can be increased by about 10%. Also with a higher upper limit of operating pressure than 342 bar, e.g. 700 bar, a higher enthalpy gradient can also be achieved. However, in each case more C02 mass or firmer operating container etc. must be provided for the two options.

 Based on the implementation example of the city of Haerbin can be eight with the o.g. 9 comments various extensions and modifications. If you increase, for example, the operating temperature of 80 ° C to 100 ° C, the enthalpy gradient of 21 kJ / kg in the example rises to about 42 kJ / kg. Similarly, it rises to about 35 kJ / kg when the

Coolant temperature as the river water temperature has a height of 5 ° C instead of the assumed in the example height of 20 ° C. Accordingly, there is a tremendous potential here to increase the enthalpy gradient to about 118 kJ / kg, if the operating temperature can be changed to 150 ° C and the coolant temperature to minus 30 ° C. However, this change is achievable by temporal or local bridging. For example, if one is able to raise the funds for building a large C02 gas storage facility, then a time shift from summer to winter can be realized by bridging the time. This generates much more electricity and more

Intermediate superheaters can reach the total enthalpy gradient even hundreds of kJ kg. Similarly, such a tremendous increase in the enthalpy gradient is also achieved by a local bridging using a C02 transport system such as

Transmission pipelines or channels. This really depends on the particular concrete situation, for which careful planning and optimization is necessary in order to achieve the highest possible level

To achieve profitability. Thus, one uses C02 for energy conversion economically highly efficient and solves the problems of climate change and lack of energy, and if necessary combats the progressing desertification.

LIST OF REFERENCE NUMBERS

patents

 Patent publication date applicant title

 DE 102009057613A1 16.06.2011 Kipp, Jens- Werner Power / Cold Coupling for

 energy

EP 0 277 777 B1 10.08.1988 Crawford, John T .; Power plant with C02 as

 Lewis, Oak Brook; Arbeitsfluidum

 Fischer, Harry C;

 Coers, Donald H.

 EP 2 277 614 AI 26.01.2017 LO Solutions Process for cleaning

 GmbH / Hermeling, and liquefying of

Werner biogas literature

 1st Thermodynamics, 6th edition, Springer Verlag 2007, Klaus Lucas

 2. Thermodynamics, 15th edition, Springer Vieweg 2012, Baehr and Kabelac

 3rd Thermodynamics, Vol. 1, 19th Edition, Springer Vieweg Verlag 2013, Peter Stephan,

 Karl Heiz scraper, Karl Stephan, Franz Mayinger

 4th Technical Thermodynamics, 2nd edition, Springer Vieweg Verlag 2015, Peter von Böckh and Matthias Stripf

 5. Thermodynamics, 2nd edition, publisher DE Gruyter 2016, Rainer Müller

 6. Thermodynamics for mechanical engineers, 5th edition, Springer Vieweg 2015, Wolfgang

 Geller

 7th VDI Heat Atlas, 11th edition, Springer Vieweg Verlag 2013

 8th heat exchanger, 5th edition, Verlag Vogel Business Media 2015, Walter Wagner

9. Fundamental Equations of State, Shaker Verlag 1998, Reiner Tillner-Roth

 10. Multiparameter Equations of State, Springer Verlag 2000, Roland Span

 11. Fundamentals of Pneumatics, 3rd edition, Verlag Hanser 2012, Horst- W. Grollius

 12. Taschenbuch der Kältetechnik, 19th edition, publisher C.F. Müller Heidelberg 2008, Walther Pohlmann

 13th turbomachinery, 5th edition, Verlag Hanser 2013, Herbert Sigloch

 14. Solid construction, 5th edition, Springer Vieweg 2015, Peter Bindseil

 15. Reinforced concrete construction, 9th edition, Springer Vieweg 2013, Stefan Baar, Karsten Ebeling, Gottfried CO. Lohmeyer

 16. Thermo-economic evaluation of the Organic Rankine Cycles in the generation of electricity from industrial waste heat, Verlag Berlin 2014, Thermodynamics Energy-Environment Technology, Volume 25, Markus Preißinger

 17. CCS technology, Springer Vieweg 2015, ed. Manfred Fischedick, Klaus Görner, Margit Thomeczek

18. Can carbon dioxide replace steam to generate power? Scientific American ™, By Umair Irfan, Climate Wire, on March 3, 2015

Analysis of the development stages of the carbonate looping process for CO 2 deposition, Verlag Cuvillier Göttingen 2014, Johannes Kremer

