Method for transferring heat between two independent processes

Abstract

The 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 T1; (ii) transferring heat from a chemical conversion process, a physicochemical process, ambient heat, or a combination of two or more thereof to the first process stream provided in (i) to obtain a heated first process stream (3) having a temperature T2, where T2gt; t1; (iii) performing the target process with the heated first process stream obtained in (ii); wherein the target process differs from the chemical conversion process, the physicochemical process, or a combination of the chemical conversion process and the physicochemical process according to (ii) from which heat is transferred. According to the method of the invention, a performance coefficient greater than 1 can be obtained.

Description

Technical Field

[0001] The present invention relates to a method for transferring heat between two independent processes in a chemical production plant, in particular for transferring heat from a chemical conversion process, a physicochemical process, ambient heat, or a combination of two or more thereof to a target process. Background Art

[0002] Providing heat energy for endothermic processes is currently accomplished by burning fossil fuels or by direct electric heating. Fossil fuels are generally preferred to direct electric heating because of lower efficiency and therefore lower cost.

[0003] By intelligently using electrical energy in a thermodynamic cycle, a heat pump achieves an increase in temperature level by a much greater amount of heat than the amount of electrical energy used. To increase the temperature level according to the Carnot cycle, the coefficient of performance (COP) is calculated according to Formula I:

[0004] ε 卡诺-WP =1 / (1-T 低 / T 高 )(I),

[0005] where ε 卡诺-WP is the coefficient of performance of the Carnot cycle of the heat pump, T 低 is the absolute temperature (in Kelvin) at which the heat is absorbed, and T 高 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 to be heated occurs.

[0006] So far, 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 occur at high temperatures.

[0007] DE 2951188 A1 relates to a method for utilizing waste heat from endothermic processes, wherein heat is initially provided from an external heat source at a high temperature level and waste heat from the reaction is obtained at a low temperature level, wherein the low temperature waste heat is recycled to the endothermic reaction by means of a heat pump.

[0008] DE 3209642 A1 discloses a process heat generating device for the joint generation of high-temperature heat and process steam.

[0009] V. Singh et al., “Investigation of new mechanical heat pump systems for heat upgrading applications,” Int. J. Energy Ress. 2018, 42, 3078-3090, disclose examples of multi-stage ultra-high temperature heat pumps with different heat transfer media that can be used in process engineering and other applications.

[0010] In the course of converting technical processes into sustainable energy, it is therefore desirable to further increase the temperature levels achieved to date by heat pumps in order to reduce the dependence on other energy sources for processes requiring heat at high temperature levels.

[0011] Thus, for an endothermic reaction at 350°C and a heat source at 30°C, a theoretical COP of 1.95 can still be achieved, and thus theoretically almost twice as much heat can be provided for the reaction if the electricity used to operate the heat pump is used directly for heating. Typically, the COP is significantly lower than 1.5, but the use of a heat pump can still be considered, for example if steam is no longer available for the process due to temperature and pressure levels, or is only available under extreme difficulty.

[0012] An important area of ​​application for ultra-high temperature heat pumps is the valorization of thermal energy, which is already available at high temperatures (e.g. at about 300°C). 卡诺 =1 / (1-(773K / 973K))=4.5), these heat pumps are suitable for heat utilization at much higher temperatures exceeding 600°C.

[0013] The object of the present invention is therefore to provide a method in which the utilization of heat, for example by means of a heat pump, is not limited to the optimization of individual heat-consuming processes, such as endothermic reactions, or to the valorization of primary energy sources and in particular sustainable energy or nuclear power. In particular, the object of the present invention is to utilize a heat transfer concept which involves the valorization of heat which does not originate from primary energy sources and in particular involves the valorization of waste heat or other available low-temperature heat. DETAILED DESCRIPTION

[0014] Thus, it has been unexpectedly found that thermal energy at low temperatures (e.g. 20°C to 80°C) can be used to upgrade them to usable thermal energy at temperatures equal to or greater than 350°C, preferably greater than 350°C, more preferably greater than 375°C, whereby a coefficient of performance (COP) greater than 1 can be achieved. In particular, it has been unexpectedly found that the use of heat pump cascades is particularly advantageous for achieving energy efficiency and reducing dependence on primary energy sources, whether they are sustainable or not. Thus, by appropriately selecting the heat transfer medium, upgrading the heat source can directly supply heat to the process (e.g. by superheating saturated steam) at a temperature equal to or greater than 350°C, preferably greater than 350°C, more preferably 375°C to 1,275°C to provide the necessary temperature in the target process. In particular, it has been found that the use of high temperature heat pumps allows difficult to achieve electrical heating and in particular has a better electrical efficiency COP greater than 1 实际 Electrification of the process.

[0015] The method of the invention is particularly advantageous if there is an exothermic heat source at low temperatures and an endothermic heat sink at higher temperatures in the production plant. In this respect, it is advantageous to use a heat pump for high-temperature applications (>200° C.). The compressor / compressor cascade and the heat transfer medium used are adapted to the high temperatures accordingly. In addition to mercury, tetraphenyl compounds are also possible heat transfer media for achieving the results of the invention. In addition, some metals are suitable as heat transfer media for applications with maximum temperatures exceeding 1,000° C.

[0016] In addition to the leverage effect due to COP>1, the use of heat pumps can also be considered if the reaction temperature is too high to achieve a practical COP>1. This is the case when conventional heating concepts become problematic due to the required high temperatures and high powers (e.g. due to very high currents at relatively low voltages of resistance heaters) or when >290°C is no longer possible using conventional process steam. The compressors used in heat pumps can be operated at medium or high pressure, thus avoiding electrical infrastructure, conversion losses and high currents. In contrast, the conventional use of electric heaters at very high temperatures usually requires an indirect heating concept, in which heat is transferred from the electric heater to the process via radiation. This usually results in an uneven temperature profile and also increased equipment requirements.

[0017] If the equipment needs to be cooled over a wide temperature range above ΔT of 50°C and can therefore be used as a heat source (e.g. cooling from about 350°C to 250°C), a two-stage heat pump using the same working fluid is advantageous in terms of electrical efficiency, since there is no need to depressurize the hotter circuit to a lower temperature and pressure level afterwards. 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). A three-stage process is also conceivable, although this increases the complexity of the system.

[0018] The process of the invention is not limited to endothermic reactions. Often, exothermic reactions are followed by energy-intensive separation steps / distillations, which in turn can benefit from the process of the invention, even when waste heat from previous reactions is used as a heat source. In these cases, the high-temperature heat pump can also act as a high-temperature heat reservoir.

[0019] The present invention therefore relates to a method for transferring heat to a target process in a chemical production plant, the method comprising:

[0020] (i) providing a first process stream (1) having a temperature T1;

[0021] (ii) transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to the first process stream provided in (i) to obtain a heated first process stream (3) having a temperature T2, wherein T2>T1;

[0022] (iii) performing the target process using the heated first process stream obtained in (ii);

[0023] wherein the target process is different from the chemical conversion process, the physicochemical process, or a combination of the chemical conversion process and the physicochemical process from which heat is transferred according to (ii).

