Thermogalvanic overtemperature effect for the direct conversion of heat into useful chemical work and its advantageous technical applications

Abstract

The invention relates to a non-isothermal-isobaric thermogalvanic overtemperature effect that, in flow-through ion transfer cells with low process temperatures, achieves a complete conversion of heat into useful chemical work. Technical applications of this effect include extremely energy-efficient galvanic processes for separating or purifying liquid mixtures and the combined generation of electrical energy and hydrogen. The methods are based on the new finding that ions in an electrolytic solution can be moved not only according to the known isothermal-isobaric electrogalvanic principle, but also according to the new, non-isothermal-isobaric thermogalvanic principle. The new thermogalvanic overtemperature effect enables this with minimal thermal heat input; - in a type 1 ion transfer cell, without electron flow, the galvanic separation of any electrolytic liquid mixtures, - in a second type of ion transfer cell, the enrichment of selective overnumber ions in the involved solution streams and thus the chemical activation of the solution streams, without electron flow and - in a 3rd type ion transfer cell, the thermogalvanic neutralization of the excess ions with deactivation of the solution currents and external potential equalization with the release of electrical energy and, for example, hydrogen. The technical implementation using the first type of ion transfer cell is the TGD process. It is the ecologically and economically superior alternative to electrodialysis (EGD) and reverse osmosis (RO). The technical implementation of the second type of ion transfer cell with the third type of ion transfer cell is the TGEW process. It is the ecologically and economically superior alternative to the electrolytic hydrogen cycle of the fuel cell and to all current thermal power generation.

Description

[0001] The invention relates to a thermogalvanic overtemperature effect for emission-free, direct conversion of heat, preferably low-temperature heat and ambient heat, into useful chemical work, as well as process designs with consumption of this useful chemical work for the thermogalvanic separation or purification of liquid mixtures and for the combined thermogalvanic generation of electrical power and hydrogen.

[0002] Under the influence of the excess temperature effect, a directed ion transfer takes place between the solution streams in an ion transfer cell through which two similar electrolytic solution streams flow non-isothermally and isobarically. The heat input is converted into useful chemical work, which is consumed in equal amounts with the ion transfer. As the useful chemical work is consumed, the solution streams cool down on their flow path through the ion transfer cell, and an equilibrium-maintaining galvanic potential builds up between the solution streams.

[0003] There are at least three basic ways in which the overtemperature effect can be advantageously used in various non-isothermal-isobaric ion transfer cells: 1. For a directed, ion-neutral, non-isothermal-isobaric transfer of complementary ions from one solution stream to the other. This first-type ion transfer cell contains a membrane selectively permeable to anions and a membrane selectively permeable to cations. This complementary, non-isothermal-isobaric ion transfer occurs without electron flow, and the resulting galvanic potential between the ion-neutral solution streams is concentration-dependent and in the low millivolt range. 2. For a directed, non-isothermal, isobaric selective ion transfer of only one ion type, for example, protons, with the formation of excess ions in both participating solution streams. This second type of ion transfer cell then contains only a selectively proton-permeable membrane and electrodes as the outer boundary of the solution-flowing channels. This selective ion transfer chemically activates both solution streams with a higher heat input. The galvanic potential that builds up between the chemically activating solution streams at the electrodes is also implemented without electron flow and can assume any voltage value in the volt range and above. 3. For the non-isothermal-isobaric neutralization of excess ions contained in the chemically activated solution streams in a third-party ion transfer cell, for example with the release of hydrogen at the cathode and the release of oxygen at the anode as well as the delivery of electrical current to an external payload resistor.

[0004] This 3rd species ion transfer cell does not contain an ion-permeable membrane, but rather a partition wall between the solution streams that is impermeable to both electrons and ions, and electrodes that form the outer boundary of the solution-flowing channels. The operating voltage of this 3rd species neutralization cell is provided by the voltage-generating 2nd species ion transfer cell. It is set to the neutralization voltage value of the excess ion species to be converted. The heat consumption of the 3rd species ion transfer cell therefore corresponds to the heat consumption of the 2nd species ion transfer cell with a limited voltage value.

[0005] Technically usable are the first type of ion transfer cells for the non-isothermal-isobaric separation or purification of liquid mixtures in a TGD process design (thermogalvanic dialysis) and the combination of 2nd type and 3rd type ion transfer cells in a non-isothermal-isobaric flow TGEW process arrangement (thermogalvanic energy converter) for the combined production of electricity and neutral gases such as hydrogen and oxygen.

[0006] The driving force behind these three process types is the new, experimentally discovered thermogalvanic overtemperature effect. This includes: that ions move under the influence of excess temperature from an ion-neutral warmer solution stream into an ion-neutral colder solution stream and, that under the influence of this excess temperature, excess ions contained in the solution streams, for example protons and hydroxide ions, neutralize into the gases hydrogen and oxygen and generate an external electron flow with the potential equalization.

[0007] The chemical activity is measurable and is reflected in the galvanic voltage difference between the solution currents involved.

[0008] The temperature difference between the solution streams involved in ion transfer is the driving force, i.e., the effective excess temperature. This temperature difference between the solution streams remains constant across the ion transfer paths in the non-isothermal, isobaric ion transfer cells and leads to the cooling of the solution streams due to the useful energy consumption of the moving ions. The effective excess temperature also provides constant local ion transfer rates in the different designs of the three types of ion transfer cells.

[0009] The various effects of excess temperature are characteristic of the excess temperature effect. In the ion-neutral transfer of complementary ions, the excess temperature between the solution streams is small (0.1 to 5 K), and thus the equivalent consumption of useful chemical work is also small.

[0010] During the selective transfer of only one type of ion, for example protons, with the formation of excess ions in the solution streams and during the neutralization of these excess ions, the excess temperature can be between 10 and 100 K due to the higher equivalent useful energy consumption and the galvanic potential value generated can assume any desired voltage value.

[0011] If the galvanic voltage in the 2nd type ion transfer cell exceeds the neutralization voltage of the excess ions contained in the solution streams, then the excess ions can be converted into neutral gases under the repeated influence of the excess temperature effect in the 3rd type ion transfer cell.

[0012] Gibbs free energy analyses for the processes according to the invention, presented in Tables 1, 2.1, and 2.2, show that the energy content of the solution cooling generated by the excess temperature effect is 100% usable chemical work. This direct conversion of heat input into chemical work is complete and emission-free. It occurs at low process temperatures above and below ambient temperature.

[0013] The resulting TGEW process utilizes the thermogalvanic overtemperature effect in two ways: first, to build up voltage in the second-type ion transfer cell and then to convert the excess protons and hydroxide ions into the neutral gases hydrogen and oxygen in the third-type ion transfer cell. Electronic potential equalization is achieved via an external payload resistor with the release of electrical energy.

[0014] The resulting electroless TGD process according to the invention utilizes the overtemperature effect in one or more first-type ion transfer cells for ion-neutral ion transfer, without electron flow.

[0015] Today’s teaching knows and assesses energetically only the controllable ion-neutral isothermal-isobaric galvanic ion transfer generated with an electrical voltage from one ion-neutral electrolytic solution to another ion-neutral similar solution and the isothermal mechanical, ion-neutral ion transfer, which is carried out by means of an overpressure of the ion-releasing solution compared to the pressure-free ion-absorbing solution.

[0016] These well-known isothermal types of neutral ion transfer can be carried out using an electrically applied galvanic potential or an applied overpressure, with and against an existing concentration gradient. Examples include electrodialysis and reverse osmosis, or the charging and discharging of a lead-acid battery.

[0017] The non-isothermal-isobaric ion transfer according to the invention, implemented with the novel thermogalvanic overtemperature effect, is functionally equivalent to the known isothermal-isobaric electrogalvanic ion transfer. The imposed overtemperature can generate the same galvanic effect in electrolytic solutions as with electrical voltage or osmotic overpressure. The analogous effect of the overtemperature effect can be demonstrated very easily using the test device described in DE 10 2022 000 982.5.

[0018] Non-isothermal-isobaric ion transfer using the overtemperature effect has not yet been mentioned in the literature. For the first time, an ion-neutral non-isothermal-isobaric ion transfer similar to the overtemperature effect has been disclosed in DE 10 2016 014415A1.

[0019] However, the theoretical principles and technical explanations of the disclosed methods are incomplete in the document and incorrect in essential functional statements, so that the disclosed technical embodiments derived therefrom are not functional.

[0020] According to the Gibbs' law analyses in Tables 2.1 and 2.2, both reversible types of ion-neutral ion transfer (electrogalvanic EGD and thermogalvanic TGD) have different energy conversions with approximately equal work inputs and the same galvanic effect. The electricity component of EGD is functionally unnecessary and results in higher electricity consumption compared to the heat consumption of the electroless TGD process. The additional electricity consumption of EGD is contained as waste heat in the product effluents and further hinders ion transfer.

[0021] The thermogalvanic voltage difference of the non-isothermal-isobaric TGEW process with electron flow is equivalent to the theoretical electrogalvanic voltage difference of the current-consuming isothermal-isobaric electrolysis process.

[0022] The TGEW process and hydrogen electrolysis, with their reversal in a fuel cell, are conceptually developed into work-performing material cycles, resulting in very different energy conversions: The well-known isothermal-isobaric hydrogen cycle (electrolysis / fuel cell) consumes electrical energy in the forward reaction of electrolysis and generates electrical energy in the reverse reaction in the hydrogen fuel cell. The energy conversions in both process steps each contain entropic energy components that must be dissipated to the environment as waste heat. The isothermal-isobaric material cycle corresponds to the energetic behavior of a chemical energy storage system with high conversion losses; it is charged with electrical energy and released waste heat, and discharged with the release of electrical energy and waste heat.

