Recycling of heat from a chemical process to a heat pump system

Abstract

The present invention relates to a method for recycling of heat from a chemical process to a heat pump system. Furthermore, the present invention relates to an apparatus facilitating heat integration of a chemical process and a heat pump system, and the use of thereof for heat integration.

Description

Recycling of heat from a chemical process to a heat pump systemTECHNICAL FIELDThe present invention relates to a method for recycling of heat from a chemical process to a heat pump system. Furthermore, the present invention relates to an apparatus facilitating heat integration of a chemical process and a heat pump system, and the use of thereof for heat integration.INTRODUCTIONProcess heat accounts for approximately 30% of all the fuel use in the manufacturing sector, and thereby contributes to a large amount of carbon dioxide emissions through the combustion of said, often carbonaceous, fuel required to generate the process heat. In an ongoing effort, many strategies and approaches arose for reducing carbon dioxide emissions and moving towards a low-carbon economy. In the manufacturing sector, the transition to renewable energy, the replacement of the carbonaceous fuel by e.g. biomass or “Power to X” derived fuel, efficient use of energy and heat or effective emission control such as e.g. carbon capture are suitable options to improve the carbon footprint of a manufacturing plant. In this regard, an important aspect of the efforts to lower carbon dioxide emissions of a manufacturing process constitutes the efficient use of any accruing waste heat throughout said process by recycling of waste heat and thus avoiding the loss of said heat by simply feeding it into the atmosphere. However, such an endeavor poses a considerable challenge, especially for existing chemical plants, as the integrity of the entire plant must be ensured.Linde & BASF, 2019, “Carbon capture, storage and utilisation”, page 05 discloses a process of a carbon capture plant, wherein the process steps comprising a pre-treating of a flue gas, which comprises carbon dioxide, an absorption of said carbon dioxide from the flue gas, as well as a regeneration of an absorber solution used to strip the carbon dioxide are described in detail.EP 2 587 005A1 discloses a thermoelectric energy storage system for the conversion of electrical energy into thermal energy. The system comprises a hot storage heat exchanger, a cold storage heat exchanger, a regenerative heat exchanger adapted to further cool the working fluid at the output of the hot storage heat exchanger and to pre-heat the working flued at the input into the hot storage heat exchanger, as well as a compressor and an expander.US 2007 / 017242 A1 discloses a system for heat refinement through utilization of waste heat comprising an evaporator to gasify the working fluid, a compressor, a condenser to release heat to a heat carrier and to condense the working fluid, and an expansion valve.DE 102 20870A1 discloses a heat pump system comprising an evaporator to generate a gaseous heat carrier, which is subsequently split by a valve and fed to a compressor and partially to an expansion machine. On the one hand, the heat carrier in the compressor is brought to a higher pressure and temperature, and then fed to a condensator to release thermal energy to a heat recipient, which leads to a condensation of the heat carrier. The condensed heat carrier is pumped back into the evaporator. On the other hand, the temperature of the heat carrier in the expansion machine is reduced, liquefied in a condenser, and then fed back to the evaporator.US 4 033 141 A discloses a method for running a heat pump plant comprising the heat transfer in two circuits, wherein heat from a first medium is transferred to a refrigerant, which is vaporized in a first circuit to drive an expansion motor, subsequently condensed by heat exchange with a coolant and recirculated for a heat exchange with the first medium. Further, heat is transferred from a second medium to a refrigerant in a second circuit, the refrigerant is vaporized using a compressor to drive an expansion motor, and then used to heat a third medium in a condenser by heat exchange, wherein the condensed refrigerant is then recirculated for a heat exchange with the second medium. The first and the second medium can be the same fluid, possibly with different temperatures.AT 522615A1 discloses a process for the generation of steam, comprising a heat source to transfer heat to a refrigerant, at least one compressor to pressurize the refrigerant, a heat exchanger in which the refrigerant transfers heat to a second medium being water, and an expansion unit, in particular an expansion valve, to expand the refrigerant before feeding it back to the heat source.US 2019 / 323704A1 discloses a heat pump system for producing steam in which a recuperator is used for a heat exchange between a refrigerant obtained from a condenser and a refrigerant prior to being fed into a compressor to generate a supercooled refrigerant that is being introduced into an evaporator, to increase the condensed heat and to elevate the temperatures at the inlet and the outlet of the compressor, whereby the efficiency of the steam production can be improved.As a further part of the decarbonisation