[0024] Within the meaning of the present invention, the term "different" with respect to the chemical conversion process and / or physicochemical process in (ii) that is different from the target process indicates that the method of the present invention does not recycle heat to the chemical conversion process and / or physicochemical process. Therefore, although according to a specific embodiment or the method of the present invention, the chemical conversion process and / or physicochemical process in (ii) can be the same as the target process, they are not the same in the following sense: the heat derived from a specific chemical conversion process and / or physicochemical process can be recycled to the same chemical conversion process and / or physicochemical process in a different process, but no longer to the chemical conversion process and / or physicochemical process from which it originates. However, according to the present invention, it is preferred that according to a specific and preferred embodiment of the present invention, wherein the target process is a chemical conversion process and / or physicochemical process, the chemical conversion process and / or physicochemical process of (ii) is not the same as the chemical conversion process and / or physicochemical process of the target process.

[0025] It is preferred that in (ii) heat is transferred from a chemical conversion process and / or a physicochemical process and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat to the heat for carrying out an autothermal reaction or an endothermic reaction.

[0026] In case in (ii) the heat is transferred from a chemical conversion process and / or a physicochemical process, and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat to the heat used to carry out the autothermal reaction or the endothermic reaction, it is preferred according to the first alternative that the exothermic reaction comprises one or more of the following: methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and the selective oxidation of one or more of alkanes, alkenes and alkynes, preferably the selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid.

[0027] In addition, in the case where heat is transferred from a chemical conversion process and / or a physicochemical process in (ii), and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat for carrying out an autothermal reaction or an endothermic reaction, according to the second alternative it is preferred that the endothermic reaction includes one or more of the following: 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.

[0028] In addition, in the case where heat is transferred from a chemical conversion process and / or a physicochemical process in (ii), and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat for carrying out an autothermal reaction or an endothermic reaction, according to the third alternative 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 these hydrocarbons are selected from the group consisting of (C1-C10) alkanes, more preferably (C1-C8) alkanes, more preferably (C1-C7) alkanes.

[0029] It is preferred that the physicochemical process comprises one or more of, preferably consists of, vapour compression evaporation and chemical adsorption processes.

[0030] It is preferred that the ambient heat transferred according to (ii) is heat from the environment, preferably heat from one or more of air, water and solar radiation, including combinations of two or more thereof.

[0031] It is preferred that the heat transferred according to (ii) does not include energy from nuclear fission, solar thermal energy, geothermal energy, hydroelectric energy, and wind energy.

[0032] Therefore, the method according to the invention does not involve the optimization of a single process with respect to its energy efficiency. In particular, the invention does not involve a method in which energy is recycled, especially a method for optimizing the efficiency of energy conversion. In addition, the method according to the invention does not involve a method in which the energy for transferring heat originates from a pure energy source.

[0033] It is preferred that transferring heat in (ii) comprises using a heat pump, wherein the heat pump is selected from the group consisting of: a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

[0034] In the case where transferring heat in (ii) comprises using a heat pump (wherein the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump), it is preferred that the absorption heat pump is a conventional heat pump (Type I heat pump), a heat converter heat pump (Type II heat pump), or an adsorption heat pump, wherein the absorption heat pump is preferably a conventional heat pump.

[0035] In the case where the absorption heat pump is a conventional heat pump (Type I heat pump), a heat converter heat pump (Type II heat pump), or an adsorption heat pump, it is preferred that the adsorption heat pump comprises an adsorbent, wherein the adsorbent comprises one or more of activated carbon, zeolite and mixtures thereof, preferably consisting thereof.

[0036] It is preferred that the target process comprises heating one or more compounds, preferably consists of it, wherein preferably the target process comprises a chemical conversion process and / or thermal separation of compounds, preferably consists of it, wherein more preferably the target process comprises one or more of a chemical reaction, evaporation, a preheating step and a crystallization process, including combinations of two or more thereof, wherein more preferably the target process comprises distillation (preferably column distillation), an endothermic reaction, an exothermic reaction or an autothermal reaction, preferably consists of it, wherein the target process preferably comprises an endothermic reaction, preferably consists of it.

[0037] In case the target process comprises, preferably consists of, heating one or more compounds, wherein preferably the target process comprises, preferably consists of, a chemical conversion process and / or a thermal separation of compounds, preferably it is preferred that the thermal separation of compounds comprises, preferably consists of, separating isobutene from a mixture comprising n-butene, 2-butene and isobutene, preferably by distillation.

[0038] Where the target process comprises, preferably consists of, distillation (preferably 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, γ-butyrolactone synthesis, and reforming,

[0039] wherein the cracking more preferably comprises cracking one or more of: steam, hydrocarbons, aliphatics, olefins (preferably one or more of ethylene, propylene and butene), dienes (preferably butadiene), acetylene, alicyclic compounds, naphtha, polymers, plastics, biomass, oily liquids, asphalt, tar urea, carbamates, preferably carbamates to olefins, aromatic compounds, fuels, isocyanates, melamine, and diamines,

[0040] wherein the dehydrogenation more preferably comprises the dehydrogenation of one or more of the following: hydrocarbons, more preferably one or more of ethane, propane, butane, pentane, hexane (preferably hexane to olefins), olefins (ethylene, propylene, butene), dienes (butadiene) and acetylene, aliphatic compounds, alicyclic compounds, naphtha, ethylbenzene, aromatic compounds and styrene,

[0041] wherein the dehydration more preferably comprises the dehydration of one or more of the following: alcohols, preferably one or more of ethanol, bioethanol, propanol and butanol, more preferably alcohols to olefins, preferably one or more of ethylene, propylene and butene,

[0042] wherein the thermal decomposition comprises one or more of pyrolysis, thermal decomposition, and gasification, more preferably the thermal decomposition of one or more of the following: polymers, plastics, biomass, waste, oily liquids, asphalt, tar to olefins, olefins (preferably one or more of ethylene, propylene and butene), dienes (preferably butadiene), acetylene, monomers, aromatic compounds, fuels and synthesis gas,

[0043] wherein one or more of the dimerization and oligomerization comprises dimerization or oligomerization of olefins, preferably one or more of ethylene, butene and hexene, more preferably to diolefins or oligomerized olefins,

[0044] wherein the reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, production of synthesis gas, and NH3 reforming,

[0045] The endothermic reaction more preferably comprises, and more preferably consists of, NH3 reforming.

[0046] Additionally, where the target process comprises, preferably consists of, distillation (preferably column distillation), an endothermic reaction, an exothermic reaction, or an autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, the dehydration of ethanol, and wherein the chemical process from which heat is transferred in (ii) comprises the production of ethylene oxide, preferably from ethylene.

[0047] In addition, when the target process includes distillation (preferably tower distillation), an endothermic reaction, an exothermic reaction, or an autothermal reaction, and preferably consists of them, it is preferred that the endothermic reaction includes the following items, and preferably consists of them: steam methane reforming, wherein the steam methane reforming is preferably carried out at 700°C to 1100°C, more preferably steam methane reforming to produce synthesis gas containing CO and hydrogen.

[0048] In addition, when the target process comprises distillation (preferably column distillation), an endothermic reaction, an exothermic reaction, or an autothermal reaction, preferably consisting of the same, it is preferred that the endothermic reaction comprises the following, preferably consists of: steam cracking, wherein the steam cracking is preferably carried out at about 850°C to about 900°C, more preferably steam cracking of naphtha to olefins, methane and hydrogen.

[0049] In addition, in the case where the target process comprises distillation (preferably column distillation), an endothermic reaction, an exothermic reaction, or an autothermal reaction, preferably consisting of the same, it is preferred that the exothermic reaction comprises one or more of the following, preferably consisting 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.