[0023] The inventive material cycle of the TGEW process, which operates non-isothermal-isobarically over the temperature interval (To -Tu), converts the heat input completely into useful chemical work in both parts of the reversible concentration change using the new excess temperature effect. If this useful chemical work is withdrawn from the process or consumed in the process, the electrolytic working fluid cools down in circulation. Only as much useful chemical work can be generated and consumed as can be stored in the material cycle in the operating temperature interval (To -Tu).

[0024] The TGD and TGEW processes according to the invention are pollutant-free. They emit neither waste heat nor water vapor or CO2 and operate virtually silently. The energy efficiency and conversion efficiency are identical and always equal to one in relation to the total heat input.

[0025] There are therefore two particularly advantageous applications for the non-isothermal-isobaric thermogalvanic overtemperature effect according to the invention; the TGD process with the lowest possible excess temperature (To-Tm) of the ion-releasing electrolytic solution in the preferred range (To-Tm) = (0.1 K to approx. 5.0 K) and the TGEW process with the highest possible excess temperature ΔTü = (To-Tm) of the ion-releasing working fluid in the preferred range 10 K to 100 K.

[0026] With a constant circulation volume of the working fluid, a low excess temperature leads to a low solution cooling and a high excess temperature leads to a correspondingly high cooling range.

[0027] The TGD process with low excess temperature and large concentration change has the inventive goal of separating or purifying liquid mixtures without phase change, in a temperature-friendly manner and with minimal thermal energy consumption.

[0028] This TGD process is an economically and ecologically advantageous alternative to the current electrodialysis, which consumes electricity, to the conventional reverse osmotic liquid mixture purification, and to the conventional, extremely heat-consuming distillative mixture separation or liquid purification. In all known processes, the energy required for the purification or separation of liquid mixtures is higher than in the TGD process according to the invention.

[0029] The inventive TGEW process, with its high excess temperature and low concentration change, aims to convert the greatest possible amount of heat into useful chemical work and use this within the process to produce hydrogen, electrical energy, and cooling. The TGEW process therefore represents a particularly economically and ecologically advantageous alternative to the familiar hydrogen cycle of fuel cells and hydrogen electrolysis, as well as to current electricity-generating thermal energy conversion processes.

[0030] The thermally driven, non-isothermal-isobaric TGEW material cycle according to the invention differs significantly in terms of energy conversion from the known isothermal-isobaric hydrogen cycle of the fuel cell and from the energy conversions of all current thermal power generation technology.

[0031] The inventive TGEW cycle, which is carried out with an aqueous electrolytic working fluid, generates twice the amount of useful chemical work in the TGEW process arrangement with the same operating voltage compared to a hydrogen fuel cell. Half of this is used internally for the release of hydrogen and oxygen from the galvanic neutralization of excess H + - and OH-ions are consumed and the other half is released as useful electrical work via the voltage-stabilizing external payload resistor of the TGEW process arrangement.

[0032] Or to put it more simply: the TGEW process according to the invention, which operates with the excess temperature effect, produces 1 kWh of hydrogen and 1 kWh of electrical energy from the consumption of 2 kWh (low-temperature heat component and environmental heat component).

[0033] The well-known closed hydrogen cycle of the isothermal-isobaric hydrogen fuel cell, which is carried out in separate process facilities, consumes 2.37 kWh of electrical energy to provide one kWh of electricity and must release a total of 1.37 kWh of waste heat to the environment.

[0034] Today's thermal power generation technology converts a maximum of 60% of its heat input into electrical energy, with the highest risk of danger, and dissipates the remainder into the environment as waste heat.

[0035] The non-isothermal-isobaric thermogalvanic energy converter (TGEW) according to the invention is used in its simplest form as shown in Fig. 2, takes place in two solution-flowing TGEW ion transfer cells, one of the 2nd type and one of the 3rd type.

[0036] The resulting simple cell design facilitates the scalability of the TGEW process. The hazard risk posed by the TGEW process is extremely low due to low operating pressures, low process temperatures, non-hazardous operating materials, and the absence of harmful emissions.

[0037] Today's thermal energy conversion technology consumes fossil, nuclear, or biologically generated fuels with conversion efficiencies ranging from 25% to a maximum of 60% and emits waste heat, climate-damaging exhaust gases, and fossil and nuclear hazardous waste. As conversion efficiency increases, the risk posed by this technology to humans and the environment steadily increases.

[0038] As DE 10 2016 014 415A1 correctly discloses, the thermally driven non-isothermal-isobaric ion transfer, with its energetic properties, opens up completely new, previously unimaginable technical possibilities. However, these are not functionally exploited with the disclosed process designs and descriptions.

[0039] Only the TGEW process according to the invention, with its overtemperature effect, opens up the possibilities revealed. Not only is complete heat conversion possible with the TGEW process, and thus without waste heat, but it also generates, via the infinitely incremental product m c p· (To -Tu) of the electrolytic working fluid circulating in the process, higher useful energy yields than current isothermal-isobaric fuel cells, for example, the co-products hydrogen, electrical energy, and cooling, which have the same useful energy. The TGEW process also covers its heat demand with process waste heat below 80°C and with ambient heat, or entirely from ambient heat, and supplies additional, free cooling with the ambient heat component.

[0040] The TGEW process operates around the clock without heat supply outages, uses industrial process waste heat and ambient heat as a heat source, and requires no recooling equipment or long-distance electrical transmission lines. It emits no CO2, no water vapor, no noise, and consumes no fossil, nuclear, or biologically generated fuels.

[0041] TGEW process technology places no special demands on its operating location. It does not disfigure the landscape, does not consume valuable farmland, and does not pose a danger to humans or animals. Above all, it protects the environment, the climate, and the limited georesources available.

[0042] The TGEW process is particularly suitable for economical and environmentally friendly energy supply, for multifunctional energy supply of residential and office buildings, and for the re-electrification of industrial waste heat. It enables economical and environmentally friendly recycling of valuable materials. Furthermore, the TGEW process is suitable for both base load and peak load applications. It is therefore not only superior to current CO2-neutral conversion technologies in terms of conversion efficiency and energy density, but also makes a valuable contribution to a fail-safe, stable energy supply.

[0043] With the introduction of this new technology, energy in the form of electricity, hydrogen and water are no longer speculative resources and are accessible to everyone.

[0044] These new possibilities are correctly identified and assessed in document DE 10 2016 014415 A1. Errors and inconclusive assumptions in the theoretical foundations lead to non-functional technical implementations of the disclosed objectives in the disclosed document.

[0045] The object of the invention is therefore to functionally enhance the disclosed technical applications with newly developed and completed theoretical principles and to correct, supplement and simplify essential functional features in such a way that they fulfill the advantageous properties of the processes already shown in the disclosed document and, above all, ensure their function.

[0046] An essential part of the inventive problem therefore concerns the simplification and functional improvement of the disclosed material, non-isothermal-isobaric cycle process.

[0047] The process simplification is achieved in the TGEW process according to the invention by the functionality of the process as in Fig. 1 does not require two solution cycles, but only one electrolytic material cycle, and only one selectively permeable membrane is required for the ion transfer forming excess ions, instead of the four membranes disclosed.

[0048] According to the invention, this functionality is achieved by not performing an ion-neutral complementary ion transfer in the material cycle, but rather an ion transfer that generates and neutralizes excess ions. Only such a transfer generates the electrons for potential equalization during ion neutralization. The fact that the TGEW process produces electricity and hydrogen in combination is another concept of the invention. This concept is not contained in the disclosed document.

[0049] As stated in the process order of the Fig. As shown in Figure 2, the working fluid flows serially through two functionally complementary non-isothermal-isobaric ion transfer cells of the 2nd and 3rd type.

[0050] In the second-kind ion transfer cell, a first overtemperature effect shifts an ion species, preferably protons, across a selectively proton-permeable membrane from a preheated solution stream into a cooled solution stream and generates a galvanic potential difference between the two chemically activated solution streams with the formation of excess ions.

[0051] The electrodes of the 2nd type cell and the 3rd type cell are electrically connected, and the excess ion solution streams are assigned to the appropriate electrodes. In the 3rd type ion transfer cell, the chemically active, excess aqueous ions are neutralized to molecular hydrogen and molecular oxygen under the influence of the voltage and a second excess temperature effect. The electrons generated on the anode side flow, releasing electrical energy, via an external payload resistor to the cathode of the second ion transfer cell. Both excess temperature effects are introduced into the electrolyte circulation via an external heating device.

[0052] The non-isothermal-isobaric process disclosed in DE 10 2016 014415 A1, on the other hand, uses two identical type 1 ion transfer cells with a complementary ion transfer between two ion-neutral solution circulations, with opposing concentration increases and concentration decreases.

[0053] The external electron flow required for power generation does not occur in the disclosed process arrangement because the two ion-neutral solution circuits do not contain any excess ions capable of neutralization and cannot form any.

[0054] The thermal overtemperature effects are particularly important in the invention. The first overtemperature effect in the TGEW process ensures the chemical activation of the solution streams and the galvanic voltage buildup in the non-isothermal, isobaric second-type ion transfer cell. The second overtemperature effect ensures the neutralization of the energized excess ions entrained in the solution streams in the non-isothermal, isobaric third-type ion transfer cell.

[0055] Both excess temperature effects of the TGEW process, created by external heating, generate an equal amount of useful chemical work with the heat input. In the TGEW process, for example, this is completely converted into the usable useful work carriers hydrogen, oxygen, and electricity. The conversion of the heat input into useful chemical work is complete and emission-free. This is demonstrated by the attached Gibbs energy analysis in Table 1.

