TECHNICAL FIELD

The present invention relates to a method for transferring heat between two independent process, in particular for transferring heat from a chemical conversion process, from a physicochemical process, from ambient heat, or from a combination of two or more thereof, to a target process in a chemical production plant.

INTRODUCTION

The provision of thermal energy for endothermic processes is currently done by burning fossil fuels or by direct electric heating. Fossil fuels are often preferred to direct electric heating because of lower efficiency and hence lower costs.

Heat pumps, by smart use of electrical energy in a thermodynamic cycle, achieve the raising of the temperature level of a quantity of heat much greater than the quantity of electrical energy used. For raising the temperature level according to a Carnot cycle, the coefficient of performance (COP) is calculated according to formula I:

£Carnot-WP ^— 1 /(1 -T|ow/Thigh) (I), wherein Ecamot-wp is the coefficient of performance of the Carnot cycle of the heat pump, T| _OW is the absolute temperature in Kelvin at which the heat is absorbed and Thigh is the absolute temperature at which the heat is released. The latter temperature must be at least equal to the temperature at which the process takes place that is to be heated.

Up to now, heat pumps have been used and designed to provide heat at a maximum temperature of about 150 °C. Many technically relevant processes require large amounts of heat at temperatures significantly above this value. Examples include the melting of metals, distillation processes and endothermic chemical reactions. For thermodynamic reasons, endothermic chemical reactions typically take place at high temperatures.

DE 2951188 A1 relates to a method for utilizing waste heat from endothermic processes wherein heat is initially supplied from an external heat source at a high temperature level and residual heat from the reaction is obtained at a low temperature level, wherein the low temperature residual heat is recycled to the endothermic reaction with the aid of a heat pump.

DE 3209642 A1 discloses a process heat generation plant for the joint generation of high-tem- perature heat and process steam. V. Singh et al. “Investigation of new mechanical heat pump systems for heat upgrading applications” in Int. J. Energy Ress. 2018, 42, 3078-3090 discloses examples of multistage ultrahigh- temperature heat pumps with different heat transfer media that can be used in process engineering processes, among other applications.

In the course of converting technical processes to sustainable energy sources, it is thus desirable to further increase the temperature levels achieved so far by heat pumps in order to reduce the dependency on other energy sources for processes requiring heat at high temperature levels.

For an endothermic reaction at 350 °C and a heat source at 30 °C, a theoretical COP of 1 .95 can thus still be achieved, and thus theoretically almost twice as much heat can be provided for the reaction than if the electric power used for operating the heat pump were used directly for heating. Typically, the COP is significantly lower at 1 .5, but the use of heat pumps can still be considered, e.g. if steam is no longer available for a process due to the temperature and pressure level, or is only available with extreme difficulty.

An important field of application for ultrahigh-temperature heat pumps is the valorization of thermal energy, which is already available at high temperatures, e.g. at about 300 °C. With regard to the theoretically possible efficiency (about COPcamot = 1/(1 -(773 K / 973 K)) = 4.5), these heat pumps are suitable for thermal utilization at much higher temperatures of over 600 °C.

Accordingly, it was the object of the present invention to provide a method in which the utilization of heat such as with the aid of heat pumps is not restricted to the optimization of individual heat consuming processes such as endothermic reactions, or to the increased valorization of primary energy sources and in particular of sustainable energy sources or nuclear power. In particular, it was the object of the present invention to utilize heat transfer concepts involving the valorization of heat not stemming from primary energy sources, and in particular involving the valorization of waste heat or of otherwise available low temperature heat.

DETAILED DESCRIPTION

Thus, it has surprisingly been found that heat sources at low temperature, e.g. 20 to 80 °C, can be used for upgrading them to usable thermal energy at a temperature of equal to or greater than 350 °C, preferably greater than 350 °C, more preferably greater than 375 °C, whereby a coefficient of performance (COP) of greater than 1 can be achieved. In particular, it has unexpectedly been found that the use of heat pump cascades are particularly advantageous for achieving energetic efficiencies and reducing the dependency from primary energy sources, whether they be sustainable or not. Accordingly, with the appropriate choice of heat transfer media, upgrading of heat sources is possible to directly supply heat to processes at temperatures of equal to or greater than 350 °C, preferably greater than 350 °C, more preferably 375 to 1 ,275 °C, e.g. by superheated saturated steam, to provide the necessary temperatures in a target process. In particular, it has been found that the use of high temperature heat pumps allows electrification of processes where electrical heating is difficult to realize, and especially with a better electrical efficiency COP _reai of greater than 1 .

The inventive method is particularly advantageous if, within a production plant, there is an exothermic heat source at low temperature and an endothermic heat sink at higher temperature. In this regard, it is advantageous to use heat pumps for high-temperature applications (> 200 °C). The compressor/compressor cascades and heat transfer media used are accordingly adapted to the high temperatures. In addition to mercury, tetraphenyl-compounds are also a possible heat transfer medium for realizing the inventive results. Further, some metals are suitable as a heat transfer medium for applications above 1 ,000 °C at the maximum temperatures.

Apart from the leverage effect due to a COP > 1 , the use of heat pumps can also be considered if the reaction temperature is too high to achieve a real COP > 1. This is the case when conventional heating concepts become problematic due to the high temperatures and high power required (for example due to very high currents at relatively low voltages of a resistive heater) or the use of regular process steam is no longer possible > 290 °C. The compressors used in a heat pump can be operated at medium or high voltage, thus avoiding the electrical infrastructure, transformation losses and high currents. In contrast, the conventional use of electric heaters at very high temperatures often requires the concept of indirect heating, where heat is transferred from the electric heater to the process via radiation. This often leads to inhomogeneous temperature profiles and also increased equipment requirements.

If an apparatus needs to be cooled over a wide temperature range of AT above 50 °C and is thus available as a heat source (for example cooled from about 350 °C to 250 °C), two-stage heat pumps using the same working fluid are advantageous in terms of electrical efficiency, since there is then no need to depressurize the hotter circuit to a lower temperature and pressure level. In this case, the heat source is tapped at two different temperature levels (approximately 350 °C to 300 °C and 300 °C to 250 °C). Three-stage processes are also conceivable, although this increases the complexity of the system.

The inventive method is not limited to endothermic reactions. Often, exothermic reactions are followed by energy-intensive separation steps/distillations, which in turn can benefit from the inventive method, even when using the waste heat from the preceding reaction as a heat source. In these cases, the high-temperature heat pump may also act as a high-temperature heat reservoir.

Therefore, the present invention relates to a method for transferring heat to a target process in a chemical production plant, the method comprising:

(i) providing a first process stream (1 ) having a temperature T 1 ;

(ii) transferring heat from a chemical conversion process, from a physicochemical process, or from ambient heat, or from a combination of two or more thereof, to the first process stream provided in (i), for obtaining a heated first process stream (3) having a temperature T2, wherein T2 > T1 ;

(iii) conducting the target process with the heated first process stream obtained in (ii); wherein the target process is different from the chemical conversion process, from the physicochemical process, or from the combination of the chemical conversion process and the physicochemical process from which heat is transferred according to (ii).