[0050] In addition, in case the target process comprises distillation (preferably column distillation), endothermic reaction, exothermic reaction, or autothermal reaction, preferably consists of the same, 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) of hydrocarbons, wherein the hydrocarbons are selected from (C1-C 10 )alkanes, more preferably (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0051] It is preferred that T1 is in the range of 20°C to 1,150°C, more preferably in the range of 80°C to 1,100°C, more preferably in the range of 200°C to 1,000°C, more preferably in the range of 400°C to 800°C, more preferably in the range of 500°C to 600°C.

[0052] It is preferred that T2 is in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1175°C, more preferably in the range of 550°C to 1,075°C.

[0053] Preferably, the first process stream provided in (i) has a pressure in the range of 1 to 300 bar (absolute), more preferably in the range of 5 to 250 bar (absolute), even more preferably 10 to 200 bar (absolute), even more preferably 20 to 150 bar (absolute), and even more preferably 50 to 100 bar (absolute).

[0054] Preferably, the first process stream provided in (i) has a weight hourly space velocity in the range of 200 to 20,000 h -1 and more preferably in the range of 400 to 15,000 h - 1 and even more preferably in the range of 600 to 10,000 h -1 and even more preferably in the range of 1,000 to 5,000 h -1 .

[0055] Preferably, the heat transfer in (ii) includes:

[0056] (ii.a) providing heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, which has a temperature T3;

[0057] (ii.b) transferring the heat provided in (ii.a) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2;

[0058] wherein T3 < T1, and wherein T3 is more preferably in the range of 255 °C to 700 °C.

[0059] In the case where the method includes (ii.a) and (ii.b), preferably the heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and / or a physicochemical process, wherein the process stream from the chemical conversion process and / or the physicochemical process preferably includes one or more of steam from a steam generation process and flue gas, and more preferably flue gas.

[0060] In addition, in the case where the method includes (ii.a) and (ii.b), preferably the heat transfer according to (ii.b) is carried out using a heat exchanger (2), wherein the heat exchanger preferably includes one or more of internal or external coils, jacket heaters, double-wall heat exchangers, internal pipe heaters, and shell-and-tube heat exchangers, and wherein the heat exchanger is preferably a reactor containing the first process stream provided in (i), and more preferably the wall of a reactor containing the first process stream provided in (i).

[0061] Additionally, 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 into H2 and N2.

[0062] In addition, in case the process 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 350°C to 1,225°C, more preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C.

[0063] Additionally, in case the process 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 0.01 to 300 bar (absolute), more preferably in the range of 1 to 275 bar (absolute), more preferably in the range of 5 to 250 bar (absolute), more preferably in the range of 10 to 200 bar (absolute), more preferably in the range of 20 to 150 bar (absolute), more preferably in the range of 50 to 100 bar (absolute).

[0064] Preferably, transferring heat in (ii) comprises:

[0065] (ii.1) providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature T3, wherein T3 is in the range of 255°C to 700°C;

[0066] (ii.2) providing a stream (10) comprising a heat transfer medium, wherein the stream (10) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 250° C.;

[0067] (ii.3) transferring the heat (4) provided in (ii.1) to the stream (10) provided in (ii.2) to obtain a heated stream (11);

[0068] (ii.4) increasing the pressure of the heated stream (11) obtained in (ii.3) to obtain a compressed heated stream (7) having a temperature in the range of 400° C. to 1,400° C.;

[0069] (ii.5) transferring heat from the compressed heated stream (7) obtained in (ii.4) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8).

[0070] In the case where the heat transfer in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), and (ii.5), it is preferred that the method further includes

[0071] (ii.6) expanding the compressed flow (8) obtained in (ii.5);

[0072] (ii.7) Optionally recycling at least a portion of the stream obtained in (ii.6) to (ii.2).

[0073] In addition, when transferring heat in (ii) includes (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 (Z)-1-chloro-2,3,3,3-tetrafluoropropene one or more of olefins and trans-1-chloro-3,3,3-trifluoropropene, one or more of hydrofluorocarbons, preferably hydrofluoroolefins, more preferably (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.

[0074] In addition, when the heat transferred in (ii) includes (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 300°C to 1000°C, and more preferably in the range of 350°C to 850°C.

[0075] In addition, when transferring heat in (ii) includes (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 0.1 bar (absolute value) to 50 bar (absolute value), more preferably in the range of 0.5 bar (absolute value) to 30 bar (absolute value), and more preferably in the range of 1 bar (absolute value) to 20 bar (absolute value).

[0076] In addition, when transferring heat in (ii) includes (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 95 to 100 Vol-%, more preferably 99 to 100 Vol-%, more preferably 99.9 to 100 Vol-% of the flow provided in (ii.2) is composed of heat transfer medium.

[0077] In addition, when the heat transfer in (ii) includes (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 flow provided in (ii.2) is in a liquid state.

[0078] In addition, when transferring heat in (ii) includes (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 flow provided in (ii.2) is a two-phase fluid having a vapor phase and a liquid phase.

[0079] In addition, when the heat transfer in (ii) includes (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 flow provided in (ii.2) is in a supercritical state.

[0080] In addition, when transferring heat in (ii) includes (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 heat in (ii.3) is carried out using a heat exchanger (5), wherein the heat exchanger preferably includes 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 a wall of a reactor containing the first process stream provided in (i).

[0081] In addition, when the heat transferred in (ii) includes (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 a physicochemical process, wherein the process stream from the chemical conversion process and / or the physicochemical process preferably includes one or more of steam from a steam generation process, flue gas, preferably flue gas.

[0082] In addition, when the heat transferred in (ii) includes (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 200°C to 700°C, preferably in the range of 250°C to 650°C, and more preferably in the range of 350°C to 550°C.

[0083] In addition, when the heat transferred in (ii) includes (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 flow obtained in (ii.3) is in a superheated vapor state.

[0084] In addition, when the heat transferred in (ii) includes (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 flow obtained in (ii.3) is in a supercritical state.

[0085] In addition, when the heat transfer in (ii) includes (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 to use a compressor (12) to increase the pressure of the flow according to (ii.4).

[0086] In addition, when the heat transfer in (ii) includes (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 pressure of the flow is increased according to (ii.4) using a multi-stage compressor (12), which preferably contains 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.

[0087] In case the pressure increase of the flow according to (ii.4) is carried out using a multi-stage compressor (12), it is preferred that the multi-stage compressor comprises one or more stages, wherein each stage independently of one another comprises a temperature increase in the range of 20°C to 500°C, more preferably in the range of 50°C to 200°C.

[0088] In addition, when the heat transfer in (ii) includes (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 pressure of the flow is increased according to (ii.4) under adiabatic conditions.

[0089] In addition, when transferring heat in (ii) includes (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 according to (ii.5) is carried out using a heat exchanger (2), wherein the heat exchanger more preferably includes 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 a wall of a reactor containing the first process stream provided in (i).

[0090] In addition, in the case where transferring heat in (ii) includes (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 includes NH3 reforming, and wherein transferring heat according to (ii.5) includes at least partially converting NH3 into H2 and N2.

[0091] In addition, when transferring heat in (ii) includes (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 to obtain a compressed stream according to (ii.5), which has a temperature in the range of 375°C to 1,400°C, more preferably in the range of 475°C to 1,100°C, and more preferably in the range of 550 to 1,000°C.

[0092] In addition, when transferring heat in (ii) includes (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 a compressed stream is obtained according to (ii.5), and the compressed stream has a pressure in the range of 1 to 300 bar (absolute value), more preferably in the range of 5 to 250 bar (absolute value), more preferably 10 to 200 bar (absolute value), more preferably 20 to 150 bar (absolute value), and more preferably 50 to 100 bar (absolute value).

