A method for transferring heat between two independent processes

Abstract

The present invention relates to a method for transferring heat to a target process in a chemical manufacturing plant, comprising the steps of: (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, where T2>T1; and (iii) carrying out the target process using the heated first process stream obtained in (ii), wherein the target process is different from the chemical conversion process, physicochemical process, or combination of chemical conversion process and physicochemical process from which heat is transferred in (ii). The method of the present invention allows a coefficient of performance greater than 1 to be achieved.

Description

[Technical Field]

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

[0002] Providing thermal energy for endothermic processes is currently done by burning fossil fuels or by direct electrical heating, which is often preferred over direct electrical heating due to its lower efficiency and therefore lower cost.

[0003] Heat pumps achieve a temperature level increase of a calorie much greater than the amount of electrical energy used by the smart use of electrical energy in a thermodynamic cycle. For a temperature level increase according to the Carnot cycle, the coefficient of performance (COP) is calculated according to formula I: ε Carnot-WP =1 / (1-T low / T high ) (I), (In the formula, ε Carnot-WP is the coefficient of performance of the Carnot cycle of the heat pump, and T low is the absolute temperature (Kelvin) at which heat is absorbed, and T high is the absolute temperature at which heat is released). The latter temperature must be at least equal to the temperature at which the heating process takes place.

[0004] Until now, heat pumps have been used and designed to provide heat at a maximum temperature of about 150 °C. Many technologically relevant processes require large amounts of heat at temperatures significantly above this value. Examples include melting metals, distillation processes, and endothermic chemical reactions. For thermodynamic reasons, endothermic chemical reactions typically take place at high temperatures.

[0005] DE 2951188 A1 relates to a method for utilizing waste heat from an endothermic process, in which heat is initially supplied at a high temperature level from an external heat source, residual heat from the reaction is obtained at a low temperature level, and the low temperature residual heat is recycled to the endothermic reaction by means of a heat pump.

[0006] DE 3209642 A1 discloses a process heat plant for the joint production of high-temperature heat and process steam.

[0007] V. Singh et al., "Investigation of new mechanical heat pump systems for heat upgrading applications," Int. J. Energy Ress. 2018, 42, 3078-3090, discloses an example of a multi-stage ultra-high temperature heat pump with different heat transfer media that can be used in process engineering processes, among other applications.

[0008] Therefore, in the process of converting technological processes to sustainable energy sources, it is desirable to further increase the temperature levels achieved so far by heat pumps in order to reduce dependence on other energy sources for processes requiring high levels of heat.

[0009] 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 therefore, theoretically, almost twice as much heat can be provided for the reaction as if the power used to operate the heat pump were used directly for heating. Typically, the COP is significantly lower at 1.5, but the use of a heat pump can still be considered, for example, when steam is no longer available for the process due to temperature and pressure levels, or is only available with extreme difficulty.

[0010] An important application area for very high temperature heat pumps is the valorization of heat energy that is already available at high temperatures, for example around 300°C. The theoretically possible efficiency (approximately COPCarnot = 1 / (1-(773 K / 973 K)) = 4.5), these heat pumps are suitable for heat utilization at much higher temperatures above 600°C. [Prior art documents] [Patent documents]

[0011] [Patent Document 1] DE 2951188 A1 [Patent Document 2] DE 3209642 [Non-patent literature]

[0012] [Non-Patent Document 1] V. Singh et al. “Investigation of new mechanical heat pump systems for heat upgrading applications” Int.J.Energy Ress.2018,42,3078-3090 Summary of the Invention [Problem to be solved by the invention]

[0013] It was therefore an object of the present invention to provide a method in which the utilization of heat, such as with a heat pump, is not limited to the optimization of individual heat-consuming processes, for example endothermic reactions, or to the valorization of primary energy sources, in particular sustainable energy sources or nuclear energy. In particular, it was an object of the present invention to utilize a heat transfer concept involving the valorization of heat not originating from a primary energy source, in particular the valorization of waste heat or other available low-temperature heat. [Means for solving the problem]

[0014] Thus, it has been surprisingly found that a low-temperature heat source, for example, between 20°C and 80°C, can be used to upgrade to usable thermal energy at temperatures above 350°C, preferably above 350°C, more preferably above 375°C, thereby achieving a coefficient of performance (COP) of greater than 1. In particular, it has been unexpectedly found that the use of heat pump cascades is particularly advantageous for achieving energy efficiency and reducing dependency from primary energy sources, regardless of whether they are sustainable or not. Thus, by appropriately selecting the heat transfer medium, it is possible to upgrade the heat source to directly supply heat to a process at temperatures above 350°C, preferably above 350°C, more preferably between 375 and 1,275°C, for example, by superheated saturated steam, to provide the temperature required for the target process. In particular, the use of high-temperature heat pumps allows the electrification of processes where electrical heating is difficult to achieve, resulting in better electrical efficiency, particularly a COP of greater than 1. real It was found to have the following structure:

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

[0016] Aside from the leverage effect of a COP > 1, the use of heat pumps can also be considered when reaction temperatures are too high to achieve a practical COP > 1. This is the case when conventional heating concepts are problematic due to the high temperatures and power requirements (e.g., due to the very high currents at the relatively low voltages of resistance heaters) or when the use of conventional process steam is no longer possible at temperatures > 290 °C. Compressors used in heat pumps can operate at medium or high voltages, thus avoiding damage to electrical equipment, transformer losses, and high currents. In contrast, the conventional use of electric heaters at very high temperatures often requires an indirect heating concept, where heat is transferred from the electric heater to the process via radiation. This often leads to uneven temperature profiles and increased equipment requirements.

[0017] If a device needs to be cooled over a wide temperature range with a ΔT of more than 50°C and is therefore available as a heat source (e.g., cooled from about 350°C to 250°C), a two-stage heat pump using the same working fluid offers advantages in terms of electrical efficiency, as it does not require the higher temperature circuit to be reduced to a lower temperature and pressure level. In this case, the heat source is tapped at two different temperature levels (about 350°C to 300°C and 300°C to 250°C). A three-stage process is also possible, but this increases the complexity of the system.

[0018] The method of the present invention is not limited to endothermic reactions. Often, exothermic reactions are followed by energy-intensive separation steps / distillations that use waste heat from the preceding reaction as a heat source and can still benefit from the method of the present invention. In these cases, the high-temperature heat pump can also function as a high-temperature heat storage.

[0019] Accordingly, the present invention provides a method for transferring heat to a target process in a chemical manufacturing plant, the method comprising: (i) providing a first process stream (1) having a temperature T1; (ii) transferring heat from a chemical conversion process, from a physicochemical process, or from ambient heat, or from a combination of two or more thereof, to the first process stream provided in (i) to obtain a heated first process stream (3) having a temperature T2, where T2>T1; (iii) performing a target process using the heated first process stream obtained in (ii); Including, the target process is different from the chemical conversion process, physicochemical process, or combination of chemical conversion process and physicochemical process from which heat is transferred by (ii).

