Low-temperature NH3 reforming method combined with heat pump

Abstract

The present invention relates to a method for transferring heat to a stream comprising NH3, the method comprising the steps of: (i) providing a stream comprising a heat transfer medium; the stream having a pressure in the range of 1 to 100 bar (abs) and a temperature of 105°C or greater; (ii) increasing the temperature of the stream provided in (i) by transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to a heat transfer medium to obtain a stream having a temperature in the range of 125 to 750°C; (iii) increasing the pressure of the flow obtained in (ii); obtaining a compressed stream having a temperature in the range of 50 to 800°C; (iv) providing a stream comprising NH3, wherein the NH3-comprising stream has a temperature in the range of -33 to 100°C; (v) heating the stream provided in (iv), wherein the heating comprises transferring heat from the compressed stream obtained in (iii) to the stream provided in (iv) to obtain a heated NH3-containing stream having a temperature in the range of 25 to 750°C; (vi) expanding the compressed stream obtained in (v); (vii) optionally recycling at least a portion of the stream obtained in (vi) to (i). Includes.

Description

[Technical Field]

[0001] The present invention relates to a method for transferring heat to a stream comprising NH3. [Background technology]

[0002] Supplying thermal energy to endothermic processes, such as ammonia decomposition, is currently accomplished by burning fossil fuels or by direct electrical heating, which is often preferred because it is less efficient and therefore less costly than direct electrical heating.

[0003] Heat pumps intelligently utilize electrical energy in a thermodynamic cycle to achieve a temperature level rise of a much greater amount of heat than the amount of electrical energy used. For a temperature level rise via a Carnot cycle, the coefficient of performance (COP) is given by Equation I: ε カルノー-WP =1 / (1-T 低 / T 高 ) (I) is calculated according to In the formula, ε カルノー-WP is the coefficient of performance of the Carnot cycle of the heat pump, and T 低 is the absolute temperature (in Kelvin) at which heat is absorbed, and T 高 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 maximum temperatures of about 150 °C. Many technologically relevant processes require large amounts of heat at temperatures significantly above this value. Examples include the melting of metals, distillation processes and endothermic chemical reactions. For thermodynamic reasons, endothermic chemical reactions typically take place at high temperatures.

[0005] DE 2951188 A1 relates to a method for utilizing waste heat from an endothermic process, whereby heat is first supplied at high temperature from an external heat source, the residual heat from the reaction is obtained at low temperature, and the low temperature residual heat is reused for the endothermic reaction with the help of a heat pump.

[0006] DE 3209642 A1 discloses a process heat production plant which produces both 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 using different heat transfer media, which can be used especially in process engineering processes.

[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 in processes that require high levels of heat. [Prior art documents] [Patent documents]

[0009] [Patent Document 1] DE2951188A1 [Patent Document 2] DE3209642A1 [Non-patent literature]

[0010] [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]

[0011] It was therefore an object of the present invention to provide a method in which the utilization of heat, for example the utilization of a heat pump, is not limited to the further valorization of primary energy sources, and in particular sustainable energy sources or nuclear power. In particular, it is an object of the present invention to utilize the concept of heat transfer in reactions involving the conversion of ammonia, and in particular in ammonia reforming, said concept of heat transfer involving the valorization of heat not coming from a primary energy source, and in particular involving the valorization of waste heat or other available low-temperature heat.

[0012] Detailed Description Thus, it has been surprisingly found that low-temperature heat sources can be used to upgrade them into usable thermal energy, thereby achieving a coefficient of performance (COP) of greater than 1. In particular, it has been unexpectedly found that the use of a heat pump cascade is particularly advantageous for achieving energy efficiency and reducing dependence on primary energy sources, whether sustainable or not. Thus, by appropriate selection of the heat transfer medium, it is possible to upgrade the heat source and directly supply heat at very high temperatures, for example by superheated saturated steam, to provide the temperatures required for processes involving the conversion of ammonia, in particular ammonia reforming. In particular, the use of high-temperature heat pumps allows the electrification of said processes, which are difficult to achieve with electrical heating, and provides excellent electrical efficiency, in particular a COP of greater than 1. real It was found that

[0013] The present invention particularly relates to a method for transferring heat from a reaction in a chemical conversion process to a stream containing NH3, wherein excess heat from the chemical process and / or ambient heat is used to heat a heat transfer medium. The heat transfer medium is then compressed to further increase its temperature. The resulting compressed stream is then used to heat the NH3-containing stream. In this way, the excess heat from the chemical process and / or ambient heat is transferred via the heat transfer medium rather than being used directly to heat the NH3. [Means for solving the problem]

[0014] The present invention therefore relates to a method for transferring heat to a stream comprising NH3, the method comprising the following steps: (i) providing a stream comprising a heat transfer medium; the stream having a pressure in the range of 1 to 100 bar (abs) and a temperature of 105°C or greater; (ii) increasing the temperature of the stream provided in (i) by transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to a heat transfer medium to obtain a stream having a temperature in the range of 125 to 750°C; (iii) increasing the pressure of the flow obtained in (ii); obtaining a compressed stream having a temperature in the range of 50 to 800°C; (iv) providing a stream comprising NH3, wherein the NH3-comprising stream has a temperature in the range of -33 to 100°C; (v) heating the stream provided in (iv), wherein the heating comprises transferring heat from the compressed stream obtained in (iii) to the stream provided in (iv) to obtain a heated NH3-containing stream having a temperature in the range of 25 to 750°C; (vi) expanding the compressed stream obtained in (v); (vii) optionally recycling at least a portion of the stream obtained in (vi) to (i). Includes.