Within the meaning of the present invention, the term „different“ with regard to the chemical conversion process and/or the physicochemical process in (ii) being different from the target process indicates that the inventive method does not recycle heat to a chemical conversion process and/or to a physicochemical process. Thus, although according to particular embodiments or the inventive method, the chemical conversion process and/or the physicochemical process in (ii) may be the same as the target process, they are not identical in the sense that heat stemming from a specific chemical conversion process and/or physicochemical process may be recycled to the same chemical conversion process and/or physicochemical process in a different process, but not to the chemical conversion process and/or physicochemical process from which it stems. According to the present invention, it is however preferred that according to particular and preferred embodiments of the present invention, wherein the target process is a chemical conversion process and/or a physicochemical process, the chemical conversion process and/or the physicochemical process in (ii) is not the same chemical conversion process and/or physicochemical process of the target process.

It is preferred that heat is transferred in (ii) from a chemical conversion process and/or from a physicochemical process, and wherein the heat which is transferred according to (ii) is obtained from an exothermic reaction or wherein the heat which is transferred according to (ii) is excess heat of the heat employed for performing an autothermal reaction or an endothermic reaction.

In the case where heat is transferred in (ii) from a chemical conversion process and/or from a physicochemical process, and wherein the heat which is transferred according to (ii) is obtained from an exothermic reaction or wherein the heat which is transferred according to (ii) is excess heat of the heat employed for performing an autothermal reaction or an endothermic reaction, it is preferred according to a first alternative that the exothermic reaction comprises one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and selective oxidation of one or more of alkanes, alkenes and alkynes, preferably selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid.

Further in the case where heat is transferred in (ii) from a chemical conversion process and/or from a physicochemical process, and wherein the heat which is transferred according to (ii) is obtained from an exothermic reaction or wherein the heat which is transferred according to (ii) is excess heat of the heat employed for performing an autothermal reaction or an endothermic reaction, it is preferred according to a second alternative that the endothermic reaction comprises one or more of steam cracking, ethane dehydrogenation, propane dehydrogenation, butane dehydrogenation, steam reforming, dry reforming , styrene production, methanol reforming, dimethyl ether reforming, reverse water-gas shift, alcohol dehydration, and NH3 reforming.

Further in the case where heat is transferred in (ii) from a chemical conversion process and/or from a physicochemical process, and wherein the heat which is transferred according to (ii) is obtained from an exothermic reaction or wherein the heat which is transferred according to (ii) is excess heat of the heat employed for performing an autothermal reaction or an endothermic reaction, it is preferred according to a third alternative that the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, wherein the hydrocarbons are selected from the group consisting of (C1-C10)alkanes, more preferably (C1-C8)alkanes, more preferably (C1- C7)alkanes.

It is preferred that the physicochemical process comprises, preferably consists of, one or more of a vapor-compression evaporation, and a chemisorption process.

It is preferred that the ambient heat which is transferred according to (ii) is heat from the environment, preferably heat from one or more or air, water, and solar radiation, including combinations of two or more thereof.

It is preferred that the heat transferred according to (ii) does not comprise energy from nuclear fission, solar thermal energy, geothermal energy, hydro energy, and wind energy.

Thus, the process according to the present invention does not relate to an optimization of a single process with respect to its energy-efficiency. In particular the present invention does not relate to a process wherein energy is recycled therein, especially for optimizing the energy conversion efficiency. Further, the process of the present invention does not relate to a process wherein the energy for transferring heat originates from a pure energy source.

It is preferred that transferring heat in (ii) comprises use of a heat pump, wherein the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemisorption heat pump.

In the case where transferring heat in (ii) comprises use of a heat pump, wherein the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemisorption heat pump, it is preferred that the absorption heat pump is a conventional heat pump (type I heat pump), a heat transformer heat pump (type II heat pump), or an adsorption heat pump, wherein the absorption heat pump is preferably a conventional heat pump.

In the case where the absorption heat pump is a conventional heat pump (type I heat pump), a heat transformer heat pump (type II heat pump), or an adsorption heat pump, it is preferred that the adsorption heat pump comprises and adsorbent, wherein the adsorbent comprises, preferably consists of, one or more of activated carbon, zeolites, and mixtures thereof.

It is preferred that the target process comprises, preferably consists of, the heating of one or more compounds, wherein preferably the target process comprises, preferably consists of, a chemical conversion process and/or a thermal separation of compounds, wherein more preferably the target process comprises one or more of a chemical reaction, an evaporation, a preheating step, and a crystallization process, including combinations of two or more thereof, wherein more preferably the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, wherein the target process preferably comprises, preferably consists of, an endothermic reaction.

In the case where the target process comprises, preferably consists of, the heating of one or more compounds, wherein preferably the target process comprises, preferably consists of, a chemical conversion process and/or a thermal separation of compounds, it is preferred that the thermal separation of compounds comprises, preferably consists of, the isolation of isobutene from a mixture comprising n-butene, 2-butene and isobutene, preferably by distillation.

In the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, one or more of cracking, preferably catalytic cracking, dehydrogenation, styrene production, reverse water- gas shift, dehydration, thermal decomposition, dimerization, oligomerization, gamma-butyrolac- tone synthesis, and reforming, wherein cracking more preferably comprises cracking of one or more of steam, hydrocarbons, aliphatics, alkenes, preferably one or more of ethylene, propylene, and butylenes, dienes, preferably butadiene, acetylenes, cycloaliphatics, naphtha, polymers, plastics, biomass, oleaginous liquids, bitumen, tar ureas, carbamates, preferably carbamates to olefins, aromatics, fuels, isocyanates, melamine, and diamines, wherein dehydrogenation more preferably comprises dehydrogenation of one or more of hydrocarbons, more preferably of one or more of ethane, propane, butanes, pentanes, hexanes, preferably hexanes to olefins, alkenes (ethylene, propylene, butylenes), dienes (butadiene), and acetylenes, aliphatics, cycloaliphatics, naphtha, ethylbenzene, aromatics and styrene, wherein dehydration more preferably comprises dehydration of one or more of alcohols, preferably one or more of ethanol, bioethanol, propanol, and butanols, more preferably dehydration of alcohols to alkenes, preferably one or more of ethylene, propylene, and butylenes, wherein thermal decomposition comprises one or more of pyrolysis, thermolysis, gasification, more preferably thermal decomposition of one or more of polymers, plastics, biomasses, wastes, oil-containing liquids, bitumen, tar to olefins, alkenes, preferably one or more of ethylene, propylene and butylene, dienes, preferably butadiene, acetylenes, monomers, aromatics, fuels and synthesis gas, wherein one or more of dimerization and oligomerization comprises dimerization or oligomerization of alkenes, preferably of one or more of ethylene, butylenes and hexenes, more preferably to di- or oligoalkenes, wherein reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, production of syngas, and NH3 reforming, wherein the endothermic reaction more preferably comprises, more preferably consists of, NH3 reforming.