[0056] In the TGD process according to the invention, the excess temperature effect in the non-isothermal-isobaric first kind ion transfer cell without current flow ensures a neutral transfer of complementary ions and generates, in addition to the liquid products, a galvanic voltage determined only by the concentration difference of the solutions.

[0057] The new physical finding of the voltage-generating first overtemperature effect has been experimentally proven: ions can be shifted from one solution stream to another through a selectively ion-permeable membrane by means of an external overtemperature imposed on the electrolytic working fluid, thereby building up a galvanic voltage between the two chemically activated solution streams.

[0058] Characteristics of the overtemperature effect are the following properties: a constant overtemperature across the common flow path within the ion transfer cells, a continuous solution cooling on both sides across the common flow path, a constant concentration difference between the ion-releasing working fluid and the ion-absorbing working fluid across the common flow path, and a constant ion transfer rate across the common flow path.

[0059] In the TGD cells, these conditions are met by the counter-current flow of the solution in the ion transfer cells and in the TGEW cells by the rectified flow of the working fluids in the ion transfer cells.

[0060] Table 1 shows the Gibbs energy analysis of the TGEW solution circulation according to the invention according to Fig. 1 of the TGEW process order according to Fig. 2.

[0061] As can be seen from the Gibbs balance in Table 1, the useful energy yield (-ΔG) which is calculated in the TGEW process arrangement according to Fig. 2 is extracted or consumed over the cooling temperature interval (To-Tu) is twice as high as the heat input possible via the external reheating of the ion-rich working fluid. This results in the double reheating of the solution circulation from (Tu → To).

[0062] The entropic useful work excess +Δ(T s) resulting from the TGEW process balance is neither theoretically nor process-technically addressed in the disclosed document. However, it fulfills two fundamental functional process functions. Firstly, without energetic compensation, when the chemical useful work is removed, it causes uninhibited cooling of the working fluid in the ion transfer cells, which only stops when the working fluid freezes. Secondly, as will be shown later, without energetic compensation of the entropic TGEW useful work excess, the formation and neutralization of excess ions of the dissociated water component is not possible. This also prevents the extraction of electrical energy in the disclosed process. However, the disclosed document correctly recognized that complete heat conversion into chemical useful work must be possible.

[0063] According to the invention, the energy deficit of the entropic TGEW useful energy surplus +Δ(T s) is compensated with an equivalent second external heating of the working material circulation. The first and second heating are carried out over the same temperature interval (Tu → To) and differ in their mode of operation.

[0064] The heat input from the initial heating (-ΔH) causes the selective displacement of one or both ionic charge carriers across an anion and / or cation permeable membrane in the second-kind ion transfer cell. This activates the solution flows and, together with the displaced ion species, defines the polarity of the electrodes of the first second-kind ion transfer cell. The displaced or retained predominant cations define the positive pole, and the displaced or retained predominant anions define the negative pole of the process arrangement according to Fig. 2.

[0065] The equivalent entropic heat input +Δ(T s) of the secondary heating of the solution circulation provides the 3rd species ion transfer cell with the chemical work required for the galvanic neutralization of the complementary excess ions of the water component, thus activating the electron flow from the anode via the external payload resistance (Ra) to the cathode. The solution streams involved in the material circulation enter the upper 2nd species ion transfer cell ion-neutral, with a higher solvent concentration, and exit the lower 3rd species ion transfer cell ion-neutral, with a lower solvent concentration.

[0066] Here, the proton-excess solution stream [(y + ) r ; (x - )a] the cathode and the hydroxide ion excess solution current [(x - )r; (y + )a] the anode of the 3rd kind ion transfer cell.

[0067] Further inventive features are the development and application of the excess temperature principle to economically and ecologically valuable process arrangements, for example the TGD process for the separation or purification of electrolytic liquid mixtures and the TGEW process for loss-free thermogalvanic energy and material conversion with the conversion of heat and the neutralization of the complementary excess ions of the dissociated water component via the intermediate stage of chemical work into gaseous hydrogen and oxygen with the release of electrical energy.

[0068] A further inventive feature is that the TGEW process, using, for example, an aqueous ammonia solution or an alkali metal ammonia solution as ion-transferring working fluid, is operable down to minus 85 °C and covers its heat demand with low-temperature heat below 80 °C and with ambient heat.

[0069] The TGEW process therefore forms the basis for a future environmentally neutral low-temperature power generation technology. It requires neither fossil, nuclear, nor biologically produced fuels. It uses exclusively industrial waste heat and solar ambient heat and does not require recooling facilities, but rather facilities for absorbing process waste heat and ambient heat.

[0070] A further inventive feature, which is particularly advantageous from an ecological and economic point of view, is that the thermogalvanic dialysis process arrangement (TGD) consists of several, preferably up to 6 serially flowing TGD ion transfer cells and thus produces industrial brine concentrated to saturation from seawater with any input salt content, drinking water or ultrapure water, and the ion-releasing salt water inlets of the individual ion transfer cells are heated externally.

[0071] The heat required for the external provision of the excess temperature in the individual TGD cells of the separation cascade add up. The smaller the individual temperature differences of the excess temperature in the TGD separation stages, the lower the overall thermal energy required for the ion-neutral TGD separation cascade.

[0072] The following functionally hindering and disadvantageous features disclosed in document DE 10 2016 014415A1 are avoided with the process changes and process additions according to the invention.

[0073] As is well known, the flow pattern through the ion transfer cell is arbitrary in isothermal-isobaric mixture separation processes and fuel cells. This is no longer arbitrary in non-isothermal-isobaric processes. In the disclosed document, no defined flow pattern was chosen for the TGD-like and TGEW-like process types.

[0074] According to the invention, there is a clear allocation of the flow type (cocurrent or countercurrent) for non-isothermal isobaric TGD and TGEW ion transfer cells. Thus, TGD mixture separation cells operating according to the overtemperature principle are advantageously flowed according to the countercurrent principle, while TGEW heat conversion cells are advantageously flowed according to the cocurrent principle.

[0075] In non-isothermal-isobaric TGD mixture separation, the flow pattern is not determined by the constant overtemperature of the ion-releasing working fluid, but rather by the concentration difference ±ΔX between the two similar working fluid streams involved in the ion transfer. The concentration difference must be kept constant throughout the flow path in the TGD ion transfer cell. This minimizes the required overtemperature of the ion-releasing fluid, thus minimizing the heat required for mixture separation.

[0076] The supertemperature ion transfer of complementary ions from the ion-donating to the ion-accepting solution stream of the TGD ion transfer cell is ion-neutral and generates no electron flow, requiring no electron flow. The TGD mixture separation method is therefore particularly energy-efficient and temperature-friendly.

[0077] The disclosed TGD-like ion transfer cell for separating liquid mixtures, however, contains functionally unnecessary electrodes. These electrodes hinder the process.

[0078] Nevertheless, the working fluids involved in the ion transfer must be galvanically separated and routed through the mixed-separation TGD ion transfer cell. This is because the overtemperature imposed on one side creates a galvanic potential difference between the fluid streams involved in the ion transfer, which counteracts the directed ion flow. A galvanic short circuit across the cell housing would destroy the driving force of the separation process.

[0079] The absence of electrodes, but the galvanic separation of the liquid streams, are innovative features of the TGD ion transfer cell. For near-ambient-temperature, thermogalvanic separation or purification of liquid mixtures, a metal-free, all-plastic construction of the TGD ion transfer cell and its supply and discharge lines, compatible with the working materials, is therefore the preferred design solution.

[0080] According to the invention, the thermogalvanic voltage difference resulting from the excess temperature must be set higher than the opposing galvanic countervoltage difference resulting from the concentration difference to be overcome. The adjustable excess temperature, as a control variable, not only prevents ion backflow, but also influences the ion transfer rate in the selectively ion-permeable membranes of the TGD cell.

[0081] The inventive overtemperature of the ion-releasing working fluid compared to the ion-absorbing working fluid of a TGD cell can be achieved either by external heating of the ion-releasing working fluid and / or by external cooling of the ion-absorbing working fluid.

[0082] Even more efficient, and also in accordance with the invention, is the interposition of a double-acting compression heat pump, which, to provide the excess temperature, externally cools the ion-absorbing working fluid and, at the same time, uses its generated waste heat to externally heat the ion-releasing working fluid. This allows the excess temperature required for ion transfer to be achieved with half the energy consumption of a single-acting heat pump.

[0083] With the intermediate heat pump, the TGD arrangement operates independently of an external heat source and with extremely low electrical separation effort. For example, if brackish water with a salinity of 2.0% is fully demineralized with a TGD cell, as shown in Table 2.1, the theoretical thermal separation effort without the use of a heat pump is only 0.54 kWh / m 3 Ultrapure water.

[0084] If the required excess temperature of 0.4 K is provided by an intermediate, double-acting compression heat pump, the theoretical separation effort drops to 12.5 Wh el / m 3 plus a pumping energy expenditure of about 80 Wh el . / m 3 Ultrapure water. Today's most efficient electrodialysis desalination plants (EGD) require about 1.5 to 2.0 kWh el / m 3 Ultrapure water, its separation effort is 15 to 20 times higher.

[0085] The use of the double-acting compression heat pump is particularly worthwhile for photovoltaic-powered decentralized TGD desalination plants. One square meter of photovoltaic surface produces an average of 0.5 kWh of electricity per day. With this amount of electricity, a TGD desalination plant produces an average of 5 m 3 Drinking water daily.