[0015] Preferably, the heat transfer medium is selected from the group consisting of evaporating and condensing working fluids and supercritical working fluids, preferably the heat transfer medium is water, more preferably the heat transfer medium is steam. DETAILED DESCRIPTION OF THE INVENTION

[0016] The stream provided in (i) preferably has a temperature of 150°C or higher, more preferably in the range of 200-550°C, more preferably in the range of 250-350°C.

[0017] The stream provided in (i) preferably has a pressure in the range of 5-50 bar (abs), more preferably in the range of 10-40 bar (abs), more preferably in the range of 20-30.

[0018] Preferably, the stream provided in (i) comprises 0-1% by volume, more preferably 0-0.1% by volume, more preferably 0-0.01% by volume of NH3.

[0019] Preferably, 95 to 100% by volume of the stream provided in (i) consists of the heat transfer medium, more preferably 99 to 100% by volume, more preferably 99.9 to 100% by volume.

[0020] The transfer of heat according to (ii) is preferably carried out using a heat exchanger.

[0021] Preferably, the ambient heat transferred by (ii) is heat from the environment, preferably from one or more of air, water, soil, solar radiation, and combinations of two or more thereof.

[0022] Preferably, the heat from the chemical conversion process transferred by (ii) is obtained from an exothermic reaction, or the heat from the chemical conversion process transferred by (ii) is excess heat to that used to carry out an autothermal or endothermic reaction.

[0023] When the heat from the chemical conversion process transferred by (ii) is obtained from an exothermic reaction, 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, preferably the selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid.

[0024] When the heat from the chemical conversion process transferred by (ii) is excess heat to that used to drive endothermic reactions, the endothermic reactions preferably include 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 dehydrogenation, and NH3 reforming.

[0025] When the heat from the chemical conversion process transferred by (ii) is excess heat to that used to carry out the autothermal reaction, it is preferred that the autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, and partial oxidation (POx) processes of hydrocarbons, and the hydrocarbons are selected from the group consisting of (C1 to C 10 )alkanes, more preferably (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0026] According to the invention, the stream obtained in (ii) preferably has a temperature in the range of 25 to 750°C, more preferably in the range of 100 to 550°C, more preferably in the range of 150 to 300°C, more preferably in the range of 180 to 200°C.

[0027] Preferably, the heat from a physicochemical process transferred by (ii) is obtained from an exothermic change in the aggregation state of a chemical compound or substance, more preferably from condensation and solidification of the chemical compound or substance. It is particularly preferred that the heat from a physicochemical process transferred by (ii) is obtained from vapor compression evaporation.

[0028] In (ii), it is preferred that the heat transfer medium at least partially evaporates.

[0029] Preferably, (iii) results in a compressed stream having a pressure in the range of 1 to 250 bar (abs), more preferably 5 to 150 bar (abs), more preferably 10 to 100 bar (abs), more preferably 20 to 90 bar (abs).

[0030] Increasing the pressure of the stream in (iii) is preferably achieved by means of a compressor.

[0031] Preferably, the method results in a coefficient of performance (COP) greater than 1, more preferably between 1.1 and 4, more preferably between 1.2 and 3, more preferably between 1.2 and 2, more preferably between 1.2 and 1.5.

[0032] The increase in the pressure of the stream according to (iii) is preferably carried out adiabatically.

[0033] In the sense of the present invention, an adiabatic or isothermal change of state is understood as a change of state which occurs in a manner close to a theoretical adiabatic or isothermal process.

[0034] Preferably, 95-100% by volume of the stream provided in (iv) consists of NH3, more preferably 99-100% by volume, more preferably 99.9-100% by volume.

[0035] The stream provided in (iv) preferably has a temperature in the range of -33 to 100°C, more preferably -15 to 80°C, more preferably 0 to 60°C, more preferably 15 to 50°C, more preferably 25 to 40°C.

[0036] The stream provided in (iv) preferably has a pressure in the range of 1 to 100 bar (abs), more preferably in the range of 20 to 35 bar (abs).

[0037] (iv) The flow provided is 200-20,000h-1 range, more preferably 2,000 to 8,000 hours -1 It is preferable that the mass hourly space velocity is in the range of

[0038] Preferably, heating according to (v) includes at least partially converting NH3 to N2 and H2, and heating according to (v) preferably includes converting 1 to 100% by volume, more preferably 15 to 50% by volume, of the NH3.

[0039] Preferably, (v) results in a compressed stream having a temperature in the range of 200 to 750°C, more preferably in the range of 300 to 550°C.

[0040] Preferably, (v) results in a compressed stream having a pressure in the range of 1 to 100 bar (abs), more preferably in the range of 20 to 35 bar (abs).