Further in the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, dehydration of ethanol, and wherein the chemical process from which heat is transferred in (ii) comprises production of ethylene oxide, preferably from ethylene.

Further in the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, steam methane reforming, wherein steam methane reforming is preferably performed at 700 to 1100 °C, more preferably steam methane reforming to syngas comprising CO and hydrogen.

Further in the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, steam cracking, wherein steam cracking is preferably performed at about 850 to about 900 °C, more preferably steam cracking of naphtha to olefins, methane, and hydrogen.

Further in the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the exothermic reaction comprises, preferably consists of, one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and selective oxidation of one or more of alkanes, alkenes and alkynes, preferably selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid.

Further in the case where the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, wherein the hydrocarbons are selected from the group consisting of (Ci-Cio)alkanes, more preferably (Ci-Cs)alkanes, more preferably (Ci-Cy)alkanes. It is preferred that T1 is in the range of from 20 to 1 ,150 °C, more preferably in the range of from 80 to 1 ,100 °C, more preferably in the range of from 200 to 1 ,000 °C, more preferably in the range of from 400 to 800 °C, more preferably in the range of from 500 to 600 °C.

It is preferred that T2 is in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1175 °C, more preferably in the range of from 550 to 1 ,075 °C.

It is preferred that the first process stream provided in (i) has a pressure in the range of from 1 to 300 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

It is preferred that the first process stream provided in (i) has a weight hourly space velocity in the range of from 200 to 20,000 IT ¹ , more preferably in the range of from 400 to 15,000 IT ¹ , more preferably from 600 to 10,000 IT ¹ , more preferably from 1 ,000 to 5,000 IT ¹ .

It is preferred that transferring heat in (ii) comprises:

(ii.a) providing heat from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature T3;

(ii.b) transferring the heat provided in (ii.a) to the first process stream (1 ) provided in (i), for obtaining a heated first process stream (3) having a temperature T2; wherein T3 < T1 , and wherein T3 is more preferably in the range of from 255 °C to 700 °C.

In the case where the method comprises (ii.a) and (ii.b), it is preferred that the heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and/or from a physicochemical process, wherein the process stream from a chemical conversion process and/or from a physicochemical process preferably comprises one or more of steam, flue gas, more preferably flue gas from a steam generation process.

Further in the case where the method comprises (ii.a) and (ii.b), it is preferred that transferring of heat according to (ii.b) is conducted using a heat exchanger (2), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

Further in the case where the method comprises (ii.a) and (ii.b), it is preferred that the target process comprises NH3 reforming, and wherein transferring heat according to (ii.b) comprises at least partially converting NH3 to H2 and N2. Further in the case where the method comprises (ii.a) and (ii.b), it is preferred that the heated first process stream obtained in (ii.b) has a temperature T2, wherein T2 is more preferably in the range of from 350 to 1 ,225 °C, more preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

Further in the case where the method comprises (ii.a) and (ii.b), it is preferred that the heated first process stream obtained in (ii.b) has a pressure in the range of from 0.01 to 300 bar(abs), more preferably in the range of from 1 to 275 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

It is preferred that transferring heat in (ii) comprises:

(11.1 ) providing heat (4) from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature T3, wherein T3 is in the range of from 255 °C to 700 °C;

(11.2) providing a stream (10) comprising a heat transfer medium, wherein the stream (10) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 250 °C;

(11.3) transferring the heat (4) provided in (ii.1 ) to the stream (10) provided in (ii.2), for obtaining a heated stream (11 ) ;

(11.4) increasing the pressure of the heated stream (11 ) obtained in (ii.3), for obtaining a compressed heated stream (7) having a temperature in the range of from 400 °C to 1 ,400 °C;

(11.5) transferring heat from the compressed heated stream (7) obtained in (ii.4) to the first process stream (1 ) provided in (i), for obtaining a heated first process stream (3) having a temperature T2 and a compressed stream (8).

In the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), it is preferred that the method further comprises

(11.6) expanding the compressed stream (8) obtained in (ii.5);

(11.7) optionally recycling at least a portion of the stream obtained in (ii.6) to (ii.2).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heat transfer medium is selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropro- pene, hydrofluorocarbons, preferably hydrofluoroolefins, more preferably one or more of (Z)-1- Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, hydrocarbons, preferably one or more of butane, pentane, and hexane, ammonia, water, carbon dioxide, nitrogen, oxygen, air, noble gases, preferably one or more of helium, neon, argon, krypton, and xenon, tetraphenyl-compounds, and mixtures of two or more thereof. Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the stream provided in (ii.2) has a temperature equal to or greater than 300 °C, more preferably in the range of from 300 °C to 1000 °C, more preferably in the range of from 350 °C to 850°C.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the stream provided in (ii.2) has a pressure in the range of from 0.1 bar(abs) to 50 bar(abs), more preferably in the range of from 0.5 bar(abs) to 30 bar(abs), more preferably in the range of from 1 bar(abs) to 20 bar(abs).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that from 95 to 100 Vol-%, more preferably from 99 to 100 Vol-%, more preferably from 99.9 to 100 Vol-%, of the stream provided in (ii.2) consist of the heat transfer medium.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heat transfer medium in the stream provided in (ii.2) is in the liquid state.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heat transfer medium in the stream provided in (ii.2) is a two-phase fluid with a vapor phase and a liquid phase.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heat transfer medium in the stream provided in (ii.2) is in the supercritical state.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that transferring the heat in (ii.3) is conducted using a heat exchanger (5), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heat provided in (ii.1 ) is obtained from a process stream from a chemical conversion process and/or from a physicochemical process, wherein the process stream from a chemical conversion process and/or from a physicochemical process preferably comprises one or more of steam, flue gas, preferably flue gas from a steam generation process. Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heated stream obtained in (ii.3) has a temperature in the range of from 200 °C to 700 °C, preferably in the range of from 250 °C to 650 °C, more preferably in the range of from 350 °C to 550 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heated stream obtained in (ii.3) is in the superheated vapor state.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heated stream obtained in (ii.3) is in the supercritical state.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that increasing the pressure of the stream according to (ii.4) is conducted using a compressor (12).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that increasing the pressure of the stream according to (ii.4) is conducted using a multi-stage compressor (12), the multi-stage compressor preferably comprising one or more working media, preferably one or two working media, wherein the two working media are chemically and/or physically different from each other.