[0086] The TGEW ion transfer cell according to the invention, like conventional electrolysis cells, only requires a membrane that is selectively permeable to ions, preferably permeable to protons.

[0087] DE 10 2016 014415A1 lacks the functional process component that converts the chemical work into usable electrical work. This is because the disclosed complementary ion shift does not generate an electron flow due to the lack of neutralizable excess anions and cations.

[0088] If electrons are to be generated using the overtemperature principle, the operating voltage of the TGEW ion transfer cell must, on the one hand, exceed the voltage value of 1.43 V for the neutralization of the aqueous excess ions. On the other hand, the separated excess anions and excess cations must be galvanically neutralized as described in the Fig.2 must be supplied to the corresponding electrodes. Only then do the necessary electrons flow from the anode to the cathode of the TGEW cell via the external electrical payload resistor to compensate for the charge.

[0089] According to the invention, the electrode allocation of the solution streams enriched with surplus ions in the TGEW process arrangement is Fig. 2 with an electrical cross-connection of the electrodes of both ion transfer cells.

[0090] Then the left electrode of the first ion transfer cell is electrically connected to the right electrode of the second ion transfer cell, while the solution currents as in Fig.2, the ion flow is shown in a straight line through the two ion transfer cells. However, the straight electrode connection of both cells and the cross-connection of the solution streams also achieve the same goal; the correct electrode assignment is crucial. The external payload resistor stabilizes the voltage difference between the electrodes of the TGEW cells and, with its electrical energy output, keeps the ion neutralization voltage of the second type of ion transfer cell constant. Internal ionic resistances of the TGEW cells can be compensated and controlled independently of each other using the excess temperature and the mass circulation of the electrolytic working fluid.

[0091] Fundamentally, the following applies: No thermogalvanic formation and separation of excess anions and cations means no possibility of neutralizing excess ions with external electron flow. No electron flow means no electrical energy release at the external payload resistor, and no consumption of useful chemical work means no solution cooling.

[0092] These requirements are missing in the method disclosed in DE 10 2016 014415A1. This explains the lack of functionality.

[0093] Another new finding from the theoretical analyses is that in the TGEW process, the chemical energy consumption values ​​of hydrogen production and the external electrical payload add up.

[0094] There is a useful work amount for the external electron flow and an equivalent useful work amount for the internal ion flow. Consequently, in the loss-free case, the two voltage differences are also equal.

[0095] This is the result of the Gibbs energy analyses of the TGEW cycle according to Table 1. The useful energy yield (-ΔG) of the process according to Fig. 1 consists of two approximately equal components (-ΔH) and (+Δ(T s)). The amount (-ΔH) is contained in the cooling temperature interval (To-Tu) of the working fluid and is introduced with the external initial heating. The entropic amount (+Δ(T s)) must be added to the working fluid for energy balance by means of the external secondary heating over the same cooling temperature interval (To-Tu).

[0096] These are therefore two parallel-connected energy consumers that share the total energy yield (-ΔG). Consequently, only half of the energy yield should be used to calculate the electrical cell voltage using the Nernst equation, so that the internal ionic voltage difference and the external electronic voltage difference of the non-isothermal-isobaric TGEW process arrangement are equal.

[0097] This is because in the TGEW process arrangement, only as many electrons can flow across the external load resistance as are converted into the galvanic neutralization of the excess anions and cations of the dissociated water component at the electrodes of the 3rd type TGEW cell.

[0098] If these statements are applied to the function of the non-isothermal-isobaric TGEW ion transfer cells, this means that the excess temperature and mass flow of the circulating ion-transferring working fluid influence the cell voltage of the 2nd kind ion transfer cell as a joint product, and only an external thermal compensation of the entropic useful work excess compensates the electronic voltage difference of the external payload resistor with the electron turnover of the 3rd kind ion transfer cell.

[0099] In this inventive way, as in Fig. As shown in Figure 2, all TGEW process conditions for combined hydrogen production and electrical energy release are realized in a single TGEW working fluid circuit. To reduce TGEW circuit losses, the electrolyte supply and discharge lines of the TGEW ion transfer cells are galvanically isolated and designed with high electrical resistance.

[0100] The disclosed document DE 10 2016 014415 A1 lacks the functionally required compensation of the entropic useful work excess. This not only results in half of the potential chemical useful work yield being lost compared to the inventive TGEW solution, but the process fails altogether because the amount of useful work required to compensate for the external electronic voltage difference of the payload resistor is missing. The TGEW-like process disclosed in document DE 10 2016 014415 A1 cannot provide hydrogen or electrical energy due to the lack of excess ion generation and thus does not allow for cooling of the working fluid.

[0101] The inventive secondary heating of the TGEW material circulation fulfills these fundamental functional requirements of the TGEW energy conversion cycle. It compensates for the entropic useful work deficit (Δ(T s)) of the TGEW working fluid circulation without changing the ion transfer rate.

[0102] Furthermore, in the disclosed process design, the temperatures and concentrations of both solution circulations in the cells of the disclosed document DE 10 2016 014415A1 overlap. Thus, the voltage across the flow path within the ion transfer cells does not remain constant. It changes, resulting in a reversal of the ion shift in the TGEW-like cells. The inventive overtemperature principle avoids these functionally detrimental overlaps.

[0103] The invention and further embodiments of the invention are described below with reference to the Fig. 1-4 schematically illustrated embodiments are explained in more detail.

[0104] The figures show in detail: Fig. 1 the electrolytic material cycle of the TGEW cycle according to the invention in a schematic temperature-concentration diagram of any electrolytic working fluid, Fig.2 the process arrangement of the TGEW cycle according to Fig. 1 for thermogalvanic water separation with combined production of hydrogen and electrical energy, with refilling of used water, Fig. 3 a TGD process arrangement for the thermogalvanic separation of an electrolytic solution, for example for the production of drinking water from brackish water with salt contents below 2.5% and Fig. 4 the flow principle of the depleted and enriched salt water streams in a multi-cell TGD separation cascade with, for example, four serially flowing, in the Fig. 3 shown TGD ion transfer cells with the products drinking water or ultrapure water and industrially usable brine with saturated salt content.

[0105] Fig. 1 shows the material circulation (U) of the TGEW process in a schematic temperature - concentration diagram of any electrolytic working fluid as in Fig.2. The reference points ① to ⑩ indicate the process steps that the electrolytic material circulation in the specified order in the process arrangement according to Fig. 2. These circled reference points serve as reference points in the Fig. 1 and Fig. 2 for better orientation.

[0106] The TGEW process operates between the upper limit temperature (To) and the lower limit temperature (Tu) and the concentration limits (X rich) and (X poor) of an aqueous electrolytic solution circulation (U). The average temperature (Tm) represents, for example, the ambient temperature (T ∞ ).

[0107] The temperature difference (To-Tm) defines the excess temperature (ΔTü) required to generate the galvanic potential in the upper 2nd type ion transfer cell and the excess temperature (ΔTü) required to neutralize the excess ions in the lower 3rd type ion transfer cell. Both excess temperatures are equivalent and are generated using an external heating device.

[0108] The excess temperature values ​​remain constant as the ion transfer cells flow through them, while the chemically active solution streams cool down continuously as a result of the chemical work consumption along their flow path in the cells.

[0109] In the upper 2nd kind cell, which builds up voltage, the proton-donating solution stream cools from (To → Tm), and the proton-accepting solution stream cools from (Tm → Tu). In the lower 3rd kind cell, which neutralizes excess ions, the cation-excessive solution stream cools from (To → Tm), and the anion-excessive solution stream cools from (Tm → Tu).

[0110] If a temperature below the ambient temperature is selected for Tm, the heat gain (Tu→ ≤Tm) can be absorbed from the environment. The heat gain (≤Tm→To) can be obtained from industrial waste heat or solar heat.

[0111] In the upper 2nd type ion transfer cell of the Fig. 2 Under the influence of the first excess temperature, the galvanic voltage difference between the chemically active solution currents involved builds up with the formation of excess ions.

[0112] In the lower 3rd type ion transfer cell of the Fig.2 neutralize the excess ions into molecular hydrogen and oxygen under the influence of the galvanic voltage and the second excess temperature, generating the external electron flow via the payload resistor. The neutral gases are removed from the solution circulation. The electrons flow from the anode via the payload resistor to the cathode of the lower third ion transfer cell. By consuming the chemical work, both chemically active solution streams cool down, thereby changing their concentration to the same ion-neutral final value (X arm) of the solution circulation.

[0113] With the addition of the stoichiometrically consumed water component, the ion-neutral, potentially proton-releasing solution stream re-enriches to the ion-neutral concentration value (X rich) of the solution circulation. External heating ensures the solution inlet temperature (To ), while the potentially proton-receiving solution stream is returned thermally untreated to the upper 2nd type ion transfer cell at the ion-neutral concentration value (X poor) of the solution circulation and at an average temperature (Tm).

[0114] The amount of chemical work that can be stored in the solution circulation of the TGEW process can be changed via the excess temperature amounts (ΔTü) and via the concentration change interval of the solution circulation ΔX = (X rich - X poor).

[0115] With the change of the ion-neutral concentration change interval, the product-specific solution circulation amount (f) changes according to the relationship f = (1 -Xa) / (Xr- Xa).

[0116] Here, (f) refers to the mass flow of the ion-neutral, rich aqueous solution, and (f-1) to the mass flow of the ion-neutral, poor solution. Both values ​​refer to the reversible depletion or enrichment rate of 1 kg of complementary ions of the dissolved mixture component.