[0093] In addition, when transferring heat in (ii) includes (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 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1,175°C, and more preferably in the range of 550°C to 1,075°C.

[0094] In addition, when transferring heat in (ii) includes (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 0.01 to 300 bar (absolute value), more preferably in the range of 1 to 275 bar (absolute value), more preferably in the range of 5 to 250 bar (absolute value), more preferably in the range of 10 to 200 bar (absolute value), more preferably in the range of 20 to 150 bar (absolute value), more preferably in the range of 50 to 100 bar (absolute value).

[0095] In addition, when the heat transferred in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the expansion according to (ii.6) is carried out using a thermal expansion valve (9) or an expansion turbine (9).

[0096] In case the expansion according to (ii.6) is carried out using an expansion turbine (9), it is preferred that increasing the pressure of the flow according to (ii.4) is carried out using a compressor (12), wherein the expansion is carried out 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 transferring energy.

[0097] In addition, in the case where heat is transferred in (ii) including (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the expanded flow obtained in (ii.6) has the same pressure and temperature as the flow containing the heat transfer medium provided in (ii.2).

[0098] In addition, when the heat transferred in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that the compressed flow is expanded under adiabatic conditions according to (ii.6).

[0099] In addition, in the case where heat is transferred in (ii) including (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), it is preferred that 1 to 100 vol-%, more preferably 10 to 90 vol-%, and more preferably 30 to 70 vol-% of the stream obtained in (ii.6) is recycled to (ii.2) according to (ii.7).

[0100] In addition, when the heat transferred in (ii) includes (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 completely recycled to (ii.2) according to (ii.7).

[0101] In case the stream obtained in (vii) is completely recycled to (ii.2) according to (ii.7), it is preferred that steps (ii.2) to (ii.7) are carried out in a closed system in which the stream comprising the heat transfer medium circulates.

[0102] It is preferred that the process (wherein the process 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 to obtain a first product stream.

[0103] In case the process further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor to obtain a first product stream, it is preferred that the heated first process stream obtained in (ii.5) is fed into the first reactor, the heated first process stream having a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C.

[0104] In addition, 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 to obtain a first product stream, it is preferred that the heated first process stream obtained in (ii.5) is fed into the first reactor, and the heated first process stream has a flow rate of 100 % in 10 hours. -1 Up to 50.000h -1 In the range of 100h, more preferably in the range of 100h -1 Up to 20,000h -1 In the range of 1,000h -1 Up to 10,000h -1 Gas hourly space velocity in the range.

[0105] In addition, in the case where the process further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor to obtain a first product stream, it is preferred that the process further comprises (iv) heating the first product stream obtained in (iii) to a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C, and feeding the heated first product stream into a second reactor to obtain a second product stream.

[0106] In case the process 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) to obtain a heated first product stream and a compressed stream having a temperature in the range of 375°C to 1,400°C.

[0107] Further, in case the process further comprises (iv), it is preferred that the first and second reactors are independently of each other adiabatic reactors, isothermal reactors, or a combination thereof.

[0108] In the context of the present invention, an adiabatic or isothermal change of state is understood to be a change of state which is achieved by a close to theoretical adiabatic or isothermal process.

[0109] Additionally, in case the process further comprises (iv), it is preferred that the first and second reactors are independently tubular reactors.

[0110] Preferably, transferring heat in (ii) comprises:

[0111] (ii.1') providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature in the range of 255°C to 700°C;

[0112] (ii.2') providing a stream (10a) comprising a first heat transfer medium, wherein the stream (10a) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 250°C;

[0113] (ii.3') transferring heat from the heat (4) provided in (ii.1') to the stream (10a) provided in (ii.2) to obtain a heated stream (11a);

[0114] (ii.4') increasing the pressure of the heated stream (11a) obtained in (ii.3') to obtain a compressed heated stream (7a) having a temperature in the range of 400°C to 1,400°C;

[0115] (ii.5') providing a stream (10b) comprising a second heat transfer medium, wherein the stream (10b) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 275°C;

[0116] (ii.6') transferring heat from the compressed heated stream (7a) obtained in (ii.4') to the stream (10b) provided in (ii.5') to obtain a heated stream (11b) and a compressed stream (8a);

[0117] (ii.7') expanding the compressed flow (8a) obtained in (ii.6');

[0118] (ii.8') recycling at least a portion of the stream obtained in (ii.7') to (ii.2')

[0119] (ii.9') increasing the pressure of the heated stream (11b) obtained in (ii.6') to obtain a compressed heated stream (7b) having a temperature in the range of 400°C to 1,400°C;

[0120] (ii.10') transferring heat from the compressed heated stream (7b) obtained in (ii.9') to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8b);

[0121] (ii.11') expanding the compressed flow (8b) obtained in (ii.10');

[0122] (ii.12') Recirculating at least a portion of the stream obtained in (ii.11') to (ii.5').

[0123] In the case where the heat transfer in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (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 selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably 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-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.

[0124] In addition, in the case where heat is transferred in (ii) including (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (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 300°C to 1000°C, and more preferably in the range of 350°C to 850°C.

[0125] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heat provided in (ii.1') is transferred using a heat exchanger (5), wherein the heat exchanger preferably includes 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.

[0126] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heated stream obtained in (ii.3') has a temperature in the range of 350°C to 950°C, more preferably in the range of 400°C to 600°C, and more preferably in the range of 450°C to 550°C.

[0127] In addition, in the case where heat is transferred in (ii) including (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred to increase the pressure of the heated stream (11a) using a compressor (12a).

[0128] In addition, in the case where the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the stream (10b) provided in (ii.5') has a temperature equal to or greater than 325°C, more preferably in the range of 325°C to 1,000°C, more preferably in the range of 375°C to 850°C, more preferably in the range of 450°C to 650°C, and more preferably in the range of 500°C to 600°C.

[0129] In addition, in the case where the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heat transferred from the compressed heating stream (7a) is carried out using a heat exchanger (13), wherein the heat exchanger preferably includes 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.

[0130] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred to obtain a compressed stream (8a) according to (ii.6'), which has a temperature in the range of 355°C to 1,400°C, more preferably in the range of 455°C to 655°C, and more preferably in the range of 505°C to 605°C.

[0131] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heated stream (11b) obtained in (ii.6') has a temperature in the range of 350°C to 1150°C, more preferably in the range of 450°C to 650°C, and more preferably in the range of 500°C to 600°C.

[0132] In addition, in the case where heat is transferred in (ii) including (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred to increase the pressure of the heated stream (11b) using a compressor (12b).

[0133] In addition, in the case where the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heat transferred from the compressed heating stream (7b) is carried out using a heat exchanger (2), wherein the heat exchanger more preferably includes 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.

[0134] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heated first process stream obtained in (ii.10') has a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1,175°C, and more preferably in the range of 550°C to 1,075°C.

[0135] In addition, in the case where heat is transferred in (ii) including (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the expansion according to (ii.7') and (ii.11') is carried out independently of each other using a thermal expansion valve (9a and / or 9b) or an expansion turbine (9a and / or 9b).

[0136] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heated first process stream obtained in (ii) is used as a feed or co-feed for an endothermic reaction, preferably a high temperature endothermic reaction.

[0137] In addition, when the heat transferred in (ii) includes (ii.1'), (ii.2'), (ii.3'), (ii.4'), (ii.5'), (ii.6'), (ii.7'), (ii.8'), (ii.9'), (ii.10'), (ii.11'), and (ii.12'), it is preferred that the heated first process stream obtained in (ii) is used as the feed stream for the NH3 reforming process.