[0020] Within the meaning of the present invention, the term "different" with respect to the chemical conversion process and / or physicochemical process in (ii) means different from the target process, indicating that the method of the present invention does not recycle heat to the chemical conversion process and / or physicochemical process. Thus, according to certain embodiments or methods of the present invention, the chemical conversion process and / or physicochemical process in (ii) can be the same as the target process, but are not identical in the sense that the heat generated from a particular chemical conversion process and / or physicochemical process can be recycled to the same chemical conversion process and / or physicochemical process in a different process, rather than to the chemical conversion process and / or physicochemical process that generated the heat. However, according to certain preferred embodiments of the present invention, it is preferred that the target process is a chemical conversion process and / or physicochemical process, and that the chemical conversion process and / or physicochemical process in (ii) is not the same chemical conversion process and / or physicochemical process as the target process.

[0021] Preferably, heat is transferred in (ii) from a chemical conversion process and / or a physicochemical process, and the heat transferred by (ii) is obtained from an exothermic reaction, or the heat transferred by (ii) is surplus heat of the heat used to carry out an autothermal or endothermic reaction.

[0022] If heat is transferred in (ii) from a chemical conversion process and / or a physicochemical process and the heat transferred by (ii) is obtained from an exothermic reaction or the heat transferred by (ii) is surplus heat of the heat used to carry out an autothermal or endothermic reaction, according to a first alternative, it is preferred that the exothermic reaction comprises one or more of 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 to acrolein or acrylic acid, preferably the selective oxidation of one or more of alkanes, alkenes and alkynes to acrolein or acrylic acid.

[0023] Furthermore, if heat is transferred in (ii) from a chemical conversion process and / or a physicochemical process, and the heat transferred by (ii) is obtained from an exothermic reaction or is surplus heat to that used to carry out an autothermal or endothermic reaction, then according to a second alternative, the endothermic reaction preferably comprises one or more of steam cracking, ethane dehydrogenation, propane dehydrogenation, butane dehydrogenation, steam reforming, dry reforming, styrene production, methanol reforming, dimethyl ether reforming, reverse water gas shift, alcohol dehydration, and NH3 reforming.

[0024] Furthermore, if heat is transferred in (ii) from a chemical conversion process and / or a physicochemical process, and the heat transferred by (ii) is obtained from an exothermic reaction, or the heat transferred by (ii) is excess heat of the heat used to carry out an autothermal or endothermic reaction, according to a third alternative, the autothermal reaction is preferably selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, and the hydrocarbons are preferably selected from the group consisting of (C1-C10) alkanes, more preferably (C1-C8) alkanes, more preferably (C1-C7) alkanes.

[0025] Preferably, the physicochemical process comprises, preferably consists of, one or more of vapor compression evaporation and chemisorption processes.

[0026] The ambient heat transferred by (ii) is preferably heat from the environment, preferably from one or more (including a combination of two or more) of air, water, and solar radiation.

[0027] Preferably, the heat transferred by (ii) does not include energy from nuclear fission, solar thermal energy, geothermal energy, hydroelectric energy, and wind energy.

[0028] Therefore, the process according to the invention does not relate to the optimization of a single process with regard to its energy efficiency. In particular, the invention does not relate to a process in which energy is recycled in order to optimize the efficiency of the energy conversion. Furthermore, the process according to the invention does not relate to a process in which the energy for transferring heat comes from a pure energy source.

[0029] Preferably, the step of transferring heat in (ii) comprises the use of a heat pump, the heat pump being selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

[0030] If the step of transferring heat in (ii) includes the use of a heat pump, the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump, and the absorption heat pump is preferably a conventional heat pump (Type I heat pump), a heat transformer heat pump (Type II heat pump), or an adsorption heat pump, and the absorption heat pump is preferably a conventional heat pump.

[0031] When the absorption heat pump is a conventional heat pump (Type I heat pump), a heat transformer heat pump (Type II heat pump), or an adsorption heat pump, the adsorption heat pump comprises an adsorbent, which preferably comprises, preferably consists of, one or more of activated carbon, zeolite, and mixtures thereof.

[0032] The target process comprises, preferably consists of, heating of one or more compounds; preferably, the target process comprises, preferably consists of, a chemical conversion process and / or a thermal separation of compounds; more preferably, the target process comprises one or more (including a combination of two or more) of a chemical reaction, evaporation, a preheating step, and a crystallization process; more preferably, the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction; preferably, the target process comprises, preferably consists of, an endothermic reaction.

[0033] If the target process comprises, preferably consists of, the heating of one or more compounds, then preferably the target process comprises, preferably consists of, a chemical conversion process and / or thermal separation of the compounds, and preferably the thermal separation of the compounds comprises, preferably consists of, the isolation of isobutene from a mixture comprising n-butene, 2-butene and isobutene, preferably by distillation.

[0034] When the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic, exothermic, or autothermal reaction, the endothermic reaction comprises, and preferably consists of, one or more of cracking, preferably catalytic cracking, dehydrogenation, styrene production, reverse water gas shift, dehydration, thermal cracking, dimerization, oligomerization, gamma-butyrolactone synthesis, and reforming; The cracking more preferably comprises the cracking of one or more of steam, hydrocarbons, aliphatics, alkenes, preferably ethylene, propylene and butylene, dienes, preferably butadiene, acetylene, cycloaliphatics, naphtha, polymers, plastics, biomass, oily liquids, bitumen, tar urea, carbamates, preferably carbamates, to olefins, aromatics, fuels, isocyanates, melamine and diamines; Dehydrogenation more preferably includes the dehydrogenation of one or more of hydrocarbons, more preferably one or more of ethane, propane, butane, pentane, hexane, preferably hexane, to olefins, alkenes (ethylene, propylene, butylene), dienes (butadiene), as well as acetylenes, aliphatics, cycloaliphatics, naphtha, ethylbenzene, aromatics and styrene; The dehydration more preferably comprises the dehydration of one or more of alcohols, preferably one or more of ethanol, bioethanol, propanol and butanol, more preferably the dehydration of alcohols to alkenes, preferably one or more of ethylene, propylene and butylene; Pyrolysis includes one or more of pyrolysis, thermal dissociation, gasification, more preferably pyrolysis of one or more of polymers, plastics, biomass, waste, oil-containing liquids, bitumen, tar, olefins, alkenes, preferably one or more of ethylene, propylene and butylene, dienes, preferably butadiene, acetylene, monomers, aromatics, fuels and synthesis gas; the one or more of dimerization and oligomerization includes dimerization or oligomerization to one or more of alkenes, preferably ethylene, butylene, and hexene, more preferably to a dialken or oligoalkene; The reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, synthesis gas production, and NH3 reforming; Preferably, the endothermic reaction comprises, more preferably consists of, NH3 reforming.