[0117] The specific circulation volume (f) of the working fluid increases at a constant ion depletion rate of one kg of complementary excess ions in water with a decrease in the concentration change ΔX = (Xr-Xa). This results in another advantageous feature of the TGEW process.

[0118] The smaller the concentration change ΔX of the dissolved component in the fluid circulation, the greater the specific circulation volume (f) of the working fluid and thus the generated useful chemical work yield, while maintaining a constant heating temperature difference (Tu →To). This property allows the internal process conditions of the TGEW process to be particularly well adapted to the externally available temperatures of the waste heat sources to be utilized.

[0119] At a constant ion transfer rate, a high circulation rate with a low excess temperature is energetically equivalent to a low circulation rate with a high excess temperature. Both generate the same galvanic potential. The distance from (Tm→Tm) changes by the same amount. This means that a high upper process temperature (Tm) results in a low process temperature (Tm). The distance from the ambient temperature (T ∞) is the same. This process behavior influences the amount of ambient heat that can be converted in the TGEW process.

[0120] This approach applies to closed electrolytic material cycles and to material cycles such as the TGEW cycle with replenishment of a continuously consumed mixture component, with continuous supply of a mixture component (X·Y), its dissociation and discharge as neutral gas products (X) and (Y).

[0121] In Fig. 2, the used mixture component (X·Y), e.g., water, is continuously introduced into the electrolytic working fluid circuit, and the neutral gases hydrogen (Y) and oxygen (X) are continuously removed from the working fluid circuit. The added used mixture component water (X·Y) dissociates in the working fluid to x - -ions and y + -ions and enriches the working fluid from the depleted final state (x - a , y + a) to the enriched initial state (x - r , y + r ) of the TGEW process. The component concentrations (X La ) and (X Lr ) the Fig. 1 correspond to the ion concentrations (x - a , y + a ) and (x - r , y + r ) the Fig. 2.

[0122] The following is the non-isothermal-isobaric electrolytic working fluid circulation of the TGEW process arrangement of the Fig. 2 described.

[0123] The TGEW process order according to Fig.2 consists of the 2nd type ion shift cell (10) and the 3rd type ion neutralization cell (11). Cells 10 and 11 are arranged one behind the other in terms of flow and contain the chambers (10.1) and (10.2) through which the electrolyte circulation (12) flows, as well as the chambers (11.1) and (11.2). Chambers 10.1 and 10.2 are separated in the middle by the cation-permeable, preferably proton-permeable, membrane 13 and are bounded on the outside by the electrodes 14 and 15. The proton-permeable membrane 13 is impermeable to electrons. Electrode 14 is assigned to the flow-through chamber 10.1, and electrode 15 to the chamber 10.2.

[0124] The chambers 11.1 and 11.2 of the 3rd Art ion neutralization cell 11 are delimited in the middle by the electrically non-conductive, ion and electron impermeable partition 16 and on the outside by the electrodes 14 and 15. The electrode 15 is assigned to the chamber 11.1 and the electrode 14 to the chamber 11.2. Both electrodes change their lateral positions from the 2nd Art ion transfer cell 10 to the 3rd Art ion neutralization cell 11, so that the positive pole 17, for example, represents the right boundary of the flow channel 10.2 in the cell 10 and the left boundary of the flow channel 11.1 in the cell 11.

[0125] In the second Art ion transfer cell 10, the negative pole 18 represents the left boundary of the flow channel 10.1, and in the third Art ion transfer cell 11, the boundary of the right flow channel 11.2. The respective same-polarity electrodes 14 and 15 of both cells 10 and 11 are externally electrically connected to each other, and the positive pole 17 and negative pole 18 of the cell arrangement are short-circuited via the external electrical load resistor 26.

[0126] The circulation 12 of the electrolytic solution through the TGEW process arrangement is as follows: The ion-neutral, rich solution 20, heated to, for example, 60 °C, is introduced into the top of chamber 10.1 of the second-type ion shift cell 10. It flows through chamber 10.1, becoming depleted of protons and undergoing self-cooling. The proton-depleted, anion-excessive solution 20.1 exits chemically activated at the bottom of chamber 10.1 at 20 °C. The cooled, chemically activated, anion-excess solution 20.1 is reheated to 60°C in the external heat exchanger 21.1 and then flows through the chamber 11.1 of the third ion transfer cell 11 located below. In chamber 11.1, the excess anions are neutralized by releasing electrons and gaseous oxygen 22, and by consuming useful chemical work. The oxygen is removed from the solution circulation 12 via the gas separator 25.1.

[0127] The electrons generated on the anode side in the chamber 11.1 flow to the cathode 14 of the cell arrangement via the external load resistor 26, reducing the voltage difference between the negative pole 18 and the positive pole 17 and releasing electrical energy.

[0128] The ion-neutral solution 20.3 flowing out of cell chamber 11.1 has an outlet temperature of, for example, +20 °C. It is introduced into chamber 10.2 at the top of the second-type ion transfer cell 10 without reheating and flows through chamber 10.2 and the subsequent chamber 11.2 in the same flow direction as the solution stream 20 flows through chambers 10.1 and 11.1 of the TGEW process arrangement.

[0129] In chamber 10.2, the solution stream 20.3 absorbs the protons flowing across the membrane 13, consuming useful chemical work. The excess proton solution stream 20.2 flowing out of chamber 10.2 is reheated in the heating device 21.2, for example, from -20°C to +20°C, and introduced on the cathode side into chamber 11.2 of the third type of ion transfer cell 11. The excess cations (protons) are converted to molecular hydrogen 23 in the neutralization chamber 11.2, absorbing the electrons generated on the anode side and conducted through the load resistor 26, and consuming useful chemical work. The hydrogen 23 is then removed from the solution stream 20.3 via the gas separator 25.2. The solution effluent 20.3 from chamber 11.1 is reheated to ambient temperature in the heating device 21.3. The used circulation water 24 is then added.Pump 19 ensures solution circulation through the TGEW process arrangement and initially conveys the rich solution 20 to its initial temperature of 60°C through heater 21.4 before being reintroduced into chamber 10.1 at the top of the second type ion transfer cell 10. Heaters 21.1 and 21.4 preferably utilize industrial process waste heat or solar heat to reheat the circulating solution streams, while heaters 21.2 and 21.3 preferably utilize ambient heat.

[0130] Functionally, the excess temperature of the proton-depleting solution stream 20 compared to the proton-accepting solution stream 20.2 provides the thermogalvanic driving force for the proton shift. The proton-accepting solution 20.2 becomes electrically positive due to the excess protons, thus defining electrode 15 as the positive pole 17 of the TGEW process arrangement. On the other hand, the excess anions of the proton-depleting solution stream 20.1 make it negative, thus defining electrode 14 as the negative pole 18 of the TGEW process arrangement.

[0131] The solutions charged with excess ions flowing out of the second type ion transfer cell 10 on both sides are, after being externally heated in the heating devices 21.1 and 21.2, introduced into the third type ion transfer cell 11 without changing sides at the head. The solution stream 20.2 charged with excess protons or cations flows through the negative pole channel 11.2, and the solution stream 20.1 charged with excess anions flows through the positive pole channel 11.1. At the lower outlet of chambers 11.1 and 11.2, the solution streams 20.3 and 20.4 are ion-neutral, but lower than the ion-neutral solution stream 20 by the stoichiometrically converted amount of water. By means of crossed external electrical connecting lines 27.1 and 27.2, the positive and negative poles change their positions at the transition from the 2nd type ion transfer cell 10 to the 3rd type ion transfer cell 11, so that the flow through both cells remains straight.

[0132] The conversion of the excess ions into the neutral gases hydrogen and oxygen in the 3rd kind ion transfer cell 11 requires the same amount of chemical work as the galvanic voltage buildup through the proton shift in the 2nd kind ion transfer cell 10. This process leads to solution cooling by consuming the generated chemical work in the flow-through chambers (10.1 and 10.2) and (11.1 and 11.2) of the TGEW process arrangement. In the serial pass through the chambers (10.1 and 11.1), the solution circulation 12 changes its ion-neutral state from the initial state (x - r , y + r ) to the final state (x - a , y + a ). The addition of the consumed water component (X·Y) restores the ion-neutral initial state (x - r , y + r) in the solution circulation 12. When flowing through the chambers (10.2 and 11.2), the ion-neutral, poor state (x - a , y + a ) in the solution circuit 12 at the inlet of chamber 10.2 is the same as that at the outlet of chamber 11.2.

[0133] The energy requirement of the voltage-building ion-transfer process section corresponds to the cooling of the working fluid over the temperature interval (To→Tu). The reheating (Tu→To) of the working fluid occurs with the external initial heating in the heating devices 21.3 and 21.4. In the Gibbs energy balance of the TGEW process, as shown in Table 1, the initial heating provides the -ΔH component of the total amount of generated useful chemical work -(ΔG). This amount of useful work is dissipated as electrical energy at the external useful load resistor 26.

[0134] The transfer of the excess ions (x - r - x - a ) and (y + r - y + a ) in the third type of ion transfer cell 11 into the neutral gases hydrogen (Y) and oxygen (X) requires the same amount of energy. This energy is supplied by the external secondary heating of the working fluid over the same temperature interval (Tu→To) in the heating devices 21.1 and 21.2.

[0135] The secondary heating produces the entropic +Δ((T o - s o ) - (T u · s u ))-Share of the total amount of useful chemical work generated -(ΔG). This useful work share is included in the calorific value of the discharged product neutral gases.