[0138] The unit bar (absolute) refers to absolute pressure, where 1 bar is equal to 10 5 Pa.

[0139] The present invention is further illustrated by the following group of embodiments and the combination of embodiments obtained by the dependencies and back-references as shown. In particular, it should be noted that in each case where a series of embodiments is mentioned, for example, in the context of a term such as "a method as described in any one of embodiments 1 to 4", each embodiment in this series is intended to be clearly disclosed to the technician, that is, the wording of this term should be understood by the technician as synonymous with "a method as described in any one of embodiments 1, 2, 3 and 4". In addition, it is explicitly pointed out that the following group of embodiments is not a group of claims that determine the scope of protection, but represents an appropriate structural part of this specification related to the general and preferred aspects of the present invention.

[0140] 1. A method for transferring heat to a target process in a chemical production plant, the method comprising:

[0141] (i) providing a first process stream (1) having a temperature T1;

[0142] (ii) transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to the first process stream provided in (i) to obtain a heated first process stream (3) having a temperature T2, wherein T2>T1;

[0143] (iii) performing the target process using the heated first process stream obtained in (ii);

[0144] wherein the target process is different from the chemical conversion process, the physicochemical process, or a combination of the chemical conversion process and the physicochemical process from which heat is transferred according to (ii).

[0145] 2. A method as described in Example 1, wherein in (ii) heat is transferred from a chemical conversion process and / or a physicochemical process, and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat for performing an autothermal reaction or an endothermic reaction.

[0146] 3. A method as described in Example 2, wherein the exothermic reaction comprises one or more of the following: 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.

[0147] 4. A method as described in Example 2, wherein the endothermic reaction includes one or more of the following: 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.

[0148] 5. A method as described in Example 2, wherein the autothermal reaction is selected from the group consisting of: autothermal reforming of natural gas and hydrocarbons, including a partial oxidation (POx) process 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.

[0149] 6. The method of any one of embodiments 1 to 5, wherein the physicochemical process comprises one or more of vapor compression evaporation and chemical adsorption processes, and preferably consists of them.

[0150] 7. The method of any one of embodiments 1 to 6, wherein the ambient heat transferred according to (ii) is heat from the environment, preferably heat from one or more of air, water and solar radiation, including combinations of two or more thereof.

[0151] 8. The method of any one of embodiments 1 to 7, wherein the heat transferred according to (ii) does not include energy from nuclear fission, solar thermal energy, geothermal energy, hydroelectric energy, and wind energy.

[0152] 9. The method of any one of embodiments 1 to 8, wherein transferring heat in (ii) comprises using a heat pump, wherein the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

[0153] 10. The method of embodiment 9, wherein the absorption heat pump is a conventional heat pump (Type I heat pump), a heat converter heat pump (Type II heat pump), or an adsorption heat pump, wherein the absorption heat pump is preferably a conventional heat pump.

[0154] 11. The method of embodiment 10, wherein the adsorption heat pump comprises an adsorbent, wherein the adsorbent comprises one or more of activated carbon, zeolite and mixtures thereof, and preferably consists of the same.

[0155] 12. A method as described in any one of embodiments 1 to 11, wherein the target process includes heating one or more compounds, preferably consists of the same, wherein preferably the target process includes a chemical conversion process and / or thermal separation of compounds, preferably consists of the same, wherein more preferably the target process includes one or more of a chemical reaction, evaporation, a preheating step and a crystallization process, including a combination of two or more thereof, wherein more preferably the target process includes distillation, preferably column distillation, an endothermic reaction, an exothermic reaction or an autothermal reaction, preferably consists of the same, wherein the target process preferably includes an endothermic reaction, preferably consists of the same.

[0156] 13. The method of embodiment 12, wherein the thermal separation of the compounds comprises, preferably consists of, separating isobutylene from a mixture comprising n-butene, 2-butene and isobutylene, preferably by distillation.

[0157] 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, γ-butyrolactone synthesis, and reforming,

[0158] wherein the cracking more preferably comprises cracking one or more of: steam, hydrocarbons, aliphatics, olefins (preferably one or more of ethylene, propylene and butene), dienes (preferably butadiene), acetylene, alicyclic compounds, naphtha, polymers, plastics, biomass, oily liquids, asphalt, tar urea, carbamates, preferably carbamates to olefins, aromatic compounds, fuels, isocyanates, melamine, and diamines,

[0159] wherein the dehydrogenation more preferably comprises the dehydrogenation of one or more of the following: hydrocarbons, more preferably one or more of ethane, propane, butane, pentane, hexane (preferably hexane to olefins), olefins (ethylene, propylene, butene), dienes (butadiene) and acetylene, aliphatic compounds, alicyclic compounds, naphtha, ethylbenzene, aromatic compounds and styrene,

[0160] wherein the dehydration more preferably comprises the dehydration of one or more of the following: alcohols, preferably one or more of ethanol, bioethanol, propanol and butanol, more preferably alcohols to olefins, preferably one or more of ethylene, propylene and butene,

[0161] wherein the thermal decomposition comprises one or more of pyrolysis, thermal decomposition, and gasification, more preferably the thermal decomposition of one or more of the following: polymers, plastics, biomass, waste, oily liquids, asphalt, tar to olefins, olefins (preferably one or more of ethylene, propylene and butene), dienes (preferably butadiene), acetylene, monomers, aromatic compounds, fuels and synthesis gas,

[0162] wherein one or more of the dimerization and oligomerization comprises dimerization or oligomerization of olefins, preferably one or more of ethylene, butene and hexene, more preferably to diolefins or oligomerized olefins,

[0163] wherein the reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, production of synthesis gas, and NH3 reforming,

[0164] The endothermic reaction more preferably comprises, and more preferably consists of, NH3 reforming.

[0165] 15. The method of embodiment 12, wherein the endothermic reaction comprises, preferably consists of, the dehydration of ethanol, and wherein the chemical process from which heat is transferred in (ii) comprises the production of ethylene oxide, preferably from ethylene.

[0166] 16. A method as described in Example 12, wherein the endothermic reaction comprises, preferably consists of, steam methane reforming, wherein the steam methane reforming is preferably carried out at 700°C to 1100°C, more preferably steam methane reforming to produce synthesis gas containing CO and hydrogen.

[0167] 17. A method as described in Example 12, wherein the endothermic reaction comprises, preferably consists of, steam cracking, wherein the steam cracking is preferably carried out at about 850°C to about 900°C, more preferably steam cracking of naphtha to olefins, methane and hydrogen.

[0168] 18. A method as described in Example 12, wherein the exothermic reaction comprises one or more of the following, preferably consists 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.

[0169] 19. 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) of hydrocarbons, wherein the hydrocarbons are selected from (C1-C 10 )alkanes, more preferably (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0170] 20. The method of any one of embodiments 1 to 19, wherein T1 is in the range of 20°C to 1,150°C, preferably in the range of 80°C to 1,100°C, more preferably in the range of 200°C to 1,000°C, more preferably in the range of 400°C to 800°C, more preferably in the range of 500°C to 600°C.

[0171] 21. The method of any one of embodiments 1 to 19, wherein T2 is in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, more preferably in the range of 450°C to 1175°C, more preferably in the range of 550°C to 1,075°C.

[0172] 22. 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 1 to 300 bar (absolute), preferably in the range of 5 to 250 bar (absolute), more preferably in the range of 10 to 200 bar (absolute), more preferably in the range of 20 to 150 bar (absolute), more preferably in the range of 50 to 100 bar (absolute).