[0041] Preferably, the compressed stream obtained in (v) has the same pressure as the compressed stream obtained in (iii).

[0042] The heating according to (v) is preferably carried out using a heat exchanger, which is preferably the reactor containing the stream provided in (iv), more preferably the wall of the reactor containing the stream provided in (iv).

[0043] Preferably, (v) results in a stream comprising NH3 having a temperature in the range of 250-750°C, more preferably in the range of 290-310°C.

[0044] Preferably, (v) results in a stream comprising NH3 having a pressure in the range of 1 to 100 bar (abs), more preferably in the range of 10 to 40 bar (abs).

[0045] The expansion according to (vi) is preferably carried out using a thermal expansion valve.

[0046] The expanded stream obtained in (v) preferably has the same pressure and temperature as the stream containing the heat transfer medium provided in (i).

[0047] The expansion of the compressed stream according to (vi) is preferably carried out adiabatically.

[0048] Preferably, 1 to 100% by volume, more preferably 50 to 100% by volume of the stream obtained in (vi) is recycled to (i) via (vii).

[0049] The stream obtained in (vi) is preferably completely recycled to (i) by (vii).

[0050] If the stream obtained in (vi) is completely recycled to (i) by (vii), steps (i) to (vii) are preferably carried out in a closed system in which a stream containing the heat transfer medium circulates.

[0051] According to the present invention, the method comprises: (viii) feeding the heated NH3-containing stream obtained in (v) to a first reactor to obtain a first product stream, more preferably wherein the heat of the first product stream is used in (ii) as at least a portion of the heat from the chemical conversion process transferred to the heat transfer medium. It is preferred that the composition further comprises:

[0052] When the method further comprises the step of (viii) feeding the heated NH3-containing stream obtained in (v) to a first reactor to obtain a first product stream, it is preferred that the heated stream obtained in (v) is fed to the first reactor having a temperature in the range of 200 to 750°C, more preferably in the range of 250 to 550°C.

[0053] Furthermore, independently, the heated stream obtained in (v) is heated for 200 to 20,000 hours. -1 range, more preferably 400 to 4,000 h -1 It is preferable to supply the first reactor at a gas hourly space velocity in the range of

[0054] Furthermore, independently therefrom, it is preferred that the first product stream obtained in (viii) has a temperature in the range of 110 to 350°C, more preferably in the range of 160 to 250°C.

[0055] Furthermore, independently, it is preferred that, for every 100 mol % of NH3 contained in the heated stream fed to the first reactor, 1 to 75 mol %, more preferably 5 to 45 mol % of the NH3 contained in the heated stream fed to the first reactor is converted to N2 and H2.

[0056] Furthermore, independently, the method further comprises: (ix) providing the first product stream obtained in (viii) as a stream comprising NH3 in a subsequent process for transferring heat to a stream comprising NH3 according to any of the specific preferred embodiments of the present invention, and heating the first product stream in said subsequent process (v) to a temperature in the range of 200 to 750°C, more preferably to a temperature in the range of 20 to 450°C, and feeding the heated first product stream to a second reactor to obtain a second product stream. Preferably, the composition further comprises Preferably, the heat of the second product stream is used in (ii) as at least a portion of the heat from the chemical conversion process is transferred to the heat transfer medium.

[0057]

[0023] If the method further comprises providing the first product stream obtained in (ix)(viii) as a stream comprising NH3 in a process for subsequently transferring heat to a stream comprising NH3 according to any of the specific preferred embodiments of the present invention, the first product stream is reacted with (ix) for 350 to 20,000 h. -1 range, more preferably 400 to 4000 h -1 It is preferred that the second reactor has a gas hourly space velocity in the range of

[0058] Furthermore, independently therefrom, it is preferred that the second product stream obtained in (ix) has a temperature in the range of 110 to 350°C, more preferably in the range of 160 to 250°C.

[0059] Furthermore, independently, it is preferred that 1 to 50 mol %, more preferably 5 to 25 mol %, of the NH3 in the first product stream fed to the second reactor is converted to N2 and H2, relative to 100 mol % of NH3 in the heated stream fed to the first reactor.

[0060] Furthermore, independently, the method comprises the steps of: (x) providing the second product stream obtained in (ix) as a stream comprising NH3 in a subsequent process for transferring heat to a stream comprising NH3 according to any of the certain preferred embodiments of the present invention, and heating the first product stream in said subsequent process (v) to a temperature in the range of 250 to 550°C, more preferably in the range of 290 to 310°C, and feeding the heated second product stream to a third reactor to obtain a third product stream. Preferably, the composition further comprises Preferably, the heat of the third product stream is used in (ii) as at least a portion of the heat from the chemical conversion process that is transferred to the heat transfer medium.

[0061]

[0023] When the method further comprises providing the second product stream obtained in (ix) as a stream comprising NH3 in a process for subsequently transferring heat to a stream comprising NH3 according to any of the specific preferred embodiments of the present invention, the second product stream is reacted with (x) for 400 to 20,000 h. -1 range, more preferably 540 to 4000h -1 It is preferred that the mixture is fed to the third reactor having a gas hourly space velocity in the range of

[0062] Furthermore, independently therefrom, it is preferred that the third product stream obtained in (x) has a temperature in the range of 120 to 300°C, more preferably in the range of 170 to 235°C.