In the case where increasing the pressure of the stream according to (ii.4) is conducted using a multi-stage compressor (12), it is preferred that the multi-stage compressor comprises one or more stages, wherein independently from one another each stage comprises a temperature elevation in the range of from 20 to 500 °C, more preferably in the range of from 50 to 200 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that increasing the pressure of the stream according to (ii.4) is conducted adiabatically.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that transferring of heat according to (ii.5) is conducted using a heat exchanger (2), wherein the heat exchanger more preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the target process comprises NHs reforming, and wherein transferring heat according to (ii.5) comprises at least partially converting NH3 to H2 and N2.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that according to (ii.5) a compressed stream is obtained having a temperature in the range of from 375 °C to 1 ,400 °C, more preferably in the range of from 475 °C to 1 ,100 °C, more preferably in the range of from 550 to 1 ,000 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that according to (ii.5) a compressed stream is obtained having a pressure in the range of from 1 to 300 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heated first process stream obtained in (ii.5) has a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the heated first process stream obtained in (ii.5) has a pressure in the range of from 0.01 to 300 bar(abs), more preferably in the range of from 1 to 275 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

Further in the case where transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that expanding according to (ii.6) is conducted using a thermal expansion valve (9) or an expansion turbine (9).

In the case where expanding according to (ii.6) is conducted using an expansion turbine (9), it is preferred that increasing the pressure of the stream according to (ii.4) is conducted using a compressor (12), wherein expanding is conducted using an expansion turbine, wherein the energy obtained from the expansion turbine, wherein the energy is more preferably obtained as electricity, is used to operate the compressor, or wherein the energy obtained from the expansion turbine is used to operate the compressor mechanically, more preferably via a shaft for directly transmitting the energy. Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the expanded stream obtained in (ii.6) has the same pressure and temperature as the stream comprising a heat transfer medium provided in (ii.2).

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that expanding the compressed stream according to (ii.6) is conducted adiabatically.

Further in the case where transferring heat in (ii) comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that from 1 to 100 vol-%, more preferably from 10 to 90 vol-%, more preferably from 30 to 70 vol-%, of the stream obtained in (ii.6) are recycled to (ii.2) according to (ii.7).

Further in the case where transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the stream obtained in (vii) is entirely recycled to (ii.2) according to (ii.7).

In the case where the stream obtained in (vii) is entirely recycled to (ii.2) according to (ii.7), it is preferred that steps (ii.2) to (ii.7) are conducted in a closed system in which the stream comprising a heat transfer medium is circulated.

It is preferred that the method, wherein the method preferably further comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor, for obtaining a first product stream.

In the case where the method further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor, for obtaining a first product stream, it is preferred that the heated first process stream obtained in (ii.5) is fed into the first reactor having a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

Further in the case where the method further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor, for obtaining a first product stream, it is preferred that the heated first process stream obtained in (ii.5) is fed into the first reactor having a gas hourly space velocity in the range of from 10 h’ ¹ to 50.000 IT ¹ , more preferably in the range of from 100 h’ ¹ to 20,000 IT ¹ , more preferably in the range of from 1 ,000 h’ ¹ to 10,000 IT ¹ .

Further in the case where the method further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor, for obtaining a first product stream, it is preferred that the method further comprises (iv) heating the first product stream obtained in (iii) to a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C, and feeding the heated first product stream into a second reactor for obtaining a second product stream.

In the case where the method further comprises (iv), it is preferred that heating the first product stream according to (iv) comprises transferring heat from the compressed stream obtained in (ii.4) to the first product stream obtained in (iii), for obtaining a heated first product stream, and a compressed stream having a temperature in the range of from 375 °C to 1 ,400 °C.

Further the case where the method further comprises (iv), it is preferred that the first and second reactor independently from one another is an adiabatic reactor, an isothermal reactor, or a combination thereof.

In the context of the present invention, an adiabatic or isothermal change of state is to be understood as a change of state effected close to the theoretical adiabatic or isothermal process.

Further the case where the method further comprises (iv), it is preferred that the first and second reactor independently from one another is a tubular reactor.

It is preferred that transferring heat in (ii) comprises:

(ii.1 ’) providing heat (4) from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature in the range of from 255 °C to 700 °C;

(ii.2’) providing a stream (10a) comprising a first heat transfer medium, wherein the stream (10a) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 250 °C;

(ii.3’) transferring heat from the heat (4) provided in (ii.1 ’) to the stream (10a) provided in (ii.2), for obtaining a heated stream (11a);

(ii.4’) increasing the pressure of the heated stream (11 a) obtained in (ii.3’), for obtaining a compressed heated stream (7a) having a temperature in the range of from 400 °C to 1 ,400 °C;

(ii.5’) providing a stream (10b) comprising a second heat transfer medium, wherein the stream (10b) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 275 °C;

(ii.6’) transferring heat from the compressed heated stream (7a) obtained in (ii.4’) to the stream (10b) provided in (ii.5’), for obtaining a heated stream (11 b) and a compressed stream (8a);

(ii.7’) expanding the compressed stream (8a) obtained in (ii.6’);

(ii.8’) recycling at least a portion of the stream obtained in (ii.7’) to (ii.2’)

(ii.9’) increasing the pressure of the heated stream (11 b) obtained in (ii.6’), for obtaining a compressed heated stream (7b) having a temperature in the range of from 400 °C to 1 ,400 °C;

(ii.1 O’) transferring heat from the compressed heated stream (7b) obtained in (ii.9’) to the first process stream (1 ) provided in (i), for obtaining a heated first process stream (3) having a temperature T2 and a compressed stream (8b); (ii.11 ’) expanding the compressed stream (8b) obtained in (ii.1 O’);

(ii.12’) recycling at least a portion of the stream obtained in (ii.11 ’) to (ii.5’).

In the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred that the first heat transfer medium in (ii.2’) and the second heat transfer medium in (ii.5’) are independently from one another selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably one or more of (Z)- 1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, hydrofluorocarbons, preferably hydrofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetra- fluoropropene and trans-1-chloro-3,3,3-trifluoropropene, hydrocarbons, preferably one or more of butane, pentane, and hexane, ammonia, water, carbon dioxide, nitrogen, oxygen, air, noble gases, preferably one or more of helium, neon, argon, krypton, and xenon, tetraphenyl-com- pounds, and mixtures of two or more thereof.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred that the stream (10a) provided in (ii.2’) has a temperature equal to or greater than 300 °C, more preferably in the range of from 300 °C to 1000 °C, more preferably in the range of from 350 °C to 850°C.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred that transferring the heat provided in (ii.1 ’) is conducted using a heat exchanger (5), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the heated stream obtained in (ii.3’) has a temperature in the range of from 350 °C to 950 °C, more preferably in the range of from 400 °C to 600 °C, more preferably in the range of from 450 °C to 550 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred increasing the pressure of the heated stream (11a) is conducted using a compressor (12a).