Gas2energy.net, 1st edition, Deutscher Industrieverlag GmbH 2015, Jens Mischner, Hans-Georg Fasold, Jürgen Heymer, Volker Trenkle

The Gas Engineers Dictionary, Deutscher Industrieverlag GmbH 2013, Klaus Hofmann, Rainer Reimert, Bernhard Klocke

Claims

claims

 1. A process for energy conversion by means of carbon dioxide as a working medium for the heat engines, characterized in that the plant system contains the following five plants:

 1.1 a heat exchanger system with the following features,

 1.1.1. At least one container with a volume of at least 27 cubic meters and

1.1.2 is partially or completely thermally insulated on its outer wall, and

 1.1.3 is placed in the at least one metal line (5) from top to bottom, within which the fluids flow via an import of gas (1) from top to bottom, and

1.1.4 in the lower wall area there is an export of gas (2) from which e.g. the flue gas flows through the metal pipe, and

 1.1.5 in the lower part of an input is present, through which the cold water flows into the container, from the top via an import of cold water (3) through a water pipe, which is connected to the entrance, and

 1.1.6 at its upper wall region an export of heating water (4) exists, from which the cold water flowing into the container after the heat transfer over the surface of the metal pipe (5) overflows as heating water;

 1.2 a sedimentation plant with the following features,

 1.2.1 at least one container with a volume of at least 27 cubic meters and

1.2.2 has a sloping bottom for collecting sediments from C02-containing fluids, and

 1.2.3 there is an import of gas (6) in its wall area, and

 1.2.4 a double valve (7) exists in its lowest floor area for the extraction of sediments from C02-containing fluids, and

 1.2.5 on the wall of an outlet for the removal of condensed water from the C02-containing fluids is present, and

 1.2.6 in the upper interior, a heat exchanger (10) may be installed for cooling of C02-containing gas, and

1.2.7 at the upper part of which there is an export of gas (8) for gas discharge and a Block valve (9) exist, and

an optional fan and / or optional dust filter can be installed when exporting gas (8);

a C02 liquefaction plant with the following features,

at least one gas compression plant with an optional switchable bypass, and at least one tank for receiving compressed C02-containing fluid, such as e.g. Flue gas from the gas compression plant, and

a group of heat exchangers for transferring heat such as

Compressive heat from the gas compression unit or other usable heat to heat the carbon dioxide, e.g. are deposited from the C02-containing gas, and / or to heat the existing residual C02-containing gas after CO 2 deposition, and

a group of heat engines for the relaxation of C02 fluids, and / or for the relaxation of the existing residual CO 2 -containing gas after CO 2 deposition, and

a container for receiving the CO 2 fluids which have been expanded in heat engines, and

an optional vessel for receiving the existing expanded residual CO 2 -containing gas after CO 2 separation, and

a group of CO 2 liquid containers for storing the CO 2 fluids, wherein the CO 2 liquid containers can be equipped with heat exchangers if necessary, and

an optional group of containers for receiving the existing expanded residual CO 2 -containing gas after CO 2 separation, which containers may be provided with any required heat exchangers;

a C02 fluid storage system with one or two of the following two subsystems, a C02 fluid storage system having the following features,

a group of containers that can be connected by valves, and each container in the group has: an inlet for CO 2 liquid (11) with an optional shut-off valve (13) and an optional pump (12), and a bypass correlated with the pump (12), and an export for CO 2 liquid (14) with an optional shut-off valve (12). 15), and at least one security exit, and

possibly one, several or no heat exchanger (16) in the interior, and partially or completely thermally isolate the outer wall, and

to withstand at least the pressure of 20 bar;

a C02 gas storage facility with the following features,

a group of containers, which can be connected to each other via valves, and each container of the group has:

an import of C02 gas (17) with a check valve (19) and an optional fan (18), and a correlated with the fan (18) bypass, and an export of C02 gas (20) with an optional check valve (21 ), and at least one security exit, and

one or more or no heat exchanger (22) in the interior, and partially or completely or no heat insulation on the outer wall, and to withstand at least the pressure of 1.2 bar;

a C02 wool kiln plant with the following features,

a group of heat engines with electric generators, and

a heat source system, which can supply heat to all heat exchangers of the C02-Wärmelaaftmaschinenanlage, and

a refrigeration source system, which can supply cold to all heat exchangers of the C02 heat engine plant, and