[0063] Furthermore, independently, it is preferred that 1 to 50 mol %, more preferably 5 to 25 mol %, of the NH3 in the second product stream fed to the third reactor is converted to N2 and H2, relative to 100 mol % of NH3 in the heated stream fed to the first reactor.

[0064] According to the present invention, the first, second and third reactors are preferably, independently of each other, adiabatic reactors, isothermal reactors, or a combination thereof. In the sense of the present invention, an adiabatic or isothermal reactor is understood to be a reactor which operates in close proximity to a theoretical adiabatic or isothermal process.

[0065] Furthermore, the first, second and third reactors are preferably, independently of one another, tubular reactors.

[0066] Furthermore, the first, second and third reactors preferably have diameters independently of one another in the range of 0.5 to 5 m, more preferably in the range of 1.5 to 2.5 m, more preferably in the range of 1.9 to 2.1 m.

[0067] Furthermore, the first, second and third reactors preferably have lengths independently of one another in the range of 1.0 to 20.0 m, more preferably in the range of 2.0 to 13.0 m, and more preferably in the range of 3.0 to 12.0 m.

[0068] According to the present invention, the heated stream obtained in (v) is preferably used as a fuel or co-fuel for combustion with oxygen to provide heat for an endothermic reaction.

[0069] Furthermore, it is preferred to use the heated stream obtained in (v) as a feed stream for the NH3 reforming process.

[0070] The present invention also relates to a method for transferring heat to a stream comprising NH3, said method comprising the steps of: (1) transferring heat to a stream comprising NH3 according to any one of the specific preferred embodiments of the present invention, wherein the initial stream has a temperature T0 and the resulting heated stream has a temperature T1, where T1 > T0; (2) transferring heat to the NH3-containing stream obtained in (1) according to any one of the specific preferred embodiments of the present invention, wherein the resulting heated stream has a temperature T2, where T2>T1; Includes.

[0071] According to the invention, the method comprises one or more of the following successive steps: (N) transferring heat to the NH3-containing stream obtained in (N-1) according to any one of the specific preferred embodiments of the present invention, wherein the resulting heated stream reaches a temperature T N T N >T N-1 and In the formula, N is 3, or 3 and 4, or 3 to 5, or 3 to 6, or 3 to 7, or 3 to 8, or 3 to 9, or 3 to 10, or 3 to 11, or 3 to 12, or 3 to 13, or 3 to 14, or 3 to 15, or 3 to 16, or 3 to 17, or 3 to 18, or 3 to 19, or 3 to 20. It is preferred that the composition further comprises:

[0072] In the context of the present invention, a process further comprising one or more subsequent sequential steps (N) comprises x additional steps, where x=N-2. For example, a process where N is 3 further comprises one subsequent sequential step (3), i.e., after step (2). As a further example, a process where N is 3 to 5 comprises, after step (2), three subsequent sequential steps (3), (4), and (5).

[0073] The unit bar (abs) means absolute pressure, and 1 bar is 10 5 Equivalent to Pa.

[0074] The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the indicated dependencies and backward references. In particular, it should be noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "the method of any one of embodiments 1 to 4," all embodiments within this range are meant to be expressly disclosed for those skilled in the art, i.e., this expression means that those skilled in the art will understand that it is synonymous with "the method of any one of embodiments 1, 2, 3, and 4." Furthermore, it is expressly noted that the following set of embodiments represents a suitably structured part of the description directed to the general and preferred aspects of the present invention, rather than a set of claims determining the scope of protection.

[0075] 1. A method for transferring heat to a stream comprising NH3, comprising the steps of: (i) providing a stream comprising a heat transfer medium; the stream having a pressure in the range of 1 to 100 bar (abs) and a temperature of 105°C or greater; (ii) increasing the temperature of the stream provided in (i) by transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to a heat transfer medium to obtain a stream having a temperature in the range of 125 to 750°C; (iii) increasing the pressure of the flow obtained in (ii); obtaining a compressed stream having a temperature in the range of 50 to 800°C; (iv) providing a stream comprising NH3, wherein the NH3-comprising stream has a temperature in the range of -33 to 100°C; (v) heating the stream provided in (iv), wherein the heating comprises transferring heat from the compressed stream obtained in (iii) to the stream provided in (iv) to obtain a heated NH3-containing stream having a temperature in the range of 25 to 750°C; (vi) expanding the compressed stream obtained in (v); (vii) optionally recycling at least a portion of the stream obtained in (vi) to (i). A method comprising:

[0076] 2. The method of embodiment 1, wherein the heat transfer medium is selected from the group consisting of evaporating and condensing working fluids, and supercritical working fluids; preferably, the heat transfer medium is water; more preferably, the heat transfer medium is steam.

[0077] 3. The process of embodiment 1 or 2, wherein the stream provided in (i) has a temperature of 150°C or higher, preferably in the range of 200 to 550°C, more preferably in the range of 250 to 350°C.