of a manufacturing process, various options may be considered to directly reduce the carbon dioxide emissions associated with said process, one of which may be the installation of a post combustion carbon capture unit to strip carbon dioxide from the flue gas resulting from the combustion of a carbonaceous fuel. However, this type of emission control requires a large amount of thermal energy that is often linked with additional carbon dioxide emissions, mitigating the effect of the carbon capture on the manufacturing process.DETAILED DESCRIPTIONThus, it was an object of the present invention to utilize waste heat to lower carbon dioxideemissions of a chemical and / or manufacturing process.Surprisingly, it was found that heat from a chemical process can be recycled to a heat pump system. In particular, it was surprisingly found that waste heat originating from a heat recipient stream derived from the chemical process can be recycled to a heat transfer material stream of the heat pump system, which is used to transfer heat from a heat source stream derived from a manufacturing process to the chemical process to reduce external thermal energy need required for the operation of the chemical process, thus improving heat and energy efficiency of both the chemical process and the manufacturing process and contributing to the reduction of carbon dioxide emissions.Therefore, as a first alternative, the present invention relates to a method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain a liquid heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii) Expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l); iii) Compressing the stream HTMS2b(g) to obtain a stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .As a second alternative, the present invention relates to a method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i’) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain an at least partially gaseous heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii') Optionally, expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l); iii’) Compressing the stream HTMS2a from step i) or the stream HTMS2b(g) from step ii) to obtain a heat transfer material stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv’) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .According to the first alternative, it is preferred that the method comprises after step i) and prior to step ii) the additional steps ofi.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain a liquid heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii).According to the second alternative, it is preferred that the method comprises after step i') and prior to step ii’) the additional steps of i'.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain an at least partially gaseous heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii’) or step iii’).It is preferred that step ii) or ii’) further comprises a separation of the gaseous stream HTMS2b(g) and the liquid stream HTMS2b(l).It is preferred that the method comprises the additional steps of v) Separating prior to step i) or step i') at least part of the heat source stream HS1 , obtaining the additional heat source stream HST; vi) Transferring heat from the additional heat source stream HS1 ’ to a liquid heat transfer material stream MS1 , obtaining an additional heat source stream HS2’ having a lower thermal energy than the heat source stream HST and a liquid heat transfer material stream MS2 having a higher thermal energy than the liquid heat transfer material stream MS1 ; vii) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii’), step i.a) or step i'.a).Alternatively, it is preferred that the method comprises the additional steps of v’) Transferring heat from the stream HTMS4 after step iv) or step iv’) or HTMS5 to a liquid heat transfer material stream MS1 to obtain a heat transfer material stream HTMS6 having a reduced thermal energy than the stream HTMS4 or the stream HTMS5 and a liquid heat transfer material stream MS2 having a higher thermal energy than stream MS1 ; vi’) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii’), step i.a) or step i'.a).It is preferred that the streams HTMS1 , HTMS2a, HTMS2a’, HTMS2b(g), HTMS2b(l), HTMS3, HTMS4, HTMS5, MS1 and MS2 are streams of a heat transfer material HTM1 .In the case where said streams are streams of the heat transfer material HTM 1 , it is preferred that the heat transfer material HTM1 is selected from the group consisting of water, ammonia, carbon dioxide, n-propane, n-butane, isobutene, n-pentane, trans-1-chloro-3,3,3-trifluoropro- pene, 1 ,1 ,1 ,3,3-pentafluoropropane, 1 ,1 ,1 ,2-tetrafluoroethane, (1 E)-1 ,3,3,3-tetrafluoroprop-1-ene, (1Z)-1 ,3,3,3-tetrafluoroprop-1-ene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-butene or mixtures of two or more thereof.Further in the case where said streams are streams of the heat transfer material HTM 1 , it is preferred that the heat transfer material HTM1 is water.It is preferred that the stream HTMS1 has a temperature in the range of from 20 to 130 °C, more preferably in the range of from 30 to 120 °C, more preferably in the range of from 40 to 100 °C.It is preferred that the the stream HTMS1 has a pressure in the range of from from 0.025 bara to 2.9 bara, more preferably in the range of from 0.045 bara