[0035] Furthermore, where the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic, exothermic, or autothermal reaction, it is preferred that the endothermic reaction comprises, preferably consists of, the dehydration of ethanol, and that the chemical process from which heat is transferred in (ii) preferably comprises the production of ethylene oxide from ethylene.

[0036] Furthermore, when the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, the endothermic reaction comprises, preferably consists of, steam methane reforming, the steam methane reforming preferably being carried out at 700-1100°C, more preferably steam methane reforming to synthesis gas containing CO and hydrogen.

[0037] Furthermore, when the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic, exothermic, or autothermal reaction, the endothermic reaction preferably comprises, preferably consists of, steam cracking, which is preferably carried out at about 850 to about 900°C, more preferably steam cracking of naphtha to olefins, methane, and hydrogen.

[0038] Furthermore, when the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic, exothermic, or autothermal reaction, it is preferred that the exothermic reaction comprises, preferably consists of, one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid, preferably the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid.

[0039] Furthermore, when the target process comprises, preferably consists of, a distillation, preferably a column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction, the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation (POx) processes of hydrocarbons, and the hydrocarbons are selected from the group consisting of (C1-C 10 )alkanes, more preferably (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0040] T1 is preferably in the range of 20 to 1,150°C, more preferably in the range of 80 to 1,100°C, more preferably in the range of 200 to 1,000°C, more preferably in the range of 400 to 800°C, and more preferably in the range of 500 to 600°C.

[0041] T2 is preferably in the range of 350 to 1,225°C, preferably in the range of over 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 to 1,175°C, and more preferably in the range of 550 to 1,075°C.

[0042] Preferably, the first process stream provided in (i) has a pressure in the range of 1 to 300 bar (abs), more preferably 5 to 250 bar (abs), more preferably 10 to 200 bar (abs), more preferably 20 to 150 bar (abs), more preferably 50 to 100 bar (abs).

[0043] The first process stream provided in (i) is -1 range, more preferably 400 to 15,000 h -1 , more preferably 600 to 10,000 h -1 , more preferably 1,000 to 5,000 h -1 It is preferred that the weight hourly space velocity be in the range of

[0044] The step of transferring heat in (ii) comprises: (ii.a) Providing heat from a chemical conversion process, a physicochemical process, or ambient heat having a temperature T3, or a combination of two or more thereof; (ii.b) Transmitting 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; comprising T3 < T1, and T3 is preferably in the range of 255 °C to 700 °C.

[0045] When the method includes (ii.a) and (ii.b), the heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and / or a process stream from a physicochemical process, and the process stream from a chemical conversion process and / or the process stream from a physicochemical process preferably includes one or more of steam from a steam generation process and flue gas, more preferably flue gas.

[0046] Furthermore, when the method includes (ii.a) and (ii.b), the heat transfer in (ii.b) is carried out using a heat exchanger (2), and 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 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).

[0047] Furthermore, when the method includes (ii.a) and (ii.b), the target process includes NH3 reforming, and the heat transfer in (ii.b) preferably includes the step of at least partially converting NH3 into H2 and N2.

[0048] Furthermore, when the method comprises (ii.a) and (ii.b), it is preferred that the heated first process stream obtained in (ii.b) has a temperature T2, wherein T2 is more preferably in the range of 350 to 1,225°C, more preferably in the range of above 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0049] Furthermore, when the method comprises (ii.a) and (ii.b), it is preferred that the heated first process stream obtained in (ii.b) has a pressure in the range of 0.01 to 300 bar (abs), more preferably in the range of 1 to 275 bar (abs), more preferably in the range of 5 to 250 bar (abs), more preferably in the range of 10 to 200 bar (abs), more preferably in the range of 20 to 150 bar (abs), more preferably in the range of 50 to 100 bar (abs).

[0050] The step of transferring heat in (ii) comprises: (ii.1) providing heat (4) from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, having a temperature T3, wherein T3 is in the range of 255°C to 700°C; (ii.2) providing a stream (10) comprising a heat transfer medium, the stream (10) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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); It is preferred that the compound contains:

[0051] When the step of transferring heat in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), and (ii.5), the method further comprises: (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); It is preferred that the composition further comprises:

[0052] Furthermore, when the step of 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), the heat transfer medium may be selected from mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene. Preferably, the fluorocarbon is selected from the group consisting of one or more of: pentafluoropropene, hydrofluorocarbons, preferably one or more of hydrofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene; one or more of 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.

[0053] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the stream provided in (ii.2) has a temperature of 300°C or above, more preferably in the range of 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0054] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the stream provided in (ii.2) has a pressure in the range of 0.1 bar(abs) to 50 bar(abs), more preferably in the range of 0.5 bar(abs) to 30 bar(abs), more preferably in the range of 1 bar(abs) to 20 bar(abs).

[0055] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that 95-100% by volume, more preferably 99-100% by volume, more preferably 99.9-100% by volume of the stream provided in (ii.2) consists of the heat transfer medium.

[0056] Furthermore, when the step of 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), the heat transfer medium in the stream provided in (ii.2) is preferably in a liquid state.

[0057] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the heat transfer medium in the flow provided in (ii.2) is preferably a two-phase fluid having a gas phase and a liquid phase.

[0058] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the heat transfer medium in the stream provided in (ii.2) is preferably in a supercritical state.

[0059] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the heat transfer in (ii.3) is carried out using a heat exchanger (5), which 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 the heat exchanger is preferably the reactor containing the first process stream provided in (i), more preferably the wall of the reactor containing the first process stream provided in (i).

[0060] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the heat provided in (ii.1) is obtained from a process stream from a chemical conversion process and / or a process stream from a physicochemical process, and that the process stream from the chemical conversion process and / or the process stream from the physicochemical process preferably comprises one or more of steam, flue gas, preferably flue gas from a steam generation process.

[0061] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the heat flow 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.

[0062] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the heated stream obtained in (ii.3) is preferably in a superheated vapor state.

[0063] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the heated stream obtained in (ii.3) is preferably in a supercritical state.

[0064] Furthermore, when the step of 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), the increase in pressure of the stream according to (ii.4) is preferably performed using a compressor (12).

[0065] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the increasing of the pressure of the flow according to (ii.4) is carried out using a multi-stage compressor (12), which preferably comprises one or more working media, preferably one or two working media, and the two working media are preferably chemically and / or physically different from each other.

[0066] If the increase in the pressure of the stream 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, each of which, independently of one another, comprises a temperature increase in the range of 20 to 500°C, more preferably in the range of 50 to 200°C.

[0067] Furthermore, when the step of 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 increase in the pressure of the stream by (ii.4) is carried out adiabatically.