[0173] 23. The method of any one of embodiments 1 to 22, wherein the first process stream provided in (i) has a flow rate of 200 to 20,000 h. -1 In the range of 400 to 15,000h -1 , more preferably 600 to 10,000h -1 , more preferably 1,000 to 5,000h -1 The weight hourly space velocity is within the range of .

[0174] 24. The method of any one of embodiments 1 to 23, wherein transferring heat in (ii) comprises:

[0175] (ii.a) providing heat from a chemical conversion process, a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature T3;

[0176] (ii.b) transferring the heat provided in (ii.a) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2;

[0177] wherein T3 < T1, and wherein T3 is preferably in the range of 255 °C to 700 °C.

[0178] 25. The method according to embodiment 24, wherein the heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and / or a physicochemical process, wherein the process stream from the chemical conversion process and / or the physicochemical process preferably comprises one or more of steam from a steam generation process, flue gas, preferably flue gas.

[0179] 26. The method according to embodiment 24 or 25, wherein the heat transfer according to (ii.b) is carried out 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, and 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).

[0180] 27. The method according to any one of embodiments 24 to 26, wherein the target process comprises NH3 reforming, and wherein the heat transfer according to (ii.b) comprises at least partially converting NH3 into H2 and N2.

[0181] 28. The method according to 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 350 °C to 1,225 °C, more preferably in the range greater than 350 °C to 1,225 °C, more preferably in the range of 375 °C to 1,225 °C, preferably in the range of 450 °C to 1,175 °C, more preferably in the range of 550 °C to 1,075 °C.

[0182] 29. The method according to any one of embodiments 24 to 28, wherein the heated first process stream obtained in (ii.b) has a pressure in the range of 0.01 to 300 bar (absolute), preferably in the range of 1 to 275 bar (absolute), more preferably in the range of 5 to 250 bar (absolute), more preferably 10 to 200 bar (absolute), more preferably 20 to 150 bar (absolute), more preferably 50 to 100 bar (absolute).

[0183] 30. The method according to any one of embodiments 1 to 29, wherein the heat transfer in (ii) comprises:

[0184] (ii.1) providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature T3, wherein T3 is in the range of 255°C to 700°C;

[0185] (ii.2) providing a stream (10) comprising a heat transfer medium, wherein the stream (10) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 250° C.;

[0186] (ii.3) transferring the heat (4) provided in (ii.1) to the stream (10) provided in (ii.2) to obtain a heated stream (11);

[0187] (ii.4) increasing the pressure of the heated stream (11) obtained in (ii.3) to obtain a compressed heated stream (7) having a temperature in the range of 400° C. to 1,400° C.;

[0188] (ii.5) transferring heat from the compressed heated stream (7) obtained in (ii.4) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8).

[0189] 31. The method of embodiment 30, further comprising

[0190] (ii.6) expanding the compressed flow (8) obtained in (ii.5);

[0191] (ii.7) Optionally recycling at least a portion of the stream obtained in (ii.6) to (ii.2).

[0192] 32. A method as described in Example 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-trifluoropropene, 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, rare gases, preferably one or more of helium, neon, argon, krypton and xenon, tetraphenyl compounds, and mixtures of two or more thereof.

[0193] 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 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0194] 34. A method as described in any of Examples 30 to 33, wherein the stream provided in (ii.2) has a pressure in the range of 0.1 bar (absolute value) to 50 bar (absolute value), preferably in the range of 0.5 bar (absolute value) to 30 bar (absolute value), and more preferably in the range of 1 bar (absolute value) to 20 bar (absolute value).

[0195] 35. The method of any one of embodiments 30 to 34, wherein 95 to 100 Vol-%, preferably 99 to 100 Vol-%, more preferably 99.9 to 100 Vol-% of the stream provided in (ii.2) consists of the heat transfer medium.

[0196] 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 a liquid state.

[0197] 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 having a vapor phase and a liquid phase.

[0198] 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 a supercritical state.

[0199] 39. A method as described in any one of Examples 30 to 38, wherein the heat transferred in (ii.3) is carried out 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-walled heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a wall of a reactor containing the first process stream provided in (i), more preferably a reactor containing the first process stream provided in (i).

[0200] 40. A method as described in any of Examples 30 to 39, wherein the heat provided in (ii.1) is obtained from a process stream from a chemical conversion process and / or a physicochemical process, wherein the process stream from a chemical conversion process and / or a physicochemical process preferably comprises one or more of steam from a steam generation process, flue gas, preferably flue gas.

[0201] 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 200°C to 700°C, preferably in the range of 250°C to 650°C, more preferably in the range of 350°C to 550°C.

[0202] 42. The method of any one of embodiments 30 to 41, wherein the heated stream obtained in (ii.3) is in a superheated vapor state.

[0203] 43. The method of any one of embodiments 30 to 42, wherein the heated stream obtained in (ii.3) is in a supercritical state.

[0204] 44. The method of any one of embodiments 30 to 43, wherein increasing the pressure of the stream according to (ii.4) is performed using a compressor (12).

[0205] 45. A method as described in any of Examples 30 to 44, wherein increasing the pressure of the flow according to (ii.4) is carried out using a multi-stage compressor (12), which preferably contains 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.

[0206] 46. ​​The method of embodiment 45, wherein the multi-stage compressor comprises one or more stages, wherein each stage independently of one another comprises a temperature increase in the range of 20°C to 500°C, preferably in the range of 50°C to 200°C.

[0207] 47. The method of any one of embodiments 30 to 46, wherein increasing the pressure of the stream according to (ii.4) is performed under adiabatic conditions.

[0208] 48. A method as described in any of Examples 30 to 47, wherein transferring heat according to (ii.5) is carried out using a heat exchanger (2), wherein the heat exchanger preferably includes one or more of an internal or external coil, a jacket heater, a double-walled heat exchanger, an internal pipe heater, and a shell and tube heat exchanger, wherein the heat exchanger is preferably a wall of a reactor containing the first process stream provided in (i), more preferably a reactor containing the first process stream provided in (i).

[0209] 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 into H2 and N2.

[0210] 50. A method as described in any of Examples 30 to 49, wherein a compressed stream is obtained according to (ii.5), the compressed stream having a temperature in the range of 375°C to 1,400°C, preferably in the range of 475°C to 1,100°C, and more preferably in the range of 550°C to 1,000°C.

[0211] 51. A method as described in any of Examples 30 to 50, wherein a compressed stream is obtained according to (ii.5), the compressed stream having a pressure in the range of 1 to 300 bar (absolute value), preferably in the range of 5 to 250 bar (absolute value), more preferably 10 to 200 bar (absolute value), more preferably 20 to 150 bar (absolute value), more preferably 50 to 100 bar (absolute value).

[0212] 52. A method as described in any of Examples 30 to 51, wherein the heated first process stream obtained in (ii.5) has a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C.

[0213] 53. A method as described in any of Examples 30 to 52, wherein the heated first process stream obtained in (ii.5) has a pressure in the range of 0.01 to 300 bar (absolute value), preferably in the range of 1 to 275 bar (absolute value), more preferably in the range of 5 to 250 bar (absolute value), more preferably 10 to 200 bar (absolute value), more preferably 20 to 150 bar (absolute value), more preferably 50 to 100 bar (absolute value).

[0214] 54. A method as described in any one of Examples 31 to 53, wherein the method preferably includes (ii.6) and (ii.7) as defined in Example 31, wherein the expansion according to (ii.6) is performed using a thermal expansion valve (9) or an expansion turbine (9).