to 2.0 bara, more preferably in the range of from 0.075 to 1.1 bara.Alternatively, it is preferred that the the stream HTMS1 has a pressure in the range of from from 0.025 bara to 20 bara, more preferably in the range of from 0.045 bara to 15 bara, more preferably in the range of from 0.05 to 10 bara, more preferably in the range of from 0.075 to 1 .1 bara.It is preferred that the the stream HTMS2a has a temperature in the range of from 50 to 150 °C, more preferably in the range of from 60 to 120 °C, more preferably in the range of from 65 to 90 °C, more preferably in the range of from 70 to 80 °C.It is preferred that the the temperature of the stream HTMS2a is in the range of from >0 to <30 °C lower than the temperature of the stream HS1 , more preferably in the range of from >2.0 to < 20 °C, more preferably in the range of from >3.0 to <10 °C.It is preferred that the the stream HTMS2a’ has a temperature in the range of from 50 to 180 °C, more preferably in the range of from 60 to 135 °C, more preferably in the range of from 65 to 100 °C, more preferably in the range of from 70 to 80 °C.It is preferred that the the temperature of the stream HTMS2a’ is in the range of from >0 to <30 °C higher than the temperature of the stream HTMS2a, more preferably in the range of from > 2.0 to <15 °C, more preferably in the range of from >3.0 to <10°C.It is preferred that the the stream HTMS2b(g) has a temperature in the range of from 40 to 130 °C, more preferably in the range of from 50 to 120 °C, more preferably in the range of from 55 to 100 °C.It is preferred that the the stream HTMS2b(g) has a pressure in the range of from from 0.074 to 2.7 bara, more preferably in the range of from 0.12 to 1 .98 bara, more preferably in the range of from 0.15 to 1.0 bara.It is preferred that the the stream HTMS3 has a temperature in the range of from 80 to 200 °C, more preferably in the range of from 90 to 170 °C, more preferably in the range of from 120 to 160 °C, more preferably in the range of from 130 to 150 °C.It is preferred that the the stream HTMS3 has a pressure in the range of from 0.4 to 15.0 bara, more preferably in the range of from 0.6 to 7.5 bara, more preferably in the range of from 1 .5 to 6.0 bara.It is preferred that the the stream HTMS4 has a temperature in the range of from 75 to 195 °C more preferably in the range of from 85 to 165 °C, more preferably in the range of from 115 to 155 °C, more preferably in the range of from 120 to 145 °C.In the case where the process comprises the additional step i.a) or i’a), it is preferred that the the stream HTMS5 has a temperature in the range of from 50 to 120 °C, more preferably in the range of from 60 to 90 °C, more preferably in the range of from 70 to 80 °C.Further in the case where the process comprises the additional step i.a) or i’a), it is preferred that the temperature of the stream HTMS5 is in the range of from >0 to <20 °C higher than the temperature of the stream HTMS2a, more preferably in the range of from >1.0 to <15 °C, more preferably in the range of from >2.0 to <10 °C.In the case where the process comprises the additional step v) or v’), it is preferred that the stream MS1 has a temperature in the range of from 10 to 50 °C, more preferably in the range of from 15 to 40 °C, more preferably in the range of from 20 to 30 °C.Further in the case where the process comprises the additional step v) or v’), it is preferred that the stream MS1 has a pressure higher than the vapour pressure of HTM1 at the temperature of MS1 , more preferably in the range of from 0.1 to 5 bar higher than the vapour pressure, more preferably in the range of from 0.5 to 3 bar higher than the vapour pressure, more preferably 1 to 2 bar higher than the vapour pressure.Further in the case where the process comprises the additional step v) or v’), it is preferred that the stream MS2 has a temperature in the range of from 50 to 120 °C, more preferably in the range of from 60 to 90 °C, more preferably in the range of from 65 to 75 °C.Further in the case where the process comprises the additional step v) or v’), it is preferred that the stream HTSM6 has a temperature in the range of from 15 to 60 °C, more preferably in the range of from 20 to 45 °C, more preferably in the range of from 25 to 35 °C.Further in the case where the process comprises the additional step v) or v’), it is preferred that the temperature of the stream HTMS6 is in the range of from >0 to <30 °C higher than the temperature of the stream MS1 , more preferably in the range of from >2.0 to <15 °C, more preferably in the range of from >3.0 to <10°C.It is preferred that the compression in step iii) or step iii’) comprises compressing the stream HTMS2a or HTMS2b(g) in at least two subsequent compression steps.In the case where the compression in step iii) or step iii’) comprises compressing the stream HTMS2a or HTMS2b(g) in at least two subsequent compression steps, it is preferred that additional heat transfer material HTM1 is added in-between each compression step.In the case where additional heat transfer material HTM1 is added in-between each compression step, it is preferred that at least part of the heat transfer material stream MS2 is used as the source for the heat transfer material HTM1 .It is preferred that the stream HTMS5 after step i.a) or step i'.a) or HTMS6 after step