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the stream (10b) provided in (ii.5’) has a temperature equal to or greater than 325 °C, more preferably in the range of from 325 to 1 ,000 °C, more preferably in the range of from 375 to 850 °C, more preferably in the range of from 450 to 650 °C, more preferably in the range of from 500 to 600 °C. Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred transferring heat from the compressed heated stream (7a) is conducted using a heat exchanger (13), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred according to (ii.6’) a compressed stream (8a) is obtained having a temperature in the range of from 355 °C to 1 ,400 °C, more preferably in the range of from 455 °C to 655 °C, more preferably in the range of from 505 to 605 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the heated stream (11 b) obtained in (ii.6’) has a temperature in the range of from 350 °C to 1150 °C, more preferably in the range of from 450 °C to 650 °C, more preferably in the range of from 500 °C to 600 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred increasing the pressure of the heated stream (11 b) is conducted using a compressor (12b).

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred transferring heat from the compressed heated stream (7b) is conducted using a heat exchanger (2), wherein the heat exchanger more preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the heated first process stream obtained in (ii.1 O’) has a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred expanding according to (ii.7’) and (ii.11 ’) are independently from one another conducted using a thermal expansion valve (9a and/or 9b) or an expansion turbine (9a and/or 9b).

Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the heated first process stream obtained in (ii) is used as feed or co-feed for an endothermic reaction, preferably for a high temperature endothermic reaction. Further in the case where transferring heat in (ii) comprises (ii.1 ’), (ii.2’), (ii.3’), (ii.4’), (ii.5’), (ii.6’), (ii.7’), (ii.8’), (ii.9’), (ii.1 O’), (ii.11 ’), and (ii.12’), it is preferred the heated first process stream obtained in (ii) is used as feed stream for a NH3 reforming process.

The unit bar(abs) refers to an absolute pressure wherein 1 bar equals 10 ⁵ Pa.

The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The method of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The method of any one of embodiments 1 , 2, 3, and 4". Further, it is explicitly noted that the following set of embodiments is not the set of claims determining the extent of protection, but represents a suitably structured part of the description directed to general and preferred aspects of the present invention.

1 . A method for transferring heat to a target process in a chemical production plant, the method comprising:

(i) providing a first process stream (1 ) having a temperature T 1 ;

(ii) transferring heat from a chemical conversion process, from a physicochemical process, or from ambient heat, or from a combination of two or more thereof, to the first process stream provided in (i), for obtaining a heated first process stream (3) having a temperature T2, wherein T2 > T1 ;

(iii) conducting the target process with the heated first process stream obtained in (ii); wherein the target process is different from the chemical conversion process, from the physicochemical process, or from the combination of the chemical conversion process and the physicochemical process from which heat is transferred according to (ii).

2. The method of embodiment 1 , wherein heat is transferred in (ii) from a chemical conversion process and/or from a physicochemical process, and wherein the heat which is transferred according to (ii) is obtained from an exothermic reaction or wherein the heat which is transferred according to (ii) is excess heat of the heat employed for performing an autothermal reaction or an endothermic reaction.

3. The method of embodiment 2, wherein the exothermic reaction comprises one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and selective oxidation of one or more of alkanes, alkenes and alkynes, preferably selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid. 4. The method of embodiment 2, wherein the endothermic reaction comprises one or more of steam cracking, ethane dehydrogenation, propane dehydrogenation, butane dehydrogenation, steam reforming, dry reforming , styrene production, methanol reforming, dimethyl ether reforming, reverse water-gas shift, alcohol dehydration, and NH3 reforming.

5. The method of embodiment 2, wherein the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, wherein the hydrocarbons are selected from the group consisting of (C1-C10)alkanes, more preferably (C1-C8)alkanes, more preferably (C1-C7)alkanes.

6. The method of any one of embodiments 1 to 5, wherein the physicochemical process comprises, preferably consists of, one or more of a vapor-compression evaporation, and a chemisorption process.

7. The method of any one of embodiments 1 to 6, wherein the ambient heat which is transferred according to (ii) is heat from the environment, preferably heat from one or more or air, water, and solar radiation, including combinations of two or more thereof.

8. The method of any one of embodiments 1 to 7, wherein the heat transferred according to (ii) does not comprise energy from nuclear fission, solar thermal energy, geothermal energy, hydro energy, and wind energy.

9. The method of any one of embodiments 1 to 8, wherein transferring heat in (ii) comprises use of a heat pump, wherein the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemisorption heat pump.

10. The method of embodiment 9, wherein the absorption heat pump is a conventional heat pump (type I heat pump), a heat transformer heat pump (type II heat pump), or an adsorption heat pump, wherein the absorption heat pump is preferably a conventional heat pump.

11 . The method of embodiment 10, wherein the adsorption heat pump comprises and adsorbent, wherein the adsorbent comprises, preferably consists of, one or more of activated carbon, zeolites, and mixtures thereof.

12. The method of any one of embodiments 1 to 11 , wherein the target process comprises, preferably consists of, the heating of one or more compounds, wherein preferably the target process comprises, preferably consists of, a chemical conversion process and/or a thermal separation of compounds, wherein more preferably the target process comprises one or more of a chemical reaction, an evaporation, a pre-heating step, and a crystallization process, including combinations of two or more thereof, wherein more preferably the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, wherein the target process preferably comprises, preferably consists of, an endothermic reaction.

13. The method of embodiment 12, wherein the thermal separation of compounds comprises, preferably consists of, the isolation of isobutene from a mixture comprising n-butene, 2- butene and isobutene, preferably by distillation.

14. The method of embodiment 12, wherein the endothermic reaction comprises, preferably consists of, one or more of cracking, preferably catalytic cracking, dehydrogenation, styrene production, reverse water-gas shift, dehydration, thermal decomposition, dimerization, oligomerization, gamma-butyrolactone synthesis, and reforming, wherein cracking more preferably comprises cracking of one or more of steam, hydrocarbons, aliphatics, alkenes, preferably one or more of ethylene, propylene, and butylenes, dienes, preferably butadiene, acetylenes, cycloaliphatics, naphtha, polymers, plastics, biomass, oleaginous liquids, bitumen, tar ureas, carbamates, preferably carbamates to olefins, aromatics, fuels, isocyanates, melamine, and diamines, wherein dehydrogenation more preferably comprises dehydrogenation of one or more of hydrocarbons, more preferably of one or more of ethane, propane, butanes, pentanes, hexanes, preferably hexanes to olefins, alkenes (ethylene, propylene, butylenes), dienes (butadiene), and acetylenes, aliphatics, cycloaliphatics, naphtha, ethylbenzene, aromatics and styrene, wherein dehydration more preferably comprises dehydration of one or more of alcohols, preferably one or more of ethanol, bioethanol, propanol, and butanols, more preferably dehydration of alcohols to alkenes, preferably one or more of ethylene, propylene, and butylenes, wherein thermal decomposition comprises one or more of pyrolysis, thermolysis, gasification, more preferably thermal decomposition of one or more of polymers, plastics, biomasses, wastes, oil-containing liquids, bitumen, tar to olefins, alkenes, preferably one or more of ethylene, propylene and butylene, dienes, preferably butadiene, acetylenes, monomers, aromatics, fuels and synthesis gas, wherein one or more of dimerization and oligomerization comprises dimerization or oligomerization of alkenes, preferably of one or more of ethylene, butylenes and hexenes, more preferably to di- or oligoalkenes, wherein reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, production of syngas, and NH3 reforming, wherein the endothermic reaction more preferably comprises, more preferably consists of, NH3 reforming.