[0068] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the transfer of heat according to (ii.5) is carried out using a heat exchanger (2), which more preferably comprises one or more of an internal or external coil, a jacket heater, a double-wall heat exchanger, an internal pipe heater, and a shell-and-tube heat exchanger, and the heat exchanger is preferably the reactor containing the first process stream provided in (i), more preferably the wall of the reactor containing the first process stream provided in (i).

[0069] Furthermore, when the step of 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), the target process includes NH3 reforming, and the heat transfer according to (ii.5) preferably includes converting NH3 at least partially to H2 and N2.

[0070] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), preferably (ii.5) results in a compressed stream having a temperature in the range of 375°C to 1,400°C, more preferably in the range of 475°C to 1,100°C, more preferably in the range of 550°C to 1,000°C.

[0071] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that according to (ii.5) a compressed stream is obtained having a pressure in the range of 1 to 300 bar (abs), more preferably 5 to 250 bar (abs), more preferably 10 to 200 bar (abs), more preferably 20 to 150 bar (abs), more preferably 50 to 100 bar (abs).

[0072] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the heated first process stream obtained in (ii.5) has a temperature in the range of 350 to 1,225°C, preferably in the range of above 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0073] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), preferably (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the heated first process stream obtained in (ii.5) has a pressure in the range of 0.01 to 300 bar (abs), more preferably in the range of 1 to 275 bar (abs), more preferably in the range of 5 to 250 bar (abs), more preferably in the range of 10 to 200 bar (abs), more preferably in the range of 20 to 150 bar (abs), more preferably in the range of 50 to 100 bar (abs).

[0074] Furthermore, when the step of transferring heat in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the expansion according to (ii.6) is preferably performed using a thermal expansion valve (9) or an expansion turbine (9).

[0075] Preferably, if the expansion according to (ii.6) is performed using a turbine (9), the increase in the pressure of the flow according to (ii.4) is performed using a compressor (12) and the expansion is performed using an expansion turbine, and the energy obtained from the expansion turbine is preferably obtained as electricity and used to operate the compressor, or the energy obtained from the expansion turbine is used to operate the compressor mechanically, more preferably via a shaft for direct energy transfer.

[0076] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the expanded stream obtained in (ii.6) has the same pressure and temperature as the stream containing the heat transfer medium provided in (ii.2).

[0077] Furthermore, when the step of transferring heat in (ii) includes (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), the expansion of the compressed stream according to (ii.6) is preferably carried out adiabatically.

[0078] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that 1 to 100% by volume, more preferably 10 to 90% by volume, more preferably 30 to 70% by volume of the stream obtained in (ii.6) is recycled to (ii.2) via (ii.7).

[0079] Furthermore, when the step of transferring heat in (ii) comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6) and (ii.7), it is preferred that the stream obtained in (vii) is fully recycled to (ii.2) by (ii.7).

[0080] If the stream obtained in (vii) is completely recycled to (ii.2) by (ii.7), steps (ii.2) to (ii.7) are preferably carried out in a closed system in which a stream containing the heat transfer medium is circulated.

[0081] Preferably, the process further comprising (ii.1), (ii.2), (ii.3), (ii.4), (ii.5) further comprises the step of (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) to a first reactor to obtain a first product stream.

[0082] If the process further comprises the step of (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) to a first reactor to obtain a first product stream, it is preferred that the heated first process stream obtained in (ii.5) is fed to the first reactor having a temperature in the range of from 350 to 1,225°C, preferably in the range of from above 350°C to 1,225°C, more preferably in the range of from 375°C to 1,225°C, more preferably in the range of from 450 to 1,175°C, more preferably in the range of from 550 to 1,075°C.

[0083] Furthermore, when the method further comprises the step of (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) to a first reactor to obtain a first product stream, the heated first process stream obtained in (ii.5) is -1 ~50,000 hours -1 in the range of 100 h -1 ~20,000 hours -1 range, more preferably 1,000 h -1 ~10,000 hours -1It is preferred that the first reactor has a gas hourly space velocity in the range of

[0084] Furthermore, when the method further comprises the step of (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) to a first reactor to obtain a first product stream, it is preferred that the method further comprises the step of (iv) heating the first product stream obtained in (iii) to a temperature in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C, and feeding the heated first product stream to a second reactor to obtain a second product stream.

[0085] If the method further comprises (iv), then heating the first product stream in (iv) preferably 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.

[0086] Furthermore, when the method further comprises (iv), the first and second reactors are preferably, independently of each other, adiabatic reactors, isothermal reactors, or a combination thereof.

[0087] In the context of the present invention, an adiabatic or isothermal change of state is to be understood as a change of state that approximates a theoretical adiabatic or isothermal process.

[0088] Furthermore, when the method further comprises (iv), the first and second reactors are preferably, independently of each other, tubular reactors.

[0089] The step of transferring heat in (ii) comprises: (ii.1') providing heat (4) from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, having a temperature in the range of 255°C to 700°C; (ii.2') providing a stream (10a) comprising a first heat transfer medium, the stream (10a) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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, the stream (10b) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 275°C or greater; (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') A step of expanding the compressed stream (8a) obtained in (ii.6'); (ii.8') recycling at least a portion of the stream obtained in (ii.7') to (ii.2'); (ii.9') Increasing the pressure of the heated stream (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 stream (8b) obtained in (ii.10'); (ii.12') recycling at least a portion of the stream obtained in (ii.11') to (ii.5'); It is preferred that the compound contains:

[0090] When the step of transferring heat in (ii) comprises (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′), the first heat transfer medium in (ii.2′) and the second heat transfer medium in (ii.5′) are, independently of each other, mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene, and Preferably, the hydrocarbon is selected from the group consisting of trans-1-chloro-3,3,3-trifluoropropene, hydrofluorocarbons, preferably one or more of hydrofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, one or more of 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.

[0091] Furthermore, when the step of transferring heat in (ii) comprises steps (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 of 300°C or higher, more preferably in the range of 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0092] Furthermore, when the step of transferring heat 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'), the transfer of the heat provided in (ii.1') is carried out using a heat exchanger (5), which 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.

[0093] Furthermore, when the step of transferring heat in (ii) comprises (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 flow 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, more preferably in the range of 450°C to 550°C.

[0094] Furthermore, when the step of transferring heat in (ii) comprises steps (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′), the increase in pressure of the heated stream (11a) is preferably performed using a compressor (12a).

[0095] Furthermore, when the heat transferring step in (ii) comprises steps (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 of 325°C or higher, more preferably in the range of 325 to 1,000°C, more preferably in the range of 375 to 850°C, more preferably in the range of 450 to 650°C, more preferably in the range of 500 to 600°C.

[0096] Furthermore, when the step of transferring heat 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′), the heat transfer from the compressed heated stream (7a) is carried out using a heat exchanger (13), which 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.