[0215] 55. A method as described in Example 54, wherein increasing the pressure of the flow according to (ii.4) is performed using a compressor (12), wherein the expansion is performed 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, more preferably via a shaft for directly transferring energy.

[0216] 56. A method as described in any one of Examples 31 to 55, wherein the method preferably includes (ii.6) and (ii.7) as defined in Example 31, wherein the expanded flow obtained in (ii.6) has the same pressure and temperature as the flow containing the heat transfer medium provided in (ii.2).

[0217] 57. The method of any one of Examples 31 to 56, wherein the method comprises (ii.6), and preferably (ii.7), as defined in Example 31, wherein the expansion of the compressed stream according to (ii.6) is performed under adiabatic conditions.

[0218] 58. A method as described in any one of Examples 31 to 57, wherein the method includes (ii.6) as defined in Example 31, and preferably (ii.7), wherein according to (ii.7), 1 to 100 vol-%, preferably 10 to 90 vol-%, more preferably 30 to 70 vol-% of the stream obtained in (ii.6) is recycled to (ii.2).

[0219] 59. The method of any one of embodiments 31 to 58, wherein the method preferably comprises (ii.6) as defined in embodiment 31, and preferably (ii.7), wherein the stream obtained in (vii) is completely recycled to (ii.2) according to (ii.7).

[0220] 60. The method of embodiment 59, wherein steps (ii.2) to (ii.7) are performed in a closed system in which the stream comprising the heat transfer medium is circulated.

[0221] 61. The method of any one of embodiments 1 to 60, further comprising (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) into a first reactor to obtain a first product stream.

[0222] 62. A method as described in Example 61, wherein the heated first process stream obtained in (ii.5) or (ii.b) is fed into the first reactor, and the heated first process stream has a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, preferably in the range of 450°C to 1,175°C, and more preferably in the range of 550°C to 1,075°C.

[0223] 63. The method of embodiment 61 or 62, wherein the heated first process stream obtained in (ii.5) or (ii.b) is fed to the first reactor, wherein the heated first process stream has a flow rate of 10 h. -1 Up to 50.000h-1 Within the range, preferably within 100h -1 Up to 20,000h -1 In the range of 1,000h -1 Up to 10,000h -1 Gas hourly space velocity in the range.

[0224] 64. A method as described in any one of Examples 61 to 63, wherein the method further comprises (iv) heating the first product stream obtained in (iii) to a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C, and feeding the heated first product stream into a second reactor to obtain a second product stream.

[0225] 65. A method as described in Example 64, wherein the method includes (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), wherein heating the first product stream according to (iv) includes transferring heat from the compressed stream obtained in (ii.4) to the first product stream obtained in (iii) to obtain a heated first product stream, and a compressed stream having a temperature in the range of 375°C to 1,400°C.

[0226] 66. The method of embodiment 64 or 65, wherein the first and second reactors are independently adiabatic reactors, isothermal reactors, or a combination thereof.

[0227] 67. The method of any one of embodiments 64 to 66, wherein the first and second reactors are independently tubular reactors.

[0228] 68. The method of any one of embodiments 1 to 67, wherein transferring heat in (ii) comprises:

[0229] (ii.1') providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature in the range of 255°C to 700°C;

[0230] (ii.2') providing a stream (10a) comprising a first heat transfer medium, wherein the stream (10a) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 250°C;

[0231] (ii.3') transferring heat from the heat (4) provided in (ii.1') to the stream (10a) provided in (ii.2) to obtain a heated stream (11a);

[0232] (ii.4') increasing the pressure of the heated stream (11a) obtained in (ii.3') to obtain a compressed heated stream (7a) having a temperature in the range of 400°C to 1,400°C;

[0233] (ii.5') providing a stream (10b) comprising a second heat transfer medium, wherein the stream (10b) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 275°C;

[0234] (ii.6') transferring heat from the compressed heated stream (7a) obtained in (ii.4') to the stream (10b) provided in (ii.5') to obtain a heated stream (11b) and a compressed stream (8a);

[0235] (ii.7') expanding the compressed flow (8a) obtained in (ii.6');

[0236] (ii.8') recycling at least a portion of the stream obtained in (ii.7') to (ii.2')

[0237] (ii.9') increasing the pressure of the heated stream (11b) obtained in (ii.6') to obtain a compressed heated stream (7b) having a temperature in the range of 400°C to 1,400°C;

[0238] (ii.10') transferring heat from the compressed heated stream (7b) obtained in (ii.9') to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8b);

[0239] (ii.11') expanding the compressed flow (8b) obtained in (ii.10');

[0240] (ii.12') Recirculating at least a portion of the stream obtained in (ii.11') to (ii.5').

[0241] 69. A method as described in Example 68, wherein the first heat transfer medium in (ii.2') and the second heat transfer medium in (ii.5') are independently 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-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, rare gases, preferably one or more of helium, neon, argon, krypton and xenon, tetraphenyl compounds, and mixtures of two or more thereof.

[0242] 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 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0243] 71. A method as described in any of Examples 68 to 70, wherein the heat provided in transferring (ii.1') is carried out using a heat exchanger (5), wherein the heat exchanger preferably includes 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.

[0244] 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 350°C to 950°C, preferably in the range of 400°C to 600°C, more preferably in the range of 450°C to 550°C.

[0245] 73. The method of any one of embodiments 68 to 72, wherein increasing the pressure of the heated stream (11a) is performed using a compressor (12a).

[0246] 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 325°C to 1,000°C, more preferably in the range of 375°C to 850°C, more preferably in the range of 450°C to 650°C, more preferably in the range of 500°C to 600°C.

[0247] 75. A method as described in any of Examples 68 to 74, wherein transferring heat from the compressed heating stream (7a) is performed using a heat exchanger (13), wherein the heat exchanger preferably includes 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.

[0248] 76. A method as described in any of Examples 68 to 75, wherein a compressed stream (8a) is obtained according to (ii.6'), the compressed stream having a temperature in the range of 355°C to 1,400°C, preferably in the range of 455°C to 655°C, more preferably in the range of 505°C to 605°C.

[0249] 77. The method of any one of embodiments 68 to 76, wherein the heated stream (11b) obtained in (ii.6') has a temperature in the range of 350°C to 1150°C, preferably in the range of 450°C to 650°C, more preferably in the range of 500°C to 600°C.

[0250] 78. The method of any one of embodiments 68 to 77, wherein increasing the pressure of the heated stream (11b) is performed using a compressor (12b).

[0251] 79. A method as described in any of Examples 68 to 78, wherein transferring heat from the compressed heating stream (7b) is performed using a heat exchanger (2), wherein the heat exchanger preferably includes 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.

[0252] 80. A method as described in any of embodiments 68 to 79, wherein the heated first process stream obtained in (ii.10') has a temperature in the range of 350°C to 1,225°C, preferably in the range of greater than 350°C to 1,225°C, more preferably in the range of 375°C to 1,225°C, preferably in the range of 450°C to 1,175°C, more preferably in the range of 550°C to 1,075°C.

[0253] 81. A method as described in any of Examples 68 to 80, wherein the expansion according to (ii.7') and (ii.11') is performed independently of each other using a thermal expansion valve (9a and / or 9b) or an expansion turbine (9a and / or 9b).

[0254] 82. The method of any one of embodiments 1 to 81, wherein the heated first process stream obtained in (ii) is used as a feed or co-feed to an endothermic reaction, preferably a high temperature endothermic reaction.