[0136] The double heating or reheating of the working fluid circulation 20 in the external heat exchangers 21.1 to 21.4 takes place over two temperature intervals, in the heat exchangers 21.2 and 21.3 over the temperature interval (Tu→Tm) and in the heat exchangers 21.1 and 21.4 over the temperature interval (Tm →To).

[0137] The following Table 1 shows the calculation procedure for the Gibbs energy balance of the non-isothermal-isobaric TGEW cycle according to Fig. 1 and Fig. 2. The calculations were carried out using the Gibbs equilibrium state variables of the electrolytic working fluid table salt / water as an example.

[0138] For the energy balance of the TGEW process according to Fig. 1 and Fig.2, only the energetic inlet values ​​of the ion-neutral, rich working fluid (20) at To and the energetic outlet values ​​of the ion-neutral, poor working fluid (20.4) at Tu are important. The energetic values ​​of the non-neutral, excess ion-laden fluid streams (20.1 to 20.3) cancel each other out in the energy and material balance of the TGEW process arrangement.

[0139] As the Gibbs TGEW energy analysis in Table 1 reveals, the imposed excess temperature ΔTü = (To-Tm) generates the same operating voltage as the known isothermal-isobaric fuel cell, but with twice the useful energy output. The process produces hydrogen and the same amount of electrical energy. The calorific value of the produced hydrogen corresponds to the electrical energy output of the payload resistor (26).

[0140] Although the energy balance of the TGEW cycle is balanced overall, the values ​​of ΔH and Δ(T·S) are not equal. This is due to inaccurate Gibbs phase equilibrium state variables, particularly their deviation from the isobaric process conditions of the cycle.

[0141] For example, with the process temperatures (To, Tm, and Tu) and concentration changes specified in Table 1, the TGEW cycle with the working fluid NaCl / H2O achieves a total specific useful energy output of 394 Ws / g of circulating rich solution. Of this, 197 Ws / g is attributable to hydrogen release and another 197 Ws / g to electrical energy release. The process's own electrical consumption is less than 1% of the usable useful energy output.

[0142] As long as the operating voltage of the TGEW process with the working fluid circulation of the selected aqueous saline solution is limited to 1.43 V and thus remains below the neutralization voltage of the chlorine, hydrogen is formed as the neutral gas and no chlorine.

[0143] According to the Nernst equation, the basis for calculating the thermogalvanic voltage difference of the 2nd type ion transfer cell is only the useful work output (-ΔG / 2), since the consumed chemical work amounts of the internal ion displacement and the external electrical energy output at the payload resistor are equivalent.

[0144] The total voltage difference of the non-isothermal-isobaric TGEW process arrangement according to Fig. 2 is 11.4 V for the NaCl / water electrolyte system using the process data in Table 1. The voltage value of 1.43 V for the neutralization of the excess complementary H + - and OH --ions is achieved with these process data using a solution circulation volume (20) of 49.45 g. This results in a minimum energy conversion of 9,446 kJ.

[0145] Any electrolytic basic or acidic solution can be used as the ion or electron transferring working fluid in the TGEW process, for example an aqueous saline solution or an aqueous ammonia solution or an aqueous alkali metal hydroxide solution or an alkali metal ammonia solution or an alkali metal alcohol solution.

[0146] The use of an electrolytic solution with a particularly low freezing point, such as an aqueous ammonia solution or a sodium ammonia solution, is beneficial and effective for the process. An aqueous ammonia solution with an ammonia content between 25 and 35% can be cooled to minus 85 °C (Tc) without freezing.

[0147] With this lower temperature (Tu), the working fluid circulation can, for example, be heated externally with ambient heat Q ∞ to the temperature (Tm). Only for further reheating up to the upper process temperature (To) is low-temperature heating energy (Q H ) needed.

[0148] The TGEW process only requires upper working fluid temperatures (To) of a maximum of 80°C, although lower process temperatures are also sufficient. This makes it possible to use all industrial process waste heat and solar heat, both combined with ambient heat, as a replacement for fossil fuels for heating the TGEW energy conversion and material separation process according to the invention. Waste heat from decommissioned nuclear power plants can also be permanently converted into electricity using the TGEW process.

[0149] The TGEW process not only provides useful chemical work in a particularly economical and ecological way, but also, with the environmental heat component, simultaneously and without additional expenditure, valuable process cooling. Today's electricity-consuming refrigeration systems and recooling equipment are no longer required when using the TGEW process, and cooling water is also no longer required for electricity generation.

[0150] With external heating of the aqueous working fluid using the self-generated neutral products hydrogen (23) and oxygen (22), the TGEW process can be carried out according to Fig. 1 and Fig. 2 cover its heat requirements entirely from ambient heat when using only electrical energy.

[0151] If the neutral products (22) and (23) are recycled and catalytically combusted into the working fluid circuit (12), the TGEW cycle process that generates electrical energy does not require an external water supply (24). This TGEW process design is therefore particularly suitable as an energy source for future space missions.

[0152] The following descriptions ( Fig. 3 and Fig. 4) relate to extremely efficient and energy-saving TGD process arrangements for the separation of liquid mixtures. The separation of the mixture components takes place in a particularly temperature-friendly manner, with only a slight temperature increase compared to the ambient temperature and without phase change.

[0153] For example, the following Tables 2.1 and 2.2 show a comparison of the Gibbs TGD and EGD energy balances for the separation of an aqueous saline solution.

[0154] Table 2.1 shows the energy ratios of the thermogalvanic, non-isothermal-isobaric TGD mixture separation method according to the invention. Table 2.2 shows the energy ratios of the electrogalvanic isothermal-isobaric EGD mixture separation technique according to the state of the art.

[0155] For minimal thermogalvanic separation effort, the entropy term Δ(T s) in the Gibbs energy balance of the TGD must approach zero. Then, the external heat input (-ΔH) provides the required negative work potential (-ΔG) for the displacement of the ions without external electron flow. This value (-ΔG) is stored as additional work potential in the product streams flowing out of the TGD cell.

[0156] As the comparison of the results in Tables 2.1 and 2.2 shows, the energy separation requirements of the thermal TGD method according to the invention and the electrogalvanic EGD separation method, which represents the state of the art, are almost equivalent. However, they differ in their signs. The EGD separation method consumes electrical energy (+ΔG), which leads to heating of the product streams within the EGD cell. The TGD method according to the invention consumes low-temperature heat (-ΔH) and delivers the same amount of useful work (-ΔG).

[0157] The new thermogalvanic TGD separation method according to Fig.3, for example, requires, under the separation conditions shown in Table 2.1, only a constant excess temperature of the ion-releasing solution compared to the ion-absorbing solution of 0.4 K for the ion displacement over the entire flow path. The consistently constant excess temperature of the TGD method thus provides the same galvanic equilibrium voltage as the current-consuming electrogalvanic EGD method, according to Table 2.2.

[0158] The thermogalvanic TGD process arrangement for separating liquid mixtures according to Fig. 3 contains as components a flow-through non-isothermal-isobaric 1st type ion transfer cell 31, an external heating device (32), and a conveying device (33). The TGD ion transfer cell (31) operates, for example, in the separation of aqueous solutions with a thermally generated operating voltage below 1.23 volts, without water decomposition and therefore also without external electron flow compensation.

[0159] The first ion transfer cell of the TGD process (31) contains an anion-permeable membrane wall (34) and a cation-permeable membrane wall (35) for complementary ion-neutral ion transfer. The two media-separating membrane walls (34) and (35), together with the electrically non-conductive housing (36) of the first ion transfer cell (31), form a central channel (37) and two galvanically isolated outer channels (38) and (39).

[0160] The liquid mixture (41.1) to be depleted of ions is introduced into the central channel (37) of the first-type ion transfer cell (31) at an excess temperature set in the external heating device (32). The similar mixture (41.2 and 41.3) to be enriched in ions is passed through the two outer channels (38) and (39) at half the amount of (41.2) and (41.3) without increasing the temperature. The mixture to be depleted (41.1) is preferably passed through the first-type ion transfer cell (31) in countercurrent to the divided partial mixture streams (41.2) and (41.3) to be enriched.

[0161] The two partially enriched streams (42.1) and (42.2) are combined after leaving the first type ion transfer cell to form the ion-neutral concentrate stream (42) and are then discharged. The depleted product (43) is, for example, ultrapure water. The enriched product (42) can be used, for example, as in Fig.4 can also be a saturated saline solution. The pump (33) conveys the entire saline feed stream (40) through the TGD mixture separation device (30).

[0162] With parallel-connected TGD cells, for example, in a TGD battery arrangement, the complementary ions can be transferred in an ion-neutral manner in the battery's intermediate chambers, with the exception of the two outer enrichment chambers, i.e., with significantly lower galvanic countervoltage. The excess temperature required for ion transfer in the ion-neutral intermediate chambers is reduced by half compared to the excess temperature in the two outer chambers. In a ring-shaped arrangement of several first-order ion transfer cells, the driving excess temperature thus minimizes the separation effort.

[0163] Fig.Figure 4 shows a TGD separation cascade consisting of four individual cells of the first type ion transfer cells 50.1 to 50.4, for example, for the desalination of seawater with any initial salinity (51.x) and the products drinking water or ultrapure water (52.0) and saturated brine (53.0) for industrial processing. This TGD separation cascade does not discharge any enriched salt solution back into the sea. This makes this TGD plant type particularly valuable not only economically but also from a marine ecological perspective. The TGD individual cells (50.1) to (50.4) operate uniformly with the TGD separation principle of the Fig. 3.

[0164] Particularly advantageous and effective is the Fig. 4 shows the flow of the salt solution streams to be enriched and depleted in the individual TGD separation stages through the TGD separation cascade.