[0097] Furthermore, when the step of transferring heat in (ii) comprises steps (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 according to step (ii.6') a compressed stream (8a) is obtained having a temperature in the range of 355°C to 1,400°C, more preferably in the range of 455°C to 655°C, more preferably in the range of 505°C to 605°C.

[0098] Furthermore, when the step of transferring heat in (ii) comprises steps (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, more preferably in the range of 500°C to 600°C.

[0099] Furthermore, when the step of transferring heat in (ii) comprises steps (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′), the increase in pressure of the heated stream (11b) is preferably performed using a compressor (12b).

[0100] Furthermore, when the step of transferring heat 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′), the heat transfer from the compressed heated stream (7b) is carried out using a heat exchanger (2), more preferably comprising 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.

[0101] Furthermore, when the step of transferring heat in (ii) comprises (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 to 1,225°C, preferably in the range of above 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0102] Furthermore, when the step of transferring heat 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'), the expansions according to (ii.7') and (ii.11') are preferably carried out independently of each other using thermal expansion valves (9a and / or 9b) or expansion turbines (9a and / or 9b).

[0103] Furthermore, when the step of transferring heat in (ii) comprises (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′), the heated first process stream obtained in (ii) is preferably used as a feedstock or co-feedstock for an endothermic reaction, preferably a high temperature endothermic reaction.

[0104] Furthermore, when the step of transferring heat in (ii) comprises (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′), the heated first process stream obtained in (ii) is preferably used as a feed stream for the NH3 reforming process.

[0105] The unit bar (abs) is 1 bar = 10 5 Refers to absolute pressure equal to Pa. [Brief explanation of the drawings]

[0106] [Figure 1] FIG. 1 illustrates a process scheme in which mercury is used as the heat transfer medium. [Figure 2] FIG. 1 shows a method scheme for a thermodynamic cycle or heat pump process as a closed-loop process. [Figure 3] FIG. 1 shows a method scheme for a two-stage thermodynamic cycle or two-stage heat pump process, where each stage comprises a closed-loop process. DETAILED DESCRIPTION OF THE INVENTION

[0107] The present invention is further described by the following set of embodiments, as well as combinations of embodiments resulting from the indicated dependencies and backward references. It should be noted that whenever a range of embodiments is mentioned, particularly in connection with a term such as "the method according to any one of embodiments 1 to 4," it means that all embodiments within this range are expressly disclosed to those skilled in the art, that is, the wording of this term should be understood by those skilled in the art to be synonymous with "the method according to any one of embodiments 1, 2, 3, and 4." Furthermore, it is expressly noted that the following set of embodiments represents a properly structured part of the description of the general and preferred aspects of the present invention, rather than a set of claims determining the scope of protection.

[0108] 1. A method for transferring heat to a target process in a chemical manufacturing plant, the method comprising: (i) providing a first process stream (1) having a temperature T1; (ii) transferring heat from a chemical conversion process, from a physicochemical process, or from 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 T2>T1; (iii) performing a target process using the heated first process stream obtained in (ii); The method wherein the target process is different from a chemical conversion process, a physicochemical process, or a combination of a chemical conversion process and a physicochemical process in which heat is transferred by (ii).

[0109] 2. The method of embodiment 1, wherein heat is transferred in (ii) from a chemical conversion process and / or a physicochemical process, and the heat transferred by (ii) is obtained from an exothermic reaction, or the heat transferred by (ii) is excess heat of heat used to carry out an autothermal or endothermic reaction.

[0110] 3. The method of embodiment 2, wherein the exothermic reactions include one or more of 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 to acrolein or acrylic acid, preferably the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid.

[0111] 4. The method of embodiment 2, wherein the endothermic reaction comprises one or more of steam cracking, ethane dehydrogenation, propane dehydrogenation, butane dehydrogenation, steam reforming, dry reforming, styrene production, methanol reforming, dimethyl ether reforming, reverse water gas shift, alcohol dehydration, and NH3 reforming.

[0112] 5. The method of embodiment 2, wherein the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including partial oxidation of hydrocarbons (POx) processes, and the hydrocarbons are selected from the group consisting of (C1-C10) alkanes, more preferably (C1-C8) alkanes, more preferably (C1-C7) alkanes.

[0113] 6. The method of any one of embodiments 1 to 5, wherein the physicochemical process comprises, preferably consists of, one or more of vapor compression evaporation and chemisorption processes.

[0114] 7. The method of any one of embodiments 1 to 6, wherein the ambient heat transferred by (ii) is heat from the environment, preferably one or more of air, water, and solar radiation, including a combination of two or more.

[0115] 8. The method of any one of embodiments 1 to 7, wherein the heat transferred by (ii) does not include energy from nuclear fission, solar thermal energy, geothermal energy, hydroelectric energy, and wind energy.

[0116] 9. The method of any one of embodiments 1 to 8, wherein the step of transferring heat in (ii) comprises the use of a heat pump, and the heat pump is selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

[0117] 10. The method of embodiment 9, wherein the absorption heat pump is a conventional heat pump (type I heat pump), a heat transformer heat pump (type II heat pump), or an adsorption heat pump, and the absorption heat pump is preferably a conventional heat pump.

[0118] 11. The method of embodiment 10, wherein the adsorption heat pump comprises an adsorbent, the adsorbent comprising, preferably consisting of, one or more of activated carbon, zeolite, and mixtures thereof.

[0119] 12. The method of any one of embodiments 1 to 11, wherein the target process comprises, preferably consists of, heating of one or more compounds; preferably, the target process comprises, preferably consists of, a chemical conversion process and / or a thermal separation of compounds; more preferably, the target process comprises one or more of a chemical reaction, evaporation, a preheating step, and a crystallization process comprising a combination of two or more; more preferably, the target process comprises, preferably consists of, distillation, preferably column distillation, an endothermic reaction, an exothermic reaction, or an autothermal reaction; and the target process preferably comprises, preferably consists of, an endothermic reaction.

[0120] 13. The method of embodiment 12, wherein the thermal separation of compounds comprises, preferably consists of, isolation of isobutene from a mixture comprising n-butene, 2-butene and isobutene, preferably by distillation.