15. The method of embodiment 12, wherein the endothermic reaction comprises, preferably consists of, dehydration of ethanol, and wherein the chemical process from which heat is transferred in (ii) comprises production of ethylene oxide, preferably from ethylene. The method of embodiment 12, wherein the endothermic reaction comprises, preferably consists of, steam methane reforming, wherein steam methane reforming is preferably performed at 700 to 1100 °C, more preferably steam methane reforming to syngas comprising CO and hydrogen. The method of embodiment 12, wherein the endothermic reaction comprises, preferably consists of, steam cracking, wherein steam cracking is preferably performed at about 850 to about 900 °C, more preferably steam cracking of naphtha to olefins, methane, and hydrogen. The method of embodiment 12, wherein the exothermic reaction comprises, preferably consists of, one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and selective oxidation of one or more of alkanes, alkenes and alkynes, preferably selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid. The method of embodiment 12, wherein the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, wherein the hydrocarbons are selected from the group consisting of (Ci-C )alkanes, more preferably (Ci-Cs)alkanes, more preferably (Ci-Cy)alkanes. The method of any one of embodiments 1 to 19, wherein T1 is in the range of from 20 to 1 ,150 °C, preferably in the range of from 80 to 1 ,100 °C, more preferably in the range of from 200 to 1 ,000 °C, more preferably in the range of from 400 to 800 °C, more preferably in the range of from 500 to 600 °C. The method of any one of embodiments 1 to 19, wherein T2 is in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, more preferably in the range of from 450 to 1175 °C, more preferably in the range of from 550 to 1 ,075 °C. The method of any one of embodiments 1 to 21 , wherein the first process stream provided in (i) has a pressure in the range of from 1 to 300 bar(abs), preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs). The method of any one of embodiments 1 to 22, wherein the first process stream provided in (i) has a weight hourly space velocity in the range of from 200 to 20,000 IT ¹ , preferably in the range of from 400 to 15,000 IT ¹ , more preferably from 600 to 10,000 IT ¹ , more preferably from 1 ,000 to 5,000 IT ¹ . 24. The method of any one of embodiments 1 to 23, wherein transferring heat in (ii) comprises:

(ii.a) providing heat from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature T3;

(ii.b) transferring the heat provided in (ii.a) to the first process stream (1 ) provided in (i), for obtaining a heated first process stream (3) having a temperature T2; wherein T3 < T1 , and wherein T3 is preferably in the range of from 255 °C to 700 °C.

25. The method of embodiment 24, wherein the heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and/or from a physicochemical process, wherein the process stream from a chemical conversion process and/or from a physicochemical process preferably comprises one or more of steam, flue gas, preferably flue gas from a steam generation process.

26. The method of embodiment 24 or 25, wherein transferring of heat according to (ii.b) is conducted using a heat exchanger (2), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

27. The method of any one of embodiments 24 to 26, wherein the target process comprises NH3 reforming, and wherein transferring heat according to (ii.b) comprises at least partially converting NH3 to H2 and N2.

28. The method of any one of embodiments 24 to 27, wherein the heated first process stream obtained in (ii.b) has a temperature T2, wherein T2 is preferably in the range of from 350 to 1 ,225 °C, more preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, preferably in the range of from 450 to

1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

29. The method of any one of embodiments 24 to 28, wherein the heated first process stream obtained in (ii.b) has a pressure in the range of from 0.01 to 300 bar(abs), preferably in the range of from 1 to 275 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

30. The method of any one of embodiments 1 to 29, wherein transferring heat in (ii) comprises:

(ii.1 ) providing heat (4) from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature T3, wherein T3 is in the range of from 255 °C to 700 °C; (11.2) providing a stream (10) comprising a heat transfer medium, wherein the stream (10) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 250 °C;

(11.3) transferring the heat (4) provided in (ii.1) to the stream (10) provided in (ii.2), for obtaining a heated stream (11);

(11.4) increasing the pressure of the heated stream (11 ) obtained in (ii.3), for obtaining a compressed heated stream (7) having a temperature in the range of from 400 °C to 1 ,400 °C;

(11.5) transferring heat from the compressed heated stream (7) obtained in (ii.4) to the first process stream (1) provided in (i), for obtaining a heated first process stream (3) having a temperature T2 and a compressed stream (8).

31 . The method of embodiment 30, further comprising

(11.6) expanding the compressed stream (8) obtained in (ii.5);

(11.7) optionally recycling at least a portion of the stream obtained in (ii.6) to (ii.2).

32. The method of embodiment 30 or 31 , wherein the heat transfer medium is selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropro- pene, hydrofluorocarbons, preferably hydrofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, hydrocarbons, preferably one or more of butane, pentane, and hexane, ammonia, water, carbon dioxide, nitrogen, oxygen, air, noble gases, preferably one or more of helium, neon, argon, krypton, and xenon, tetraphenyl-compounds, and mixtures of two or more thereof.

33. The method of any one of embodiments 30 to 32, wherein the stream provided in (ii.2) has a temperature equal to or greater than 300 °C, preferably in the range of from 300 °C to 1000 °C, more preferably in the range of from 350 °C to 850°C.

34. The method of any one of embodiments 30 to 33, wherein the stream provided in (ii.2) has a pressure in the range of from 0.1 bar(abs) to 50 bar(abs), preferably in the range of from 0.5 bar(abs) to 30 bar(abs), more preferably in the range of from 1 bar(abs) to 20 bar(abs).

35. The method of any one of embodiments 30 to 34, wherein from 95 to 100 Vol-%, preferably from 99 to 100 Vol-%, more preferably from 99.9 to 100 Vol-%, of the stream provided in (ii.2) consist of the heat transfer medium.

36. The method of any one of embodiments 30 to 35, wherein the heat transfer medium in the stream provided in (ii.2) is in the liquid state. 37. The method of any one of embodiments 30 to 36, wherein the heat transfer medium in the stream provided in (ii.2) is a two-phase fluid with a vapor phase and a liquid phase.

38. The method of any one of embodiments 30 to 37, wherein the heat transfer medium in the stream provided in (ii.2) is in the supercritical state.

39. The method of any one of embodiments 30 to 38, wherein transferring the heat in (ii.3) is conducted using a heat exchanger (5), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

40. The method of any one of embodiments 30 to 39, wherein the heat provided in (ii.1) is obtained from a process stream from a chemical conversion process and/or from a physicochemical process, wherein the process stream from a chemical conversion process and/or from a physicochemical process preferably comprises one or more of steam, flue gas, preferably flue gas from a steam generation process.