[0078] 4. The process of any one of embodiments 1 to 3, wherein the stream provided in (i) has a pressure in the range of 5 to 50 bar (abs), preferably in the range of 10 to 40 bar (abs), more preferably in the range of 20 to 30.

[0079] 5. The process of any one of embodiments 1 to 4, wherein the stream provided in (i) comprises 0-1 vol. %, preferably 0-0.1 vol. %, more preferably 0-0.01 vol. % NH3.

[0080] 6. The process of any one of embodiments 1 to 5, wherein 95-100% by volume, preferably 99-100% by volume, more preferably 99.9-100% by volume of the stream provided in (i) consists of the heat transfer medium.

[0081] 7. The method of any one of embodiments 1 to 6, wherein the transfer of heat according to (ii) is carried out using a heat exchanger.

[0082] 8. The method of any one of embodiments 1 to 7, wherein the ambient heat transferred by (ii) is heat from the environment, preferably heat from one or more of air, water, soil, solar radiation, and combinations of two or more thereof.

[0083] 9. The method of any one of embodiments 1 to 8, wherein the heat from the chemical conversion process transferred by (ii) is obtained from an exothermic reaction, or the heat from the chemical conversion process transferred by (ii) is excess heat from that used to carry out an autothermal or endothermic reaction.

[0084] 10. The method of embodiment 9, wherein the exothermic reaction comprises one or more of methanol production, dimethyl ether production, NH3 production, ethylene epoxidation, sulfuric acid production, and selective oxidation of one or more of alkanes, alkenes, and alkynes, preferably selective oxidation of one or more of alkanes, alkenes, and alkynes to acrolein or acrylic acid.

[0085] 11. The method of embodiment 9, 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 dehydrogenation, and NH3 reforming.

[0086] 12. The autothermal reaction is selected from the group consisting of autothermal reforming of natural gas and hydrocarbons, and partial oxidation of hydrocarbons (POx) process, and the hydrocarbons are selected from the group consisting of (C1 to C 10 10. The method of embodiment 9, wherein the alkyl group is selected from the group consisting of (C1-C8)alkanes, more preferably (C1-C7)alkanes.

[0087] 13. The process of any one of embodiments 1 to 12, wherein the stream obtained in (ii) has a temperature in the range of 25 to 750°C, preferably in the range of 100 to 550°C, more preferably in the range of 150 to 300°C, more preferably in the range of 180 to 200°C.

[0088] 14. The method of any one of embodiments 1 to 13, wherein the heat from the physicochemical process transferred by (ii) is obtained from an exothermic change in the aggregation state of the chemical compound or substance, preferably condensation and solidification of the chemical compound or substance.

[0089] 15. The method of embodiment 14, wherein the heat from the physicochemical process transferred by (ii) is obtained from vapor compression evaporation.

[0090] 16. The method of any one of embodiments 1 to 15, wherein in (ii) the heat transfer medium is at least partially evaporated.

[0091] 17. The process of any one of embodiments 1 to 16, wherein (iii) results in a compressed stream having a pressure in the range of 1 to 250 bar (abs), preferably 5 to 150 bar (abs), more preferably 10 to 100 bar (abs), more preferably 20 to 90 bar (abs).

[0092] 18. The method of any one of embodiments 1 to 17, wherein increasing the pressure of the stream according to (iii) is performed using a compressor.

[0093] 19. The method of any one of embodiments 1 to 18, resulting in a coefficient of performance (COP) greater than 1, preferably 1.1 to 4, more preferably 1.2 to 3, more preferably 1.2 to 2, more preferably 1.2 to 1.5.

[0094] 20. The method of any one of embodiments 1 to 19, wherein increasing the pressure of the stream according to (iii) is performed adiabatically.

[0095] 21. The process of any one of embodiments 1 to 20, wherein 95-100% by volume, preferably 99-100% by volume, more preferably 99.9-100% by volume of the stream provided in (iv) consists of NH3.

[0096] 22. The process of any one of embodiments 1 to 21, wherein the stream provided in (iv) has a temperature in the range of -33 to 100°C, preferably -15 to 80°C, more preferably 0 to 60°C, more preferably 15 to 50°C, more preferably 25 to 40°C.

[0097] 23. The method of any one of embodiments 1 to 22, wherein the stream provided in (iv) has a pressure in the range of 1 to 100 bar (abs), preferably in the range of 20 to 35 bar (abs).

[0098] 24. The flow provided in (iv) is 200-20,000h -1 range, preferably 2,000 to 8,000 h -1 24. The method of any one of the preceding embodiments, wherein the mass hourly space velocity is in the range of

[0099] 25. The method of any one of embodiments 1 to 24, wherein heating according to (v) comprises at least partially converting NH3 to N2 and H2, and wherein heating according to (v) preferably comprises converting 1 to 100% by volume, preferably 15 to 50% by volume, of the NH3.

[0100] 26. The process of any one of embodiments 1 to 25, wherein (v) results in a compressed stream having a temperature in the range of 200 to 750°C, preferably in the range of 300 to 550°C.