[0121] 14. The endothermic reaction comprises, and preferably consists of, one or more of cracking, preferably catalytic cracking, dehydrogenation, styrene production, reverse water gas shift, dehydration, thermal cracking, dimerization, oligomerization, gamma-butyrolactone synthesis, and reforming; More preferably, the cracking comprises the cracking of one or more of steam, hydrocarbons, aliphatics, alkenes, preferably ethylene, propylene and butylenes, dienes, preferably butadiene, acetylene, cycloaliphatics, naphtha, polymers, plastics, biomass, oily liquids, bitumen, tar urea, carbamates, preferably carbamates, to olefins, aromatics, fuels, isocyanates, melamine and diamines; more preferably, the dehydrogenation comprises the dehydrogenation of one or more of hydrocarbons, more preferably one or more of ethane, propane, butane, pentane, hexane, preferably hexane, to olefins, alkenes (ethylene, propylene, butylene), dienes (butadiene), as well as acetylenes, aliphatics, cycloaliphatics, naphtha, ethylbenzene, aromatics and styrene; more preferably the dehydration comprises the dehydration of one or more of alcohols, preferably one or more of ethanol, bioethanol, propanol and butanol, more preferably the dehydration of alcohols to alkenes, preferably one or more of ethylene, propylene and butylene, the pyrolysis comprises one or more of pyrolysis, thermal dissociation, gasification, more preferably the pyrolysis of one or more of polymers, plastics, biomass, waste, oil-containing liquids, bitumen, tar to olefins, alkenes, preferably one or more of ethylene, propylene and butylene, dienes, preferably butadiene, acetylene, monomers, aromatics, fuels and synthesis gas; the one or more of dimerization and oligomerization comprises dimerization or oligomerization to one or more of alkenes, preferably ethylene, butylene, and hexene, more preferably to a dialken or oligoalkene; the reforming preferably comprises one or more of steam methane reforming, dry reforming of methane, methanol steam reforming, dimethyl ether reforming, synthesis gas production, and NH3 reforming; 13. The method of embodiment 12, wherein the endothermic reaction more preferably comprises, more preferably consists of, NH3 reforming.

[0122] 15. The method of embodiment 12, wherein the endothermic reaction comprises, and preferably consists of, the dehydration of ethanol, and the chemical process to which heat is transferred in (ii) comprises the production of ethylene oxide, preferably ethylene oxide from ethylene.

[0123] 16. The method of embodiment 12, wherein the endothermic reaction comprises, and preferably consists of, steam methane reforming, which is preferably carried out at 700-1100°C, more preferably steam methane reforming to a synthesis gas containing CO and hydrogen.

[0124] 17. The method of embodiment 12, wherein the endothermic reaction comprises, and preferably consists of, steam cracking, which is preferably carried out at about 850 to about 900°C, more preferably steam cracking of naphtha to olefins, methane, and hydrogen.

[0125] 18. The method of embodiment 12, wherein the exothermic reaction comprises, preferably consists of, one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid, preferably the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid.

[0126] 19. The autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, including the partial oxidation of hydrocarbons (POx) process, and the hydrocarbons are selected from the group consisting of (C1-C 10 13. The method of embodiment 12, wherein the alkyl group is selected from the group consisting of (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0127] 20. The method of any one of embodiments 1 to 19, wherein T1 is in the range of 20 to 1,150°C, preferably in the range of 80 to 1,100°C, more preferably in the range of 200 to 1,000°C, more preferably in the range of 400 to 800°C, more preferably in the range of 500 to 600°C.

[0128] 21. The method of any one of embodiments 1 to 19, wherein T2 is in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0129] The method according to 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 (abs), preferably 5 to 250 bar (abs), more preferably 10 to 200 bar (abs), more preferably 20 to 150 bar (abs), and more preferably 50 to 100 bar (abs).

[0130] 23. The first process stream provided in (i) has a range of 200 to 20,000 h -1 preferably 400 to 15,000 h -1 more preferably 600 to 10,000 h -1 more preferably 1,000 to 5,000 h -1 and has a weight hourly space velocity in the range of the method according to any one of Embodiments 1 to 22.

[0131] 24.In step (ii) of transferring heat, (ii.a) providing heat from a chemical conversion process having a temperature T3, from a physicochemical process, or providing ambient heat, or providing a combination of two or more thereof; (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, and including T3 < T1, and T3 is preferably in the range of 255 °C to 700 °C, according to the method according to any one of Embodiments 1 to 23.

[0132] 25. The heat provided in (ii.a) is obtained from a process stream from a chemical conversion process and / or a process stream from a physicochemical process, and the process stream from a chemical conversion process and / or a process stream from a physicochemical process preferably includes one or more of steam from a steam generation process and flue gas, preferably flue gas, according to the method according to Embodiment 24.

[0133] 26. The method of embodiment 24 or 25, wherein the transfer of heat according to (ii.b) is carried out using a heat exchanger (2), which 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 the heat exchanger is preferably the reactor containing the first process stream provided in (i), more preferably the wall of the reactor containing the first process stream provided in (i).

[0134] 27. The method of any one of embodiments 24 to 26, wherein the target process comprises NH3 reforming and the heat transfer according to (ii.b) comprises at least partially converting NH3 to H2 and N2.

[0135] 28. The method of any one of embodiments 24 to 27, wherein the heated first process stream obtained in (ii.b) has a temperature T2, wherein T2 is preferably in the range of 350 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, preferably in the range of 450 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0136] 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 (abs), preferably in the range of 1 to 275 bar (abs), more preferably in the range of 5 to 250 bar (abs), more preferably in the range of 10 to 200 bar (abs), more preferably in the range of 20 to 150 bar (abs), more preferably in the range of 50 to 100 bar (abs).

[0137] 30. The step of transferring heat in (ii) (ii.1) providing heat (4) from a chemical conversion process having a temperature T3, wherein T3 is in the range of 255°C to 700°C, from a physicochemical process, or from ambient heat, or a combination of two or more thereof; (ii.2) providing a stream (10) comprising a heat transfer medium, the stream (10) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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) and a compressed stream (8) having a temperature T2; 30. The method of any one of embodiments 1 to 29, comprising:

[0138] 31. (ii.6) A step of 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); 31. The method of embodiment 30, further comprising:

[0139] 32. The method of embodiment 30 or 31, wherein the heat transfer medium is selected from the group consisting of mercury, cesium, rubidium, potassium, sodium, chlorofluorocarbons, hydrochlorofluorocarbons, preferably hydrochlorofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3 trifluoropropene, hydrofluorocarbons, preferably one or more of hydrofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3 trifluoropropene, one or more of 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.

[0140] 33. The method of any one of embodiments 30 to 32, wherein the stream provided in (ii.2) has a temperature of 300°C or higher, preferably in the range of 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0141] 34. The method according to any one of embodiments 30 to 33, wherein the stream provided in (ii.2) has a pressure in the range of 0.1 bar (abs) to 50 bar (abs), preferably in the range of 0.5 bar (abs) to 30 bar (abs), more preferably in the range of 1 bar (abs) to 20 bar (abs).

[0142] 35. The method of any one of embodiments 30 to 34, wherein 95 to 100% by volume, preferably 99 to 100% by volume, more preferably 99.9 to 100% by volume of the stream provided in (ii.2) consists of the heat transfer medium.

[0143] 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.

[0144] 37. The method of any one of embodiments 30 to 36, wherein the heat transfer medium in the flow provided in (ii.2) is a two-phase fluid having a gas phase and a liquid phase.