41 . The method of any one of embodiments 30 to 40, wherein the heated stream obtained in (ii.3) has a temperature in the range of from 200 °C to 700 °C, preferably in the range of from 250 °C to 650 °C, more preferably in the range of from 350 °C to 550 °C.

42. The method of any one of embodiments 30 to 41 , wherein the heated stream obtained in (ii.3) is in the superheated vapor state.

43. The method of any one of embodiments 30 to 42, wherein the heated stream obtained in (ii.3) is in the supercritical state.

44. The method of any one of embodiments 30 to 43, wherein increasing the pressure of the stream according to (ii.4) is conducted using a compressor (12).

45. The method of any one of embodiments 30 to 44, wherein increasing the pressure of the stream according to (ii.4) is conducted using a multi-stage compressor (12), the multistage compressor preferably comprising one or more working media, preferably one or two working media, wherein the two working media are chemically and/or physically different from each other.

46. The method of embodiment 45, wherein the multi-stage compressor comprises one or more stages, wherein independently from one another each stage comprises a temperature elevation in the range of from 20 to 500 °C, preferably in the range of from 50 to 200 °C. 47. The method of any one of embodiments 30 to 46, wherein increasing the pressure of the stream according to (ii.4) is conducted adiabatically.

48. The method of any one of embodiments 30 to 47, wherein transferring of heat according to (ii.5) is conducted using a heat exchanger (2), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), more preferably the wall of a reactor containing the first process stream provided in (i).

49. The method of any one of embodiments 30 to 48, wherein the target process comprises NH3 reforming, and wherein transferring heat according to (ii.5) comprises at least partially converting NH3 to H2 and N2.

50. The method of any one of embodiments 30 to 49, wherein according to (ii.5) a compressed stream is obtained having a temperature in the range of from 375 °C to 1 ,400 °C, preferably in the range of from 475 °C to 1 ,100 °C, more preferably in the range of from 550 to 1 ,000 °C.

51 . The method of any one of embodiments 30 to 50, wherein according to (ii.5) a compressed stream is obtained having a pressure in the range of from 1 to 300 bar(abs), preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

52. The method of any one of embodiments 30 to 51 , wherein the heated first process stream obtained in (ii.5) has a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

53. The method of any one of embodiments 30 to 52, wherein the heated first process stream obtained in (ii.5) has a pressure in the range of from 0.01 to 300 bar(abs), preferably in the range of from 1 to 275 bar(abs), more preferably in the range of from 5 to 250 bar(abs), more preferably from 10 to 200 bar(abs), more preferably from 20 to 150 bar(abs), more preferably from 50 to 100 bar(abs).

54. The method of any one of embodiments 31 to 53, wherein the process preferably comprises (ii.6) and (ii.7) as defined in embodiment 31 , wherein expanding according to (ii.6) is conducted using a thermal expansion valve (9) or an expansion turbine (9).

55. The method of embodiment 54, wherein increasing the pressure of the stream according to (ii.4) is conducted using a compressor (12), wherein expanding is conducted using an expansion turbine, wherein the energy obtained from the expansion turbine, wherein the energy is preferably obtained as electricity, is used to operate the compressor, or wherein the energy obtained from the expansion turbine is used to operate the compressor mechanically, preferably via a shaft for directly transmitting the energy.

56. The method of any one of embodiments 31 to 55, wherein the process preferably comprises (ii.6) and (ii.7) as defined in embodiment 31 , wherein the expanded stream obtained in (ii.6) has the same pressure and temperature as the stream comprising a heat transfer medium provided in (ii.2).

57. The method of any one of embodiments 31 to 56, wherein the process comprises (ii.6), and preferably (ii.7), as defined in embodiment 31 , wherein expanding the compressed stream according to (ii.6) is conducted adiabatically.

58. The method of any one of embodiments 31 to 57, wherein the process comprises (ii.6), and preferably (ii.7), as defined in embodiment 31 , wherein from 1 to 100 vol-%, preferably from 10 to 90 vol-%, more preferably from 30 to 70 vol-%, of the stream obtained in (ii.6) are recycled to (ii.2) according to (ii.7).

59. The method of any one of embodiments 31 to 58, wherein the process preferably comprises (ii.6), and preferably (ii.7), as defined in embodiment 31 , wherein the stream obtained in (vii) is entirely recycled to (ii.2) according to (ii.7).

60. The method of embodiments 59, wherein steps (ii.2) to (ii.7) are conducted in a closed system in which the stream comprising a heat transfer medium is circulated.

61 . The method of any one of embodiments 1 to 60, wherein the method further comprises

(iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor, for obtaining a first product stream.

62. The method of embodiment 61 , wherein the heated first process stream obtained in (ii.5) or (ii.b) is fed into the first reactor having a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

63. The method of embodiment 61 or 62, the heated first process stream obtained in (ii.5) or (ii.b) is fed into the first reactor having a gas hourly space velocity in the range of from 10 h’ ¹ to 50.000 h’ ¹ , preferably in the range of from 100 IT ¹ to 20,000 IT ¹ , more preferably in the range of from 1 ,000 IT ¹ to 10,000 IT ¹ .

64. The method of any one of embodiments 61 to 63, wherein the method further comprises

(iv) heating the first product stream obtained in (iii) to a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C, and feeding the heated first product stream into a second reactor for obtaining a second product stream.

65. The method of embodiment 64, wherein the process comprises (ii.1 ), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), wherein heating the first product stream according to (iv) comprises transferring heat from the compressed stream obtained in (ii.4) to the first product stream obtained in (iii), for obtaining a heated first product stream, and a compressed stream having a temperature in the range of from 375 °C to 1 ,400 °C.

66. The method of embodiment 64 or 65, wherein the first and second reactor independently from one another is an adiabatic reactor, an isothermal reactor, or a combination thereof.

67. The method of any one of embodiments 64 to 66, wherein the first and second reactor independently from one another is a tubular reactor.