[0101] 27. The method of any one of embodiments 1 to 26, wherein (v) results in a compressed stream having a pressure in the range of 1 to 100 bar (abs), preferably in the range of 20 to 35 bar (abs).

[0102] 28. The method of any one of embodiments 1 to 27, wherein the compressed stream obtained in (v) has the same pressure as the compressed stream obtained in (iii).

[0103] 29. The process of any one of embodiments 1 to 28, wherein the heating according to (v) is carried out using a heat exchanger, and the heat exchanger is preferably the reactor containing the stream provided in (iv), more preferably the wall of the reactor containing the stream provided in (iv).

[0104] 30. The process of any one of embodiments 1 to 29, wherein (v) results in a stream comprising NH3 having a temperature in the range of 250 to 750 °C, preferably in the range of 290 to 310 °C.

[0105] 31. The process of any one of embodiments 1 to 30, wherein (v) results in a stream comprising NH3 having a pressure in the range of 1 to 100 bar (abs), preferably in the range of 10 to 40 bar (abs).

[0106] 32. The method of any one of embodiments 1 to 31, wherein the expansion according to (vi) is performed using a thermal expansion valve.

[0107] 33. The method of any one of embodiments 1 to 32, wherein the expanded stream obtained in (v) has the same pressure and temperature as the stream containing the heat transfer medium provided in (i).

[0108] 34. The method of any one of embodiments 1 to 33, wherein the expansion of the compressed stream according to (vi) is performed adiabatically.

[0109] 35. The process of any one of embodiments 1 to 34, wherein 1 to 100% by volume, preferably 50 to 100% by volume, of the stream obtained in (vi) is recycled to (i) via (vii).

[0110] 36. The method of any one of embodiments 1 to 35, wherein the stream obtained in (vi) is completely recycled to (i) by (vii).

[0111] 37. The method of embodiment 36, wherein steps (i)-(vii) are carried out in a closed system in which a stream containing the heat transfer medium circulates.

[0112] 38. The following steps (viii) feeding the heated NH3-containing stream obtained in (v) to a first reactor to obtain a first product stream, preferably wherein the heat of the first product stream is used in (ii) as at least a portion of the heat from the chemical conversion process transferred to the heat transfer medium. 38. The method of any one of embodiments 1 to 37, further comprising:

[0113] 39. The process of embodiment 38, wherein the heated stream obtained in (v) is fed to a first reactor having a temperature in the range of 200 to 750°C, preferably in the range of 250 to 550°C.

[0114] 40. The heated stream obtained in (v) is heated for 200 to 20,000 hours. -1 range, preferably 400 to 4,000 h -1 40. The process of embodiment 38 or 39, wherein the first reactor is fed at a gas hourly space velocity in the range of

[0115] 41. The process of any one of embodiments 38 to 40, wherein the first product stream obtained in (viii) has a temperature in the range of 110 to 350°C, preferably in the range of 160 to 250°C.

[0116] 42. The process of any one of embodiments 38 to 41, wherein, relative to 100 mol % of NH3 contained in the heated stream fed to the first reactor, 1 to 75 mol %, preferably 5 to 45 mol % of NH3 contained in the heated stream fed to the first reactor is converted to N2 and H2.

[0117] 43. The following steps: (ix) providing the first product stream obtained in (viii) as a stream comprising NH3 in a subsequent process for transferring heat to a stream comprising NH3 according to any of embodiments 1 to 42, 57, and 58, and heating the first product stream in (v) of the subsequent process to a temperature in the range of 200 to 750°C, preferably in the range of 20 to 450°C, and feeding the heated first product stream to a second reactor to obtain a second product stream. further comprising 43. The method of any one of embodiments 38 to 42, wherein preferably the heat of the second product stream is used in (ii) as at least a portion of the heat from the chemical conversion process that is transferred to the heat transfer medium.

[0118] 44. The first product stream is produced by (ix) for 350-20,000 h -1 range, preferably 400 to 4000h-1 44. The method of embodiment 43, wherein the second reactor has a gas hourly space velocity in the range of

[0119] 45. The process of embodiment 43 or 44, wherein the second product stream obtained in (ix) has a temperature in the range of 110 to 350°C, preferably in the range of 160 to 250°C.

[0120] 46. ​​The process of any one of embodiments 43 to 45, wherein 1 to 50 mol %, preferably 5 to 25 mol %, of the NH3 in the first product stream fed to the second reactor is converted to N2 and H2, relative to 100 mol % of NH3 in the heated stream fed to the first reactor.

[0121] 47. The following steps: (x) providing the second product stream obtained in (ix) as a stream comprising NH3 in a subsequent process for transferring heat to a stream comprising NH3 according to any of embodiments 1 to 42, 57, and 58, and heating the first product stream in (v) of the subsequent process to a temperature in the range of 250 to 550°C, preferably in the range of 290 to 310°C, and feeding the heated second product stream to a third reactor to obtain a third product stream. further comprising 47. The method of any one of embodiments 43 to 46, wherein preferably the heat of the third product stream is used in (ii) as at least a portion of the heat from the chemical conversion process that is transferred to the heat transfer medium.