[0145] 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.

[0146] 39. The method of any one of embodiments 30 to 38, wherein the transfer of heat in (ii.3) is carried out using a heat exchanger (5), which 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 the reactor containing the first process stream provided in (i), more preferably the wall of the reactor containing the first process stream provided in (i).

[0147] 40. The method of any one of embodiments 30 to 39, wherein the heat provided in (ii.1) is obtained from a process stream from a chemical conversion process and / or a process stream from a physicochemical process, and the process stream from the chemical conversion process and / or the process stream from the physicochemical process preferably comprises one or more of steam, flue gas, preferably flue gas from a steam generation process.

[0148] 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.

[0149] 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.

[0150] 43. The method of any one of embodiments 30 to 42, wherein the heated stream obtained in (ii.3) is in a supercritical state.

[0151] 44. The method of any one of embodiments 30 to 43, wherein increasing the pressure of the flow according to (ii.4) is performed using a compressor (12).

[0152] 45. The method of any one of embodiments 30 to 44, wherein increasing the pressure of the stream according to (ii.4) is performed using a multi-stage compressor (12), the multi-stage compressor preferably comprising one or more working media, preferably one or two working media, the two working media being chemically and / or physically different from each other.

[0153] 46. ​​The method of embodiment 45, wherein the multi-stage compressor comprises one or more stages, each stage independently of the other comprising a temperature increase in the range of 20 to 500°C, preferably in the range of 50 to 200°C.

[0154] 47. The method of any one of embodiments 30 to 46, wherein increasing the pressure of the stream according to (ii.4) is performed adiabatically.

[0155] 48. The method of any one of embodiments 30 to 47, wherein the transfer of heat according to (ii.5) is carried out using a heat exchanger (2), which 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 the heat exchanger is preferably the reactor containing the first process stream provided in (i), more preferably the wall of the reactor containing the first process stream provided in (i).

[0156] 49. The method of any one of embodiments 30 to 48, wherein the target process comprises NH3 reforming, and wherein the heat transfer according to (ii.5) comprises converting NH3 at least partially into H2 and N2.

[0157] 50. The method of any one of embodiments 30 to 49, wherein (ii.5) results in a 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, more preferably in the range of 550°C to 1,000°C.

[0158] 51. The method according to any one of embodiments 30 to 50, wherein according to (ii.5), a compressed stream is obtained having a pressure in the range of 1 to 300 bar (abs), preferably 5 to 250 bar (abs), more preferably 10 to 200 bar (abs), more preferably 20 to 150 bar (abs), more preferably 50 to 100 bar (abs).

[0159] 52. The method of any one of embodiments 30 to 51, wherein the heated first process stream obtained in (ii.5) has a temperature in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0160] 53. The method according to any one of embodiments 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 (abs), preferably in the range of 1 to 275 bar (abs), more preferably in the range of 5 to 250 bar (abs), more preferably in the range of 10 to 200 bar (abs), more preferably in the range of 20 to 150 bar (abs), more preferably in the range of 50 to 100 bar (abs).

[0161] 54. The method according to any one of embodiments 31 to 53, wherein the process preferably comprises (ii.6) and (ii.7) as defined in embodiment 31, and wherein the expansion according to (ii.6) is carried out using a thermal expansion valve (9) or an expansion turbine (9).

[0162] 55. The method of embodiment 54, wherein increasing the pressure of the flow according to (ii.4) is performed using a compressor (12), and the expansion is performed using an expansion turbine, and energy obtained from the expansion turbine is preferably obtained as electricity and used to operate the compressor, or energy obtained from the expansion turbine is used to operate the compressor mechanically, preferably via a shaft for direct energy transmission.

[0163] 56. The method according to any one of embodiments 31 to 55, wherein the process preferably comprises (ii.6) and (ii.7) as defined in embodiment 31, and wherein the expanded stream obtained in (ii.6) has the same pressure and temperature as the stream containing the heat transfer medium provided in (ii.2).

[0164] 57. The method according to any one of embodiments 31 to 56, wherein the process comprises (ii.6), preferably (ii.7), as defined in embodiment 31, and wherein the expansion of the compressed stream according to (ii.6) is carried out adiabatically.

[0165] 58. The method according to any one of embodiments 31 to 57, wherein the process comprises (ii.6), preferably (ii.7), as defined in embodiment 31, and wherein 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) via (ii.7).

[0166] 59. The method according to any one of embodiments 31 to 58, wherein the process comprises (ii.6), preferably (ii.7), as defined in embodiment 31, and the stream obtained in (vii) is completely recycled to (ii.2) via (ii.7).

[0167] 60. The method of embodiment 59, wherein steps (ii.2) to (ii.7) are carried out in a closed system in which a stream containing the heat transfer medium is circulated.

[0168] 61. The method of any one of embodiments 1 to 60, wherein the method further comprises (iii) feeding the heated first process stream obtained in (ii.5) or (ii.b) to a first reactor to obtain a first product stream.

[0169] 62. The process of embodiment 61, wherein the heated first process stream obtained in (ii.5) or (ii.b) is fed to a first reactor having a temperature in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0170] 63. The heated first process stream obtained in (ii.5) or (ii.b) is heated for 10 h -1 ~50,000 hours -1 range, preferably 100 h -1 ~20,000 hours -1 range, more preferably 1,000 h -1 ~10,000 hours -1 63. The method of embodiment 61 or 62, wherein the first reactor has a gas hourly space velocity in the range of

[0171] 64. The method of any one of embodiments 61 to 63, wherein the method further comprises (iv) heating the first product stream obtained in (iii) to a temperature in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C, and feeding the heated first product stream to a second reactor to obtain a second product stream.

[0172] 65. The method of embodiment 64, wherein the process comprises (ii.1), (ii.2), (ii.3), (ii.4), (ii.5), (ii.6), and (ii.7), and wherein heating the first product stream according to (iv) comprises transferring heat from the compressed stream obtained in (ii.4) to the first product stream obtained in (iii) to obtain a heated first product stream and a compressed stream having a temperature in the range of 375°C to 1,400°C.

[0173] 66. The method of embodiment 64 or 65, wherein the first and second reactors are, independently of each other, adiabatic reactors, isothermal reactors, or a combination thereof.

[0174] 67. The method of any one of embodiments 64 to 66, wherein the first and second reactors are, independently of each other, tubular reactors.