[0255] 83. A method as described in any one of embodiments 1 to 82, wherein the heated first process stream obtained in (ii) is used as a feed stream for an NH3 reforming process.

[0256] The present invention is further illustrated by the following reference examples.

[0257] Examples

[0258] Reference Example 1: Heat transfer method including Hg as a heat transfer medium

[0259] Figure 1 The circulation of the heat transfer medium mercury is schematically shown. This process concept is of particular interest when exothermic heat sources at low temperatures and heat absorbing heat sinks at higher temperatures are present within the production plant.

[0260] The COP is 4.27 and the volumetric heating capacity (VHC) is 8337 kJ / m 3 .

[0261] Heat is transferred to the Hg at the heat source, and heat is transferred from the Hg to the target process stream at the heat sink. BRIEF DESCRIPTION OF THE DRAWINGS

[0262] Figure 1 : shows a process scheme in which mercury is used as heat transfer medium.

[0263] Figure 2 : A method scheme of a thermodynamic cycle or heat pump process as a closed-loop process is shown.

[0264] Figure 3 : A method scheme of a two-stage thermodynamic cycle or a two-stage heat pump process is shown, wherein each stage comprises a closed-loop process.

[0265] Description of Reference Numerals

[0266] for Figure 2 :

[0267] (1) First process flow

[0268] (2) Heat exchanger

[0269] (3) Heating the first process stream

[0270] (4) Heat

[0271] (5) Heat exchanger

[0272] (6) Exhaust

[0273] (7) Compressed heating flow

[0274] (8) Compressed Stream

[0275] (9) Thermal expansion valve or expansion turbine

[0276] (10) Flow containing heat transfer medium

[0277] (11) Heating flow

[0278] (12) Compressor or multi-stage compressor

[0279] for Figure 3 :

[0280] (1) First process flow

[0281] (2) Heat exchanger

[0282] (3) Heating the first process stream

[0283] (4) Heat

[0284] (5) Heat exchanger

[0285] (6) Exhaust

[0286] (7a) Compressed heating flow

[0287] (8a) Compressed Stream

[0288] (9a) Thermal expansion valve or expansion turbine

[0289] (10a) A flow comprising a first heat transfer medium

[0290] (11a) Heated Flow

[0291] (12a) Compressor or multi-stage compressor

[0292] (13) Heat exchanger

[0293] (7b) Compressed heating flow

[0294] (8b) Compressed Stream

[0295] (9b) Thermal expansion valve or expansion turbine

[0296] (10b) A flow comprising a second heat transfer medium

[0297] (11b) Heated Flow

[0298] (12b) Compressor or multi-stage compressor

[0299] References:

[0300] -DE 2951188 A1

[0301] -DE 3209642 A1

[0302] - V. Singh et al., “Investigation of new mechanical heat pump systems for heat upgrading applications,” Int. J. Energy Ress., 2018, 42, 3078-3090

Claims

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 T1; (ii) transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to the first process stream provided in (i) to obtain a heated first process stream (3) having a temperature T2, wherein T2>T1; (iii) performing the target process using the heated first process stream obtained in (ii); wherein the target process is different from the chemical conversion process, the physicochemical process, or a combination of the chemical conversion process and the physicochemical process from which heat is transferred according to (ii).

2. The method of claim 1, wherein: In (ii) heat is transferred from a chemical conversion process and / or a physicochemical process and wherein the heat transferred according to (ii) is obtained from an exothermic reaction or wherein the heat transferred according to (ii) is excess heat to the heat for carrying out an autothermal reaction or an endothermic reaction.

3. The method according to claim 1 or 2, wherein: The heat transferred according to (ii) does not include energy from nuclear fission, solar thermal energy, geothermal energy, hydroelectric energy, and wind energy.

4. The method according to any one of claims 1 to 3, wherein: Transferring heat in (ii) includes using a heat pump, wherein the heat pump is selected from the group consisting of: a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

5. The method according to any one of claims 1 to 4, wherein: The subject process includes heating one or more compounds.

6. The method according to any one of claims 1 to 5, wherein: T1 is in the range of 20°C to 1,150°C.

7. The method according to any one of claims 1 to 6, wherein: T2 is in the range of 350°C to 1,225°C.

8. The method according to any one of claims 1 to 7, wherein: The heat transferred in (ii) includes: (ii.a) providing heat from a chemical conversion process, a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature T3; (ii.b) transferring the heat provided in (ii.a) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2, Among them, T3 <T1。 9. The method according to any one of claims 1 to 8, wherein: The heat transferred in (ii) includes: (ii.1) providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature in the range of 255°C to 700°C; (ii.2) providing a stream (10) comprising a heat transfer medium, wherein the stream (10) has a pressure in the range of 0.001 to 100 bar (absolute) and a temperature equal to or greater than 250° C.; (ii.3) transferring the heat (4) provided in (ii.1) to the stream (10) provided in (ii.2) to obtain a heated stream (11); (ii.4) increasing the pressure of the heated stream (11) obtained in (ii.3) to obtain a compressed heated stream (7) having a temperature in the range of 400° C. to 1,400° C.; (ii.5) transferring heat from the compressed heated stream (7) obtained in (ii.4) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8).

10. The method of claim 9, further comprising (ii.6) expanding the compressed flow (8) obtained in (ii.5); (ii.7) Optionally recycling at least a portion of the stream obtained in (ii.6) to (ii.2).

11. The method according to claim 9 or 10, wherein: The heat transfer medium is selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, hydrofluorocarbons, hydrocarbons, ammonia, water, carbon dioxide, nitrogen, oxygen, air, noble gases, tetraphenyl compounds, and mixtures of two or more thereof.

12. The method according to any one of claims 9 to 11, wherein: The heat transfer medium in the flow provided in (ii.2) is in a liquid state, or wherein the heat transfer medium in the flow provided in (ii.2) is a two-phase fluid having a vapor phase and a liquid phase, or wherein the heat transfer medium in the flow provided in (ii.2) is in a supercritical state.

13. The method according to any one of claims 9 to 12, wherein: The stream obtained in (vii) is completely recycled to (ii.2) according to (ii.7).

14. The method of claim 13, wherein: Steps (ii.2) to (ii.7) are carried out in a closed system in which the stream comprising the heat transfer medium is circulated.

15. The method according to any one of claims 1 to 14, wherein: The process further comprises (iii) feeding the heated first process stream obtained in (ii.5) into a first reactor to obtain a first product stream.

16. The method according to any one of claims 1 to 15, wherein: The heat transferred in (ii) includes: (ii.1') providing heat from a chemical conversion process, a physicochemical process (4), or providing ambient heat, or providing a combination of two or more thereof, the heat having a temperature in the range of 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 0.001 to 100 bar (absolute) 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) to obtain a heated stream (11a); (ii.4') increasing the pressure of the heated stream (11a) obtained in (ii.3') to obtain a compressed heated stream (7a) having a temperature in the range of 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 0.001 to 100 bar (absolute) 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') to obtain a heated stream (11b) and a compressed stream (8a); (ii.7') expanding the compressed flow (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 (11b) obtained in (ii.6') to obtain a compressed heated stream (7b) having a temperature in the range of 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) to obtain a heated first process stream (3) having a temperature T2 and a compressed stream (8b); (ii.11') expanding the compressed flow (8b) obtained in (ii.10'); (ii.12') Recirculating at least a portion of the stream obtained in (ii.11') to (ii.5').

17. The method according to any one of claims 1 to 16, wherein: The heated first process stream obtained in (ii) is used as feed or co-feed to the endothermic reaction.

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