at least two service containers each for delivering and receiving the CO 2 fluids to and from the heat treatment machines, wherein the operation containers are equipped with heat exchangers, which are in turn connected to the heat and / or refrigeration source systems via switches, and

one or more, or no, heat exchangers installed directly after the supplying service vessel and with the heat and / or cold source facilities over Switch is connected, and

one or more, or no, heat exchangers installed directly in front of the receiving service vessel and connected to the heat and / or refrigeration source systems via switches, and

a group of CO 2 containers for delivering and / or receiving CO 2 fluids, wherein the CO 2 containers can be equipped with or without heat exchangers, which in turn are each connected to the heat and / or refrigeration source systems via switches;

 where

that a large amount, i. from 5000 tons of mass carbon dioxide, is used as a working medium, and

that for C02 heating, the climatic heat and / or waste heat and / or geothermal, solar heat or other natural heat and / or heat from the combustion of CO2-neutral fuels are used, and

that for C02 cooling the climatic cold and / or other natural cold

River water, deep soil, deep seawater and / or other natural coolants and / or the possibly generated expansion cold are used in the heat engines,

that the use of climatic heat or climate cold as described in 1.11 and 1.12, respectively, is accomplished in one of three ways: on-site, using a C02 transport system or using a C02 storage facility,

that the process of CO 2 heating is carried out batchwise in some CO 2 containers, that the process of CO 2 cooling is carried out batchwise in some CO 2 containers, that the process of CO 2 feeds into some CO 2 containers is carried out in batches, that the process of CO 2 Supplied from some C02 containers batchwise that is formed in several of four subsequent process steps, a C02 cycle in the C02 heat engine plant in which the C02 mass

may also increase:

CO 2 collection, whereby the cold, in particular the natural cold, cools the CO 2 containing fluids is used,

 .2 C02 liquefaction, where the process of cooling for filling and the process of cooling for liquefaction take place in parallel and / or successively in some C02 containers,

 .3 CO 2 heating, where the process of heating to fill, the process of cooling to fill and the process of heating to pressure rise parallel and / or successively in some C02 containers,

 .4 C02 energy conversion, where the process of heating to relax during C02 flow to the weir engines, and the C02 pressure fluctuations may be smoothed.

 2. A method for energy conversion by means of carbon dioxide, which is contained in the flue gas from coal power plants or other incinerators, and according to claim 1, characterized in that

 2.1 that C02-containing fluid such as flue gas is dried and purified by the use of the heat exchanger system or sedimentation systems described in point 1.1 or 1.2 and with the help of the climatic cold and / or other natural cold, and thus the CO 2 proportion in the fluid is increased,

 2.2 that the climatic cold and / or other natural cold and / or usable

 Expansion refrigeration of gases used for cooling and / or for intermediate cooling in the gas compression,

 2.3 that the heat from fluids obtained in processes 2.1 and / or 2.2 can be used to generate electrical energy,

2.4 that prior to the compression of gas in the C02 liquefaction plant, a process of PSA (pressure swing adsorption) or MGS (membrane gas separation) or other process for increasing the CO 2 content in the gas or none is used.

3. A method of energy conversion by means of carbon dioxide according to claims 1 and 2, characterized in that several of the following three types of energy,

 3.1 the heat from flue gas or other waste heat,

3.2 the heat of compression from the gas compression plants,

3.3 the pressure energy required in C02 deposition in the C02 liquefaction plant, for which electrical energy is generated by the Wännelaaftmaschinen, the associated expansion cooling during expansion into the

 Heat engines

 3.4 for the cooling of the gases to be compressed, and / or

 3.5 for the intercooling of gas compression plants, and / or

 3.6 for the recovery of the pure substances such as oxygen and nitrogen from the residual gas remaining after the CO 2 separation, such as e.g. from the flue gas, and / or

3.7 for room air conditioning and other cooling purposes and / or

 3.8 for nothing, e.g. in an extremely cold winter

 can be used.

 4. A method for energy conversion by means of carbon dioxide, wherein the C02 properties are to exploit voltage and mass density to generate CO 2 high pressure, and according to claim 1, characterized

 4.1 that some C02 containers are filled with C02 fluids and

 4.2 that they are closed after full completion, and

 4.3 that the C02 fluids enclosed in the receptacles may be opened and relocated to other C02 receptacles and reclosed, and

 4.4 that the closed C02 fluids are heated isochoric, preferably by waste heat or climatic heat, solar heat, geothermal or other

 Natural heat, and possibly by heat from the combustion of CO 2 -neutral fuels, and, if necessary, by heat from the combustion of fossil fuels.