[0165] In the ion transfer cells of the separation cascade, the flow rates of the solution streams are balanced. The flow rates decrease gradually toward the staged salinity increase and increase gradually toward the staged desalination, with the salinity changes being equal in all separation stages. In each TGD separation stage, the respective ion-releasing solution stream is first heated in an associated external heating device (51.1) to (51.4) for directed ion displacement.

[0166] The TGD separation cascade requires only 1.2 kWh of heat to produce 1000 l of ultrapure water from 3% seawater while simultaneously producing industrially usable brine with a salt content of 15%.

[0167] By using a double-acting compression heat pump, which simultaneously cools the ion-absorbing brine and heats the ion-releasing brine to create the excess temperature, the electrical energy requirement of the separation process drops to 47 Wh el / m 3 Ultrapure water. In both cases, the additional electrical pump energy consumption is 200 Wh el . / m 3 Ultrapure water.

[0168] With the TGD cascade principle according to Fig. 4, among other things, alcohols can be concentrated from aqueous electrolytic solution to ultrapure alcohol at low temperatures, or rare elements that occur in low concentrations in seawater can be extracted with little heat, or diluted acids and bases can be concentrated. Table 1: Gibbs energy conversions of the TGEW process according to Fig. 1 and Fig. 2 Reaction cell NaCl - H2O Educt stream1 rich solution X1r Product stream 1 poor solution X1a Product stream 2.1 * Product stream 2.2* Gibbs energy conversion kJ / kg NaCl Component m%·m% 4.5NaCl / 95.5H2O 4.0 NaCl / 96.0 H2O N / a Cl2 Amount of substance m, kg -191 +190 + 0,39337 + 0,60663 Temperature t, °C 75 0 25 25 Enthalpy H, kJ / kg -15268,17 -15510,12 0 0 Reaction enthalpy G, kJ / kg - 12466,91 - 12924,49 - 667,0 - 558.9 Entropy S(T) = T· s, kJ / kg -2801,26 - 2585,63 + 667,0 + 558.9 Φ(H) = m · H, kJ +2916220,47 - 2946922,8 0 0 ΔH: - 30,702.33 ΦlG) = m · G, kJ +2381179,81 - 2455653,1 -.262,37 - 568,93 ΔG: - 75,304.59 Φ(S(T)) = m · S(T), kJ + 535040,66 - 491269,7 +262,37 + 568,93 ΔT·S: + 44,602.26 Cell voltage ΔU, V ΔU (-½ΔG): 11.4 V *based on 1.0 kg NaCl conversion with f Lӧsung = (1-Xa) / (Xr-Xa) ; X r: 4.5% and Xa 4.0%, Reaction processes ΔU (ΔG) = ½ΔG M / F z at the positive pole: at the negative pole: F: 96,485.3 As / mol 2 Cl - → Cl2+ 2 and - 2 H2O + 2e - → H2+ 2 OH - M NaCl : 58,44 g / mol 2 H2O → O2+ 4H + + 4e - Na + +e - → Na z = 2 Table 2.1: Gibbs energy balance of non-isothermal-isobaric TGD water desalination according to Fig. 3 Residual salt content: 0 ppm TGD ion transfer cell Educt partial stream 1 rich solution X1r Educt partial stream 2 poor solution, X2a Product stream 1 ultrapure water, X1a Product stream 2 concentrate solution, X2r Gibbs energy conversion kJ / kg NaCl NaCl concentration X, m-% 2,0 2,0 0.0 ppm residual salt content 4,0 Amount of substance* m, kg f1 = -50,00 f2-1 = -48,00 f1-1 = +49,00 f2 = +49,00 Temperature t, °C + 25,4 + 25,0 + 25,2 + 24,765 Enthalpy h, kJ / kg - 15686,26 - 15687,90 - 15865,05 -15511,05 Reaction enthalpy g, kJ / kg - 13042,03 - 13045,56 - 13162,87 - 12926,62 Entropy T s, kJ / kg - 2644,23 - 2642,34 - 2702,18 - 2584,43 m h, kJ + 784313,0 + 753019,2 - 777387,45 - 760041,45 ΔH - 96.70 m · g, kJ + 652101,5 + 626186,88 - 644980,63 - 633404,38 ΔG - 96.63 m · T · s, kJ +132211,5 +126832,32 - 132406,82 - 126637,07 Δ (T · s) -0.07 * based on 1.0 kg Na + Cl - -Displacement, f = (1-Xa) / (Xr-Xa) Useful energy consumption related to the ultrapure water output: 0.548 kWh / m 3 thermal, thermogalvanic working voltage ΔU: 58.2 mV Table 2.2: Gibbs energy balance of isothermal-isobaric EGD water desalination according to the state of the art Residual salt content: 0 ppm EGD - ion transfer cell Educt partial stream 1 rich solution X1r Educt partial stream 2 poor solution, X2a Product stream 1 water, X1a Product stream 2 concentrate solution, X2r Gibbs energy conversion kJ / kg NaCl NaCl concentration X, m-% 2,0 2,0 0.0 ppm residual salt content 4,0 Amount of substance* m, kg f1= -50,00 f2-1 = -48,00 f1-1 = +49,00 f2 = +49,00 Temperature t, °C + 25,0 + 25,0 + 25,0 + 25,0 Enthalpy h, kJ / kg - 15687,9 - 15687,9 -15865,89 - 15510,12 Reaction enthalpy g, kJ / kg - 13045,56 - 13045,56 - 13164,65 - 12924,49 Entropy T s, kJ / kg - 2642,34 - 2642,34 - 2701,24 - 2585,63 m h, kJ + 784395,00 + 753019,20 - 777428,61 - 759995,88 ΔH - 10.29 m·g,kJ + 652278,00 + 626186,88 - 645067,85 - 633300,01 ΔG + 97.02 m · T · s,kJ +132117,00 +126832,32 -132360,76 - 126695,87 Δ (T · s) - 107.31 * based on 1.0 kg NaCl shift, f = (1-Xa) / (Xr-Xa) Useful energy consumption related to the ultrapure water output: 0.608 kWh el / m 3 , electrogalvanic working voltage ΔU: 58.4mV List of reference symbols for Fig. 1 (TGEW cycle) U electrolytic solution circulation ① - ⑩ Process steps in solution circulation To upper process temperature Tu lower process temperature Tm average process temperature X La Concentration ion-neutral low solution X Lr Concentration ion-neutral rich solution + ΣH2 product stream hydrogen + ΣO2 product stream oxygen - ΣH2O reactant stream water

[0169] * ion-neutral means stoichiometrically balanced charge proportions of anions and cations in the electrolytic solution. List of reference symbols for Fig. 2 (TGEW process arrangement) 10 2. Art ion transfer cell 10.1 Cation depletion chamber 10.2 Cation enrichment chamber 11 3. Art ion neutralization cell 11.1 Anion neutralization chamber (O2) 11.2 Cation neutralization chamber (H2) 12 Liquid electrolyte circulation 13 Cation or proton permeable membrane 14 Cathode 15 Anode 16 electrically non-conductive, impermeable partition 17 Positive pole 18 Negative pole 19 Solution circulation pump 20 ion-neutral rich electrolyte solution 20.1 anion-excess solution 20.2 cation-excess solution 20.3 ion-neutral solution 1 arm 20.4 ion-neutral solution 2 arm 21.1 to 21.4 Heating device 22 Product stream molecular oxygen 23 Product stream molecular hydrogen 24 Educt stream water 25.1 Gas separator for O2 25.2 Gas separator for H2 26 electrical load resistance 27.1 Electrical connection lines of the cell anodes 27.2 Electrical connection of the cell cathodes List of reference symbols for Fig. 3 (TGD separation process with 1st type ion transfer cell) 31 Dialyzer housing anode side 32 Preheater desalination solution 33 Feed pump 34 anion-permeable membrane 35 cation-permeable membrane 36 Dialyzer housing cathode side 37 Desalination Canal 38 Cation enrichment channel 39 Anion enrichment channel 40 ion-neutral seawater inlet stream 41.1 Heated ion-neutral* seawater stream to be desalinated 41.2 Ion-neutral seawater partial stream for anion enrichment 41.3 Ion-neutral seawater partial stream for cation enrichment 42 ion-neutral salted concentrate effluent 42.1 anion-enriched concentrate effluent 42.2 cation-enriched concentrate effluent 43 ion-neutral desalinated drinking water effluent * The ion-neutral galvanic voltage is only concentration-dependent List of reference symbols for Fig. 4 (TGD separation cascade) 50 4-stage separation cascade 50.1 Separation stage 1 50.2 Separation stage 2 50.3 Separation stage 3 50.4 Separation stage 4 51.x ion-neutral* seawater influent stream with salinity x 51.1 Preheat exchanger for ion-releasing salt solution stage 1 51.2 Preheat exchanger for ion-releasing salt solution stage 2 51.3 Preheat exchanger for ion-releasing salt solution stage 3 51.4 Preheat exchanger for ion-releasing salt solution stage 4 52 ion-neutral desalinated drinking water effluent stream stage 1 52.1 preheated, ion-releasing brine feed stream stage 1 52.2 preheated, ion-releasing brine feed stream stage 2 52.3 preheated, ion-releasing brine feed stream stage 3 52.4 preheated, ion-releasing brine feed stream stage 4 53.0 ion-neutral, salt-enriched solution effluent stream stage 4 53.1 ion-neutral, salt-absorbing solution feed stream stage 1 53.2 ion-neutral, salt-absorbing solution feed stream stage 2 53.3 ion-neutral, salt-absorbing solution feed stream stage 3 53.4 ion-neutral, salt-absorbing solution feed stream stage 4 54.2 ion-neutral, partially demineralized solution effluent stream stage 2 54.3 ion-neutral partially demineralized solution effluent stream stage 3 54.4 ion-neutral, partially demineralized solution effluent stream stage 4 55.1 Desalination chamber stage 1 55.2 Desalination chamber stage 2 55.3 Desalination chamber stage 3 55.4 Desalination chamber stage 4 56.1 Cation enrichment chamber stage 1 56.2 Cation enrichment chamber stage 2 56.3 Cation enrichment chamber stage 3 56.4 Cation enrichment chamber stage 4 57.1 Anion enrichment chamber stage 1 57.2 Anion enrichment chamber stage 2 57.3 Anion enrichment chamber stage 3 57.4 Anion enrichment chamber stage 4 QUOTES CONTAINED IN THE DESCRIPTION