[0175] 68.(ii) The step of transferring heat is (ii.1') providing heat (4) from a chemical conversion process, from a physicochemical process, or from ambient heat, or a combination of two or more thereof, having a temperature in the range of 255°C to 700°C; (ii.2') providing a stream (10a) comprising a first heat transfer medium, the stream (10a) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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, the stream (10b) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 275°C or greater; (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') A step of expanding the compressed stream (8a) obtained in (ii.6'); (ii.8') recycling at least a portion of the stream obtained in (ii.7') to (ii.2'); (ii.9') increasing the pressure of the heated stream (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) and a compressed stream (8b) having a temperature T2; (ii.11') Expanding the compressed stream (8b) obtained in (ii.10'); (ii.12') recycling at least a portion of the stream obtained in (ii.11') to (ii.5'); 68. The method of any one of embodiments 1 to 67, comprising:

[0176] 69. The method of embodiment 68, wherein the first heat transfer medium in (ii.2') and the second heat transfer medium in (ii.5') are, independently of one another, 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 and trans-1-chloro-3,3,3-trifluoropropene, hydrofluorocarbons, preferably one or more hydrofluoroolefins, more preferably (Z)-1-chloro-2,3,3,3-tetrafluoropropene and trans-1-chloro-3,3,3-trifluoropropene, one or more 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.

[0177] 70. The method of embodiment 68 or 69, wherein the stream (10a) provided in (ii.2') has a temperature of 300°C or higher, preferably in the range of 300°C to 1000°C, more preferably in the range of 350°C to 850°C.

[0178] 71. The method according to any one of embodiments 68 to 70, wherein the transfer of heat provided in (ii.1') is carried out using a heat exchanger (5), the heat exchanger preferably comprising 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.

[0179] 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.

[0180] 73. The method according to any one of embodiments 68 to 72, wherein increasing the pressure of the heated stream (11a) is carried out using a compressor (12a).

[0181] 74. The method of any one of embodiments 68 to 73, wherein the stream (10b) provided in (ii.5') has a temperature of 325°C or higher, preferably in the range of 325 to 1,000°C, more preferably in the range of 375 to 850°C, more preferably in the range of 450 to 650°C, more preferably in the range of 500 to 600°C.

[0182] 75. The method according to any one of embodiments 68 to 74, wherein the heat transfer from the compressed heated stream (7a) is carried out using a heat exchanger (13), the heat exchanger preferably comprising 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.

[0183] 76. The method according to any one of embodiments 68 to 75, wherein according to (ii.6'), a compressed stream (8a) is obtained having a temperature in the range of 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.

[0184] 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.

[0185] 78. The method according to any one of embodiments 68 to 77, wherein increasing the pressure of the heated stream (11b) is carried out using a compressor (12b).

[0186] 79. The method according to any one of embodiments 68 to 78, wherein the heat transfer from the compressed heated stream (7b) is carried out using a heat exchanger (2), which 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.

[0187] 80. The method of any one of embodiments 68 to 79, wherein the heated first process stream obtained in (ii.10') has a temperature in the range of 350 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 to 1,175°C, more preferably in the range of 550 to 1,075°C.

[0188] 81. The method according to any one of embodiments 68 to 80, wherein 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).

[0189] 82. The method of any one of embodiments 1 to 81, wherein the heated first process stream obtained in (ii) is used as a feedstock or co-feedstock for an endothermic reaction, preferably a high-temperature endothermic reaction.

[0190] 83. The method of 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.

[0191] The present invention is further illustrated by the following reference examples. [Example]

[0192] Reference Example 1: Heat transfer method involving Hg as the heat transfer medium The cycle of the heat transfer medium mercury is shown schematically in Figure 1. This process concept is particularly interesting when a low temperature exothermic heat source and a higher temperature endothermic heat sink are present in a manufacturing plant.

[0193] The COP is 4.27 and the volumetric heating capacity (VHC) is 8337 kJ / m 3 It was.

[0194] Heat is transferred to the Hg at a heat source, and heat is transferred from the Hg to the target process stream at a heat sink. [Explanation of symbols]

[0195] About Figure 2: (1) First process stream (2) Heat exchanger (3) the heated first process stream (4) Heat (5) Heat exchanger (6) Exhaust system (7) Compressed Heat Flow (8) Compressible flow (9) Thermal expansion valve or expansion turbine (10) Flow containing heat transfer medium (11)Heating flow (12) Compressor or multi-stage compressor About Figure 3: (1) First process stream (2) Heat exchanger (3) the heated first process stream (4) Heat (5) Heat exchanger (6) Exhaust system (7a) Compression heating flow (8a) Compressible flow (9a) Thermal expansion valve or expansion turbine (10a) Flow containing the first heat transfer medium (11a) Heating flow (12a) Compressor or multistage compressor (13)Heat exchanger (7b) Compressed Heat Flow (8b) Compressible flow (9b) Thermal expansion valve or expansion turbine (10b) Flow containing a second heat transfer medium (11b) Heating flow (12b) Compressor or multistage compressor

Claims

1. 1. A method for transferring heat to a target process in a chemical manufacturing plant, said 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, where T2>T1; (iii) carrying out the target process using the heated first process stream obtained in (ii); Including, The method, wherein the target process is different from the chemical conversion process, the physicochemical process, or the combination of the chemical conversion process and the physicochemical process from which heat is transferred by (ii).

2. Heat is transferred from the chemical conversion process and / or the physicochemical process in (ii), and 2. The method of claim 1, wherein the heat transferred by (ii) is obtained from an exothermic reaction or the heat transferred by (ii) is excess heat from heat used to carry out an autothermal or endothermic reaction.

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

4. 4. The method of claim 1, wherein the step of transferring heat in (ii) comprises the use of a heat pump, the heat pump being selected from the group consisting of a compression heat pump, an absorption heat pump, and a chemical adsorption heat pump.

5. 5. The method of claim 1, wherein the target process comprises heating one or more compounds.

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

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

8. (ii) transferring heat to (ii.a) providing heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, having a temperature T3; (ii.b) transferring the heat provided in (ii.a) to the first process stream (1) provided in (i) to obtain a heated first process stream (3) having a temperature T2; Including, 8. The method of claim 1, wherein T3<T1.

9. (ii) transferring heat to (ii.1) providing heat (4) from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, having a temperature in the range of 255°C to 700°C; (ii.2) providing a stream (10) comprising a heat transfer medium, said stream (10) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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); 9. The method of claim 1, comprising:

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

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

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

14. 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 comprises:

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

16. (ii) transferring heat to (ii.1') providing heat (4) from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, having a temperature in the range of 255°C to 700°C; (ii.2') providing a stream (10a) comprising a first heat transfer medium, said stream (10a) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 250°C or greater; (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, said stream (10b) having a pressure in the range of 0.001 to 100 bar (abs) and a temperature of 275°C or greater; (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 stream (8a) obtained in (ii.6'); (ii.8') recycling at least a portion of the stream obtained in (ii.7') to (ii.2'); (ii.9') increasing the pressure of the heated stream (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 stream (8b) obtained in (ii.10'); (ii.12') recycling at least a portion of the stream obtained in (ii.11') to (ii.5'); 16. The method of any one of claims 1 to 15, comprising:

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

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