[0122] 48. The second product stream is reacted with (x) for 400 to 20,000 h. -1 range, preferably 540 to 4000h -1 48. The method of embodiment 47, wherein the second reactor is fed to the third reactor having a gas hourly space velocity in the range of

[0123] 49. The process of embodiment 47 or 48, wherein the third product stream obtained in (x) has a temperature in the range of 120 to 300°C, preferably in the range of 170 to 235°C.

[0124] 50. The process of any one of embodiments 47 to 49, wherein 1 to 50 mol %, preferably 5 to 25 mol %, of the NH3 in the second product stream fed to the third reactor is converted to N2 and H2, relative to 100 mol % of NH3 in the heated stream fed to the first reactor.

[0125] 51. The process of any one of embodiments 38 to 50, wherein the first, second, and third reactors are, independently of each other, adiabatic reactors, isothermal reactors, or a combination thereof.

[0126] 52. The process of any one of embodiments 38 to 51, wherein the first, second, and third reactors are, independently of each other, tubular reactors.

[0127] 53. The process of any one of embodiments 38 to 52, wherein the first, second, and third reactors, independently of one another, have diameters in the range of 0.5 to 5 m, preferably in the range of 1.5 to 2.5 m, and more preferably in the range of 1.9 to 2.1 m.

[0128] 54. The process of any one of embodiments 38 to 53, wherein the first, second, and third reactors, independently of one another, have lengths in the range of 1.0 to 20.0 m, preferably in the range of 2.0 to 13.0 m, and more preferably in the range of 3.0 to 12.0 m.

[0129] 55. The method of any one of embodiments 1 to 54, wherein the heated stream obtained in (v) is used as a fuel or co-fuel for combustion with oxygen to provide heat for an endothermic reaction.

[0130] 56. The method of any one of the preceding embodiments, wherein the heated stream obtained in (v) is used as a feed stream for an NH3 reforming process.

[0131] 57. A method for transferring heat to a stream containing NH3, comprising the steps of: (1) transferring heat to a stream comprising NH3 according to any one of embodiments 1 to 42, wherein the initial stream has a temperature T0 and the resulting heated stream has a temperature T1, where T1>T0; (2) transferring heat to the NH3-containing stream obtained in (1) according to any one of embodiments 1 to 42, wherein the resulting heated stream has a temperature T2, where T2>T1. A method comprising:

[0132] 58. One or more of the following subsequent consecutive steps: (N) transferring heat to the NH3-containing stream obtained in (N-1) according to any one of embodiments 1 to 42, wherein the resulting heated stream reaches a temperature T N T N >T N-1 and In the formula, N is 3, or 3 and 4, or 3 to 5, or 3 to 6, or 3 to 7, or 3 to 8, or 3 to 9, or 3 to 10, or 3 to 11, or 3 to 12, or 3 to 13, or 3 to 14, or 3 to 15, or 3 to 16, or 3 to 17, or 3 to 18, or 3 to 19, or 3 to 20. 58. The method of embodiment 57, further comprising:

[0133] The present invention will be further illustrated by the following Reference Examples, Examples and Comparative Examples. [Example]

[0134] The following examples were simulated using conventional software.

[0135] Example 1: Vaporization and preheating of NH3 with a combined heat pump The hot outlet of the heat pump was used to vaporize and preheat the NH3-containing stream for further processing. Table 1 below shows the associated power consumption values. Processing of the NH3-containing stream without a subsequent NH3 reforming step yielded coefficient of performance (COP) values ​​well above 1, of 4.0 or 1.3, depending on whether the heat pump was used only for the evaporation step or also for preheating.

[0136] [Table 1]

[0137] Example 2: NH3 reforming reaction in an adiabatic reactor coupled with a heat pump The preheated NH3-containing gas stream produced by Example 1 was used for the NH3 reforming process in an adiabatic reactor. In this case, the inlet temperature was fixed at 300°C. The NH3-containing gas stream was set at 10 t / h as a reference scenario, and the adiabatic reactor had a fixed geometry with a diameter of 2 m and a length of 10 m. Table 2 shows the inlet and outlet temperatures, NH3 conversion, and GHSV. Figure 1 shows the conversion, temperature, and equilibrium values.

[0138] [Table 2]

[0139] Example 3: NH3 reforming reaction in a cascade of adiabatic reactors coupled with a heat pump The preheated NH3-containing gas stream produced in Example 1 was used in an NH3 reforming process using a cascade of adiabatic reactors. In this case, the inlet temperature for each reactor was fixed at 300°C. The NH3-containing gas stream was set at 10 t / h in the first adiabatic reactor as a reference scenario. The outlet stream of the first adiabatic reactor was heated again to 300°C and fed to the second adiabatic reactor. The outlet stream of the second adiabatic reactor was heated again to 300°C and fed to the third adiabatic reactor. Each adiabatic reactor had a fixed geometry with a diameter of 2 m and a length of 10 m. Table 3 shows the inlet and outlet temperatures, NH3 conversion, and GHSV. Figure 2 shows the conversion, temperature, and equilibrium values.