[0000] This list of documents submitted by the applicant was generated automatically and is included solely for the convenience of the reader. This list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions. Cited patent literature

[0000] DE 10 2022 000 982.5

[0017] DE 10 2016 014415A1 [0018, 0038, 0044, 0052, 0072, 0087, 0092, 0100, 0102]

Claims

[1] Thermogalvanic overtemperature effect as a driving force for a directed ion transfer between two electrolytic solution streams in ion exchange characterized by , that the solution streams are passed in cocurrent or countercurrent through a non-isothermal-isobaric ion transfer cell, that, under the influence of the galvanic overtemperature effect, the ion-releasing solution stream has a higher temperature than the ion-absorbing solution stream and, that the ion transfer between the solution streams is carried out in an ion transfer cell with no or one or two or more selectively ion-permeable membranes and one or both ion types are transferred. [2] Thermogalvanic overtemperature effect according to claim 1 characterized by , that the thermogalvanic overtemperature effect in a flow-through 1st kind ion transfer cell carries out a non-isothermal-isobaric complementary, neutral ion transfer, that the 1st type ion transfer cell contains at least one selectively cation-permeable membrane and one selectively anion-permeable membrane, that both solution streams are guided in opposite directions through this 1st type ion transfer cell, so that a galvanic voltage in the mV range is established between the ion-neutral solution currents without electron flow, or that the thermogalvanic overtemperature effect in a flow-through 2nd kind ion transfer cell carries out an activity-increasing non-isothermal-isobaric selective ion transfer, that this 2nd species ion transfer cell contains only one ion species permeable membrane, for example a preferred proton permeable membrane, so that activity-enhancing preponderance protons accumulate in the ion-absorbing solution and activity-enhancing preponderance hydroxide ions accumulate in the proton-releasing solution, that the flow channels of this second type ion transfer cell contain electrodes and that the solution streams pass in the same direction through the 2nd species ion transfer cell, so that a galvanic voltage in the volt range or higher is established between the chemically active solution currents without electron flow, or that the thermogalvanic overtemperature effect in a third kind ion transfer cell carries out an activity-reducing neutralization of excess ions, that the flow channels of this third type ion transfer cell also contain electrodes and instead of a membrane there is an ion and electron impermeable partition between the solution streams, that the activated solution streams are guided in the same direction through the 3rd kind ion transfer cell and that the electrodes of the 3rd type ion transfer cell are electrically short-circuited via an external payload resistor for potential equalization. [3] Multiple use of the overtemperature effect in a TGEW process combination of 2nd type ion transfer cell and 3rd type ion transfer cell according to claim 1 and claim 2, characterized by , that the electrodes of the 2nd Art ion transfer cell are connected to the electrodes of the 3rd Art ion transfer cell, so that the solution stream with the predominant cations, for example the predominant protons, is assigned to the cathode and the predominant anions, for example the predominant hydroxide ions, are assigned to the anode. that the solution streams in the circuit are guided through the two 2nd Art and 3rd Art ion transfer cells, that the 2nd type ion transfer cell sets a galvanic voltage by using a 1st overtemperature effect and which in the 3rd kind ion transfer cell by using a 2nd over-temperature effect with the release of electrical energy, the neutralization of the excess ions is carried out, that the neutralization products hydrogen and oxygen are removed from the solution circulation and the used water component is added to the circulating solution and the potential-equalizing electrons release electrical energy to a payload resistor. [4] non-isothermal-isobaric ion-neutral ion transfer carried out in a TGD ion transfer cell of the 1st type according to claim 1 and claim 2 characterized by , that the galvanic voltage difference built up by the excess temperature at values below the ion neutralization voltage of the electrolytic mixture components in a TGD ion transfer cell according to Fig. 3, without electron flow and consequently without electrodes in an electrically non-conductive cell housing for separating liquid mixtures, wherein said TGD ion transfer cell contains at least two selectively ion-permeable membranes, a cation-permeable membrane and an anion-permeable membrane and the ion-depleting solution stream with a constant temperature difference is preferably passed through the TGD cell in countercurrent to the ion-enriching solution stream. [5] TGEW power generator or TGEW hydrogen generator according to claim 3 characterized by that one of the generated combination products contains the ion-enriched working fluid (x - r ; y + r ) and the generator thus produces either hydrogen or electrical energy solely from ambient heat. [6] TGEW cycle process according to one of claims 3 or 5 characterized by that the ion-transferring electrolytic working fluid is any ion-containing electrolytic solution, for example an aqueous ammonia solution or an aqueous sodium chloride solution or an aqueous alkali metal hydroxide solution or an alkali metal ammonia solution or an alkali metal alcohol solution or an acid diluted with water. [7] Formation and use of the non-isothermal-isobaric ion transfer according to claims 1, 2 and 4 to a thermally driven dialysis device (TGD process), for example for the production of drinking water or ultrapure water from saline waters, characterized by , that according to Fig. 3 the flow-through TGD ion transfer cell of the first type (31) contains two surface membranes (34) and (35), a selectively anion-permeable membrane (34) and a selectively cation-permeable membrane (35), which together with the cell housing (36) in the TGD ion transfer cell (31) form three chambers (37), (38) and (39) through which the working medium flows (41.1), (41.2) and (41.3) flow; a cation-absorbing outer chamber (38), an anion-absorbing outer chamber (39) and, between the two outer chambers (38) and (39), a middle chamber (37) releasing anions and cations, and the pump (33) conveys saline starting water (40) through the TGD ion transfer cell (31), wherein the two outer chambers (38) and (39) are each flowed through by an equal portion of the saline starting water (41.2) and (41.3) and the middle chamber (37) is flowed through by a portion of the starting salt water (41.1) corresponding to the two portions (41.2) and (41.3) and heated in the external heating device (32), so that both types of ions from the heated partial flow (41.1) of the middle chamber (37) change into the outer chambers (38) and (39) and as a result a salt solution (42) with twice the salt content flows out of the two outer chambers (38) and (39) and almost salt-free drinking water or ultrapure water (43) flows out of the middle chamber (37). [8] Formation of the TGD process according to claim 7 into a TGD separation cascade characterized by , that according to Fig.4 several similar TGD ion transfer cells of the first type (50.1), (50.2), (50.3) and (50.4) are connected in series on the salt water side and the salt-depleting salt water solutions (52.1), (52.2), (53.3) and (52.4) heated externally in the heating devices (51.1), (51.2), (51.3) and (51.4) are fed from TGD ion transfer cell to TGD ion transfer cell in the opposite direction to the salt-absorbing salt water solutions (53.1), (53.2), (53.3) and (53.4), so that the desalination rate (± ΔX) in the individual TGD ion transfer cells is kept constant, wherein the middle chambers (55.1), (55.2), (55.3) and (55.4) of the serially flowing TGD ion transfer cell are each supplied with externally heated salt water (52.1), (52.2), (52.3) and (52.4) with gradually increasing salt contents and gradually decreasing quantities from cell to cell, and unheated salt water quantities (53.1) to (53.4) flow towards these salt-depleting solutions in the associated outer chambers (56.1) to (56.4) and (57.1) to (57.4) with each adapted flow rate and equivalent inlet salt content, so that from the middle chamber (55.1) of the first TGD ion transfer cell (50.1) ultrapure water (52.0) flows out and from the outer chambers (56.4) and (57.4) of the last TGD ion transfer cell (50.4) highly enriched salt water (53.0), for example brine with a salt content concentrated to saturation and the depleted salt solution (54.4) flowing out of the middle chamber (55.4) of the last TGD ion transfer cell (50.4) is returned with a gradually increasing amount and gradually decreasing salt content through the individual middle chambers (55.3), (55.2) to the middle chamber (55.1) of the first TGD cell (50.1), and the return flow (54.2) is introduced together with fresh salt water (51.x) as a quantity-adjusted heated inflow (52.1) into the middle chamber (55.1) of the first TGD ion transfer cell (50.1), and the demineralized flow flows out of the first TGD middle chamber (55.1) as drinking or ultrapure water (52.0), so that the flow balance of the serially flowed TGD ion transfer cells (50.1), (50.2), (50.3) and (50.4) is balanced in the cells and in the cascade and only the amount of initial salt water (51.x) is introduced into the process arrangement, which flows out of the TGD cascade arrangement as saturated brine (53.0) and as ultrapure water (52.0). [9] Heating device for producing and activating the thermogalvanic overtemperature effect for the TGD process according to claims 4, 7 and 8 characterized by , that the potentially ion-depleting solution stream is heated and / or the potentially ion-enriching solution stream is cooled and that a double-acting compression heat pump is used to create the excess temperature effect, which on the one hand cools the ion-absorbing solution stream and on the other hand heats the ion-releasing solution stream with its waste heat.

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