v’) is released to the environment.It is preferred that the stream HTMS5 after step i.a) or step i'.a) or HTMS6 after step v’) is recycled to step i) or step i') as at least part of the stream HTMS1 and / or as at least part of the stream MS1 in step vi) or v’).In the case where the liquid stream HTMS2b(l) is obtained, it is preferred that the liquid stream HTMS2b(l) is recycled to step i) or step i') as at least part of the stream HTMS1.It is preferred that the heat recipient stream HR1 has a temperature in the range of from 50 to 190 °C, more preferably in the range of from 60 to 160 °C, more preferably in the range of from 75 to 140 °C.It is preferred that the heat recipient stream HR1 has a pressure in the range of from 0.1 to 100 bara, more preferably in the range of from 0.2to 50 bara, more preferably in the range of 0.3 to 10 bara, more preferably in the range of from 1 .5 to 2.5 bara.It is preferred that wherein the heat recipient stream HR2 has a temperature in the range of from 51 to 330 °C, more preferably in the range of from 80 to 250 °C, more preferably in the range of from 90 to 200 °C, more preferably in the range of from 100 to 150 °C.It is preferred that the temperature of the stream HR2 is in the range of from >0.5 to <140 °C higher than the temperature of the stream HR1 , more preferably in the range of from >0.75 to < 80 °C, more preferably in the range of from >1 to <50 °C, more preferably in the range of from > 1 to <25 °C, more preferably in the range of from >1.0 to <5.0 °C.It is preferred that the heat recipient stream HR1 is a process stream of a process, wherein preferably said process is a chemical process.It is preferred that the method of the present invention has a coefficient of performance (COP) of >1.5, preferably of >2, more preferably in the range of from 2.5 to 5, more preferably in the range of from 3.5 to 4It is preferred that the heat recipient stream HR1 is an absorbent regeneration stream ARS1 originating from a regenerator of an acid gas removal unit and the heat recipient stream HR2 is an absorbent regeneration stream ARS2 directed to the regenerator of the acid gas removal unit.It is preferred that the acid gas removal unit is a means for performing the following steps: a) an absorption step, wherein a fluid stream FS1 is contacted with an absorbent stream AS1 in an absorber to obtain an absorbent stream AS2 laden with acid gases and an at least partly deacidified fluid stream; b) a regeneration step, wherein at least a portion of the laden absorbent stream AS2 obtained from step a) is regenerated in a regenerator to obtain an at least partly regenerated absorbent stream AS3 and a gaseous stream GS comprising at least one acid gas; c) a recycling step, wherein at least a fraction of the regenerated absorbent A3 from step b) is recycled into the absorption step a).It is preferred that the at least one acid gas comprises carbon dioxide.It is preferred that the fluid stream FS1 is a flue gas stream from a combustion unit, wherein preferably FS1 comprises carbon dioxide.It is preferred that the absorbent streams AS1 , AS2 and AS3 comprise an absorbent material AM1.In the case where the absorbent streams AS1 , AS2 and AS3 comprise the absorbent material AM1 , it is preferred that the absorbent material AM1 comprises, preferably consists of, a basic absorber solution, preferably an aqueous basic amine absorber solution.In the case where the acid gas removal unit is a means for performing the steps a), b) and c), it is preferred that the absorber in absorption step a) comprises an absorber column.In the case where the absorber in absorption step a) comprises an absorber column, it is preferred that the absorber column comprises an inlet for the fluid stream FS1 at the bottom of the column.Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that the absorber column comprises an inlet for the absorbent stream AS1 in the upper section of the column.Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that the absorber column comprises absorption beds.Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that wherein the absorber column comprises an interstage cooler optionally driven by a pump, and more preferably not driven by a pump.In the case where the absorber column comprises an interstage cooler, it is preferred that the interstage cooler is installed between the absorption beds.Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that the absorber column is operated in a counter-current flow, and wherein FS1 is contacted with AS1 .Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that wherein the absorber column comprises an outlet of the absorbent stream AS2 at the bottom of the column.Further in the case where the absorber in absorption step a) comprises an absorber column, it is preferred that the absorber column comprises an outlet of a fluid stream FS2 at the head of the column.Further in the case where the acid gas removal unit is a means for performing the steps a), b) and c), it is preferred that the regenerator in the regeneration step b) comprises a reboiler and a desorber column.In the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that thermal energy is transferred from the heat source stream HS1 to the reboiler of the regenerator, wherein the reboiler comprises the absorbent regeneration streams ARS1 and ARS2.