[0140] [Table 3]

[0141] Example 4: NH3 reforming reaction in a quasi-isothermal reactor coupled with a heat pump The preheated NH3-containing gas stream produced by Example 1 was used for the NH3 reforming process within the quasi-isothermal reactor concept. Thus, the NH3-containing gas stream with a vapor temperature of 300°C was used as the heat source for the endothermic NH3 reforming process. Table 4 shows the corresponding NH3 conversion and inlet / outlet temperatures. The reactor was of fixed geometry with a diameter of 2 m and a length of 10 m. The heat flux of the quasi-isothermal process concept was 170 W / m 2 Adjusted to / K.

[0142] [Table 4]

[0143] Example 5: NH3 reforming reaction using two adiabatic reactors and one quasi-isothermal reactor in series coupled with a heat pump a) Reactor settings and NH3 conversion The preheated NH3-containing gas stream produced by Example 1 was used in an NH3 reforming process using a cascade of two adiabatic reactors followed by one quasi-isothermal reactor. In this case, the inlet temperature for each reactor was fixed at 300°C. The NH3-containing gas stream was set at 10 t / h in the first adiabatic reactor as a reference scenario. The outlet of the first adiabatic reactor was again heated to 300°C and fed to the second adiabatic reactor. All reactors had a fixed geometry with a diameter of 2 m and a length of 10 m. The heat flux of the quasi-isothermal reactor was 170 W / m 2 / K. Table 5 shows the inlet and outlet temperatures, NH3 conversion and GHSV. Figure 4 shows the conversion, temperature and equilibrium values.

[0144] [Table 5]

[0145] b) COP value of a heat pump system with a reactor inlet at 300°C The impact of heat pump integration according to Example 5 was calculated. Table 6 shows the energy values ​​that ultimately resulted in a COP value of 1.2, which means that applying the heat pump concept makes the NH3 reforming process 20% more efficient than using electricity directly to heat the reactor.

[0146] [Table 6]

[0147] References: - DE2951188A1 - DE3209642A1 - 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. (i) providing a stream comprising a heat transfer medium; said stream having a pressure in the range of 1 to 100 bar (abs) and a temperature of 105°C or greater; (ii) increasing the temperature of the stream provided in (i) by transferring heat from a chemical conversion process, a physicochemical process, or ambient heat, or a combination of two or more thereof, to the heat transfer medium to obtain a stream having a temperature in the range of 125 to 750°C; (iii) increasing the pressure of the stream obtained in (ii); obtaining a compressed stream having a temperature in the range of 50 to 800°C; (iv) NH ３ providing a stream comprising the NH ３ wherein the stream has a temperature in the range of -33 to 100°C; (v) heating the stream provided in (iv), wherein the heating transfers heat from the compressed stream obtained in (iii) to the stream provided in (iv) to produce heated NH3 having a temperature in the range of 25 to 750°C. ３ obtaining a stream comprising: (vi) expanding the compressed stream obtained in (v); (vii) optionally recycling at least a portion of the stream obtained in (vi) to (i). NH ３ A method of transferring heat to a flow containing

2. The method of claim 1 , wherein the heat transfer medium is selected from the group consisting of evaporating and condensing working fluids and supercritical working fluids.

3. 3. The method according to claim 1 or 2, wherein the transfer of heat according to (ii) is carried out using a heat exchanger.

4. 3. The method of claim 1 or 2, wherein the ambient heat transferred by (ii) is heat from the environment.

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

6. 3. The method of claim 1 or 2, wherein the heat from a physicochemical process transferred by (ii) is obtained from an exothermic change in the aggregation state of a chemical compound or substance.

7. 7. The method of claim 6, wherein the heat from the physicochemical process transferred by (ii) is obtained from vapor compression evaporation.

8. 3. The method of claim 1 or 2, wherein increasing the pressure of the stream according to (iii) is accomplished using a compressor.

9. 3. The method of claim 1 or 2, which results in a coefficient of performance (COP) greater than 1.

10. 3. The method of claim 1 or 2, wherein increasing the pressure of the stream by (iii) is performed adiabatically.

11. 3. The method of claim 1 or 2, wherein the expansion of the compressed stream by (vi) is performed adiabatically.

12. (viii) The heated NH obtained in step (v) ３ to a first reactor to obtain a first product stream. The method of claim 1 or 2, further comprising:

13. (ix) treating the first product stream obtained in step (viii) with the NH ３ and subsequently the NH ３ wherein said first product stream is heated in said subsequent process (v) to a temperature in the range of 200 to 750°C and said heated first product stream is fed to a second reactor to obtain a second product stream; The method of claim 12 further comprising:

14. (x) treating the second product stream obtained in step (ix) with the NH ３ and subsequently the NH ３ wherein said first product stream is heated to a range of 250 to 550°C in said subsequent process (v) and said heated second product stream is fed to a third reactor to obtain a third product stream; 14. The method of claim 13, further comprising:

15. (1) NH ３ 3. A process for transferring heat according to claim 1 or 2 to a stream containing ０ and the resulting heated stream has a temperature T １ and T １ >T ０ The process is (2) The NH obtained in (1) ３ 3. A process for transferring heat according to claim 1 or 2 to a stream comprising ２ and T ２ >T １ This is the process NH ３ A method of transferring heat to a flow containing

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