68. The method of any one of embodiments 1 to 67, wherein transferring heat in (ii) comprises:

(ii.T) providing heat (4) from a chemical conversion process, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, having a temperature in the range of from 255 °C to 700 °C;

(ii.2’) providing a stream (10a) comprising a first heat transfer medium, wherein the stream (10a) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 250 °C;

(ii.3’) transferring heat from the heat (4) provided in (ii.T) to the stream (10a) provided in (ii.2), for obtaining a heated stream (11 a);

(ii.4’) increasing the pressure of the heated stream (11 a) obtained in (ii.3’), for obtaining a compressed heated stream (7a) having a temperature in the range of from 400 °C to 1 ,400 °C;

(ii.5’) providing a stream (10b) comprising a second heat transfer medium, wherein the stream (10b) has a pressure in the range of from 0.001 to 100 bar(abs) and a temperature equal to or greater than 275 °C;

(ii.6’) transferring heat from the compressed heated stream (7a) obtained in (ii.4’) to the stream (10b) provided in (ii.5’), for obtaining a heated stream (11 b) and a compressed stream (8a);

(ii.7’) expanding the compressed stream (8a) obtained in (ii.6’);

(ii.8’) recycling at least a portion of the stream obtained in (ii.7’) to (ii.2’)

(ii.9’) increasing the pressure of the heated stream (11 b) obtained in (ii.6’), for obtaining a compressed heated stream (7b) having a temperature in the range of from 400 °C to 1 ,400 °C;

(ii.10’) transferring heat from the compressed heated stream (7b) obtained in (ii.9’) to the first process stream (1 ) provided in (i), for obtaining a heated first process stream (3) having a temperature T2 and a compressed stream (8b); (ii.11 ’) expanding the compressed stream (8b) obtained in (ii.1 O’);

(ii.12’) recycling at least a portion of the stream obtained in (ii.11 ’) to (ii.5’).

69. The method of embodiment 68, wherein the first heat transfer medium in (ii .2’) and the second heat transfer medium in (ii.5’) are independently from one another selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropro- pene, hydrofluorocarbons, preferably hydrofluoroolefins, more preferably one or more of (Z)-1-Chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, hydrocarbons, preferably one or more of butane, pentane, and hexane, ammonia, water, carbon dioxide, nitrogen, oxygen, air, noble gases, preferably one or more of helium, neon, argon, krypton, and xenon, tetraphenyl-compounds, and mixtures of two or more thereof.

70. The method of embodiment 68 or 69, wherein the stream (10a) provided in (ii.2’) has a temperature equal to or greater than 300 °C, preferably in the range of from 300 °C to 1000 °C, more preferably in the range of from 350 °C to 850°C.

71 . The method of any one of embodiments 68 to 70, wherein transferring the heat provided in (ii.1’) is conducted using a heat exchanger (5), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

72. The method of any one of embodiments 68 to 71 , wherein the heated stream obtained in (ii.3’) has a temperature in the range of from 350 °C to 950 °C, preferably in the range of from 400 °C to 600 °C, more preferably in the range of from 450 °C to 550 °C.

73. The method of any one of embodiments 68 to 72, wherein increasing the pressure of the heated stream (11a) is conducted using a compressor (12a).

74. The method of any one of embodiments 68 to 73, wherein the stream (10b) provided in (ii.5’) has a temperature equal to or greater than 325 °C, preferably in the range of from 325 to 1 ,000 °C, more preferably in the range of from 375 to 850 °C, more preferably in the range of from 450 to 650 °C, more preferably in the range of from 500 to 600 °C.

75. The method of any one of embodiments 68 to 74, wherein transferring heat from the compressed heated stream (7a) is conducted using a heat exchanger (13), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

76. The method of any one of embodiments 68 to 75, wherein according to (ii.6’) a compressed stream (8a) is obtained having a temperature in the range of from 355 °C to 1 ,400 °C, preferably in the range of from 455 °C to 655 °C, more preferably in the range of from 505 to 605 °C.

77. The method of any one of embodiments 68 to 76, wherein the heated stream (11 b) obtained in (ii.6’) has a temperature in the range of from 350 °C to 1150 °C, preferably in the range of from 450 °C to 650 °C, more preferably in the range of from 500 °C to 600 °C.

78. The method of any one of embodiments 68 to 77, wherein increasing the pressure of the heated stream (11b) is conducted using a compressor (12b).

79. The method of any one of embodiments 68 to 78, wherein transferring heat from the compressed heated stream (7b) is conducted using a heat exchanger (2), wherein the heat exchanger preferably comprises one or more of an internal or external coil, a jacket heater, a double wall heat exchanger, an internal pipe heater, and a shell and tube heat exchanger.

80. The method of any one of embodiments 68 to 79, wherein the heated first process stream obtained in (ii.1 O’) has a temperature in the range of from 350 to 1 ,225 °C, preferably in the range of from greater than 350 °C to 1 ,225 °C, more preferably in the range of from 375 °C to 1 ,225 °C, preferably in the range of from 450 to 1 ,175 °C, more preferably in the range of from 550 to 1 ,075 °C.

81 . The method of any one of embodiments 68 to 80, wherein expanding according to (ii .7’) and (ii.11 ’) are independently from one another conducted using a thermal expansion valve (9a and/or 9b) or an expansion turbine (9a and/or 9b).

82. The method of any one of embodiments 1 to 81 , wherein the heated first process stream obtained in (ii) is used as feed or co-feed for an endothermic reaction, preferably for a high temperature endothermic reaction.

83. The method of any one of embodiments 1 to 82, wherein the heated first process stream obtained in (ii) is used as feed stream for a NH3 reforming process.

The present invention is further illustrated by the following reference example.

EXAMPLES

Reference Example 1 : Heat transfer method comprising Hg as heat transfer medium

A cycle is shown in Figure 1 schematically for the heat transfer medium mercury. This method concept is particularly interesting when an exothermic heat source at low temperature and an endothermic heat sink at higher temperature are present within a production plant. The COP was 4.27, and the volumetric heating capacity (VHC) was 8337 kJ/m ³ .

Heat is transferred to Hg at the heat source, and heat is transferred from Hg at the heat sink to a stream of a target process.

Brief description of figures:

Figure 1 : shows a process scheme wherein mercury is used as heat transfer medium.

Figure 2: shows a method scheme for a thermodynamic cycle or heat pump process as closed loop process.

Figure 3: shows a method scheme for a two-stage thermodynamic cycle or two-stage heat pump process, wherein each stage comprises a closed loop process.

Description of Reference numerals

For Figure 2:

(1 ) first process stream

(2) heat exchanger

(3) heated first process stream

(4) heat

(5) heat exchanger

(6) exhaust

(7) compressed heated stream

(8) compressed stream

(9) thermal expansion valve or expansion turbine

(10) stream comprising a heat transfer medium

(11 ) heated stream

(12) compressor or multi-stage compressor

For Figure 3:

(1 ) first process stream

(2) heat exchanger

(3) heated first process stream

(4) heat

(5) heat exchanger

(6) exhaust

(7a) compressed heated stream

(8a) compressed stream

(9a) thermal expansion valve or expansion turbine

(10a) stream comprising a first heat transfer medium (l la) heated stream

(12a) compressor or multi-stage compressor

(13) heat exchanger

(7b) compressed heated stream (8b) compressed stream

(9b) thermal expansion valve or expansion turbine

(10b) stream comprising a second heat transfer medium

(l l b) heated stream

(12b) compressor or multi-stage compressor

Cited literature:

- DE 2951188 A1

- DE 3209642 A1 - V. Singh et al. “Investigation of new mechanical heat pump systems for heat upgrading applications” in Int. J. Energy Ress. 2018, 42, 3078-3090