 5. A method for energy conversion by means of carbon dioxide according to one of

 Claims 1 to 4, characterized

 5.1 that some C02 tanks are equipped with heat exchangers,

 5.2 that the processes of C02 heating or cooling in heat exchangers

equipped C02 containers take place in batches and they can run in parallel and / or in succession,

5.3 that the processes of CO 2 -filling into the CO 2 containers or of CO 2 -deliveries from them take place in batches and they can run parallel and / or consecutively,

 5.4 that the CO 2 flow process in the C02 heat engine plant by a

 Control program for the condition and process management of C02 fluids in some vessels and some heat exchangers of the C02 heat engine plant is controlled and controlled,

 5.5 that the total heating and cooling capacities of the C02 tanks are matched to the total electrical power of the heat engines in the system.

 6. Method for energy conversion by means of carbon dioxide according to several of

 Claims 1 to 5, characterized

 6.1 that the CO 2 pressure fluctuations before CO 2 relaxation in the

 Heat engines may be smoothed, and

 6.2 that the C02 fluids are heated during their inflow to the heat engines, and

 6.3 that after CO 2 relaxation in heat engines, the expanded CO 2 fluids from the cold climate and / or by using the cold out

 River water or other natural cold and / or available cold such as e.g. C02 expansion refrigeration be liquefied, and

 6.4 that the expanded C02 fluids according to 6.3 may still have to be compressed.

7. A method for energy conversion by means of carbon dioxide according to one of

 Claims 1 to 6, characterized

 7.1 that the fluctuation range from the C02 operating pressure before the C02 entry into the

 Heat engines is reduced by combined use of nozzles and Dusstusoren for the CO 2 streams if necessary, and / or

 7.2 that different heat engines for the different and before

Operating pressure to be used before the CÜ2 entry into the heat engines

7.3 that the two methods in points 7.1 and 7.2 are used in combination can, and / or

 7.4 that the backpressure turbines with multi-pressure flows are to be used as required, if the CO 2 density before the C02 entry into the heat engines in a

 subcritical area lies.

 8. Method for energy conversion by means of carbon dioxide according to several of

 Claims 1 to 7, characterized

 8.1 that the heights of the C02 expansion pressure for heat-generating machinery are to be interpreted as between 1 and 70 bar,

 8.2 that the heights of the C02 expansion pressure according to 8.1 are usually determined depending on the available coolant temperature,

 8.3 that the C02 flash pressure as per 8.1 is generally higher than the C02 pressure in a C02 tank of the C02 heat engine plant, after C02 has cooled in a process from C02 cooling to the given coolant temperature, the process being CO2 -Cooling takes place from the end of CO 2 supply from the CO 2 container and after switching from CO 2 to CO 2 cooling in the CO 2 container, ie a process of cooling for filling.

 9. A method for energy conversion by means of carbon dioxide according to one of

 Claims 1 to 8, characterized in that C02 transport systems such. Channels and / or transmission pipelines may be set up if there is no suitable site available for the construction of the C02 fluid storage facility at the C02 source sites, such as coal-fired power stations, and / or if there are local or temporal

 Bypasses are needed and these bypasses require the C02 transport.

 10. A method for energy conversion by means of carbon dioxide according to several of

 Claims 1 to 9, characterized

0.1 that when needed for the cooling of the C02 relaxation pressure some

Heat engines should be set as low as possible to produce the cold and more electricity, and

0.2 that the generated during cooling C02 gas is compressed by a gas driven with the electricity gas compressor and liquefied using the natural cold and / or other available refrigeration, and

0.3 that the compression heat generated by the compression of C02 gas is used for C02 heating for energy conversion.

 11. A method of energy conversion by means of carbon dioxide according to several of

 Claims 1 to 10, characterized

1.1 that C02 depressurization pressure should be kept as low as possible during the day for some thermal power generators in order to produce more electricity during the day as well as more cold when excess electrical power is available at night, and

1.2 that the excess electrical mains power at night to drive a

 Use gas compressor for the compression or liquefaction of the expanded C02 gas, and / or,

1.3 that the resulting during the gas compression C02 liquid and / or from the

 Gas compressor dissipated heat of compression during the day for the electric

 Energy to be used by the heat engines.

 12. Plant system for energy conversion by means of carbon dioxide as a working medium,

 characterized in that the plant system is set up for generating energy by a method according to one of claims 1-11.