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that thermal energy is transferred from the reboiler to the desorber column.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises an inlet of the absorbent stream AS2 in the upper section of the column.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises an inlet of the absorbent regeneration stream ARS2 at the lower section of the column.In the case where the desorber column comprises an inlet of the absorbent regeneration stream ARS2 at the lower section of the column, it is preferred that the absorbent regeneration stream ARS2 comprises steam.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column is operated in a counter-current flow, and wherein ARS2 is contacted with AS2.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises an outlet of the absorbent stream AS3 at the bottom of the column.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises an outlet of the absorbent regeneration stream ARS1 in the middle section of the column.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises an outlet of the gaseous stream GS at thehead of the column.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the desorber column comprises two separate regeneration columns connected in series, optionally with an additional heat exchanger between the two columns, wherein the heat exchanger can be operated by external heat or by exchanging heat from the absorbent AS3 to the partly regenerated absorption solution obtained from the first of the two regeneration columns.In the case where the desorber column comprises two separate regeneration columns connected in series with an additional heat exchanger between the two columns, it is preferred that the desorber column comprises a further heat exchanger, wherein heat is exchanged from the absorbent AS3 downstream of the additional heat exchanger to the absorbent AS2 upstream of the first of the two regeneration columns.Further in the case where the regenerator in the regeneration step b) comprises a reboiler and a desorber column, it is preferred that the absorbent AS2 is an aqueous basic amine absorber solution, and wherein the gaseous stream GS is subjected to a cooling step to obtain a liquid stream comprising water and a gaseous stream comprising carbon dioxide, wherein the cooling step is conducted in a condenser unit located downstream of the desorber column.It is preferred that the heat source stream HS1 comprises a process or product stream of a chemical process.In the case where the heat source stream HS1 comprises a process or product stream of a chemical process, it is preferred that the heat source stream HS1 has a temperature in the range of from from 50 to 120 °C, more preferably in the range of from 50 to 100 °C, more preferably in the range of from 60 to 90 °C, more preferably in the range of from 70 to 80 °C.Further in the case where the heat source stream HS1 comprises a process or product stream of a chemical process, it is preferred that the heat source stream HS1 has a flow rate in the range of from 1 to 5000 t / h, more preferably in the range of from 5 to 4000 t / hr, more preferably in the range of from 10 to 3500 t / hr, more preferably in the range of from 100 to 3000 t / hr, more preferably in the range of from 200 to 2600, more preferably in the range of from 500 to 1500 t / h, more preferably in the range of from 800 to 1200 t / h.In the case where the heat source stream HS1 comprises a process or product stream of a chemical process, it is preferred that the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials.In the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that oil refining comprises one or more selected from the group consisting of catalytic cracking, steam cracking, catalytic reforming, and hydrocracking.Further in the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that natural gas processing comprises one or more selected from the group consisting of adsorption operations, absorption operations, and fractionation operations.Further in the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that food processing comprises one or more selected from the group consisting of primary, secondary, and tertiary food processing.Further in the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that manufacturing of chemical compounds comprises one or more selected from the group consisting of production and formulation of pharmaceutical compounds and production of basic, fine, and specialty chemicals.Further in the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that manufacturing of polymers comprises one or more selected from the group consisting of synthesis of polymers, pre-shaping operations, shaping operations, and post-shaping operations.Further in the case where the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials, it is preferred that material manufacturing comprises one or more selected from the group consisting of the production of metals, alloys, glass, and paper.Further in the case where the heat source stream HS1 comprises a process or product stream of a chemical process, the heat source stream HS1 is a water stream from a water quench column.In the case where the heat source stream HS1 is a water stream from a water quench column, it is preferred that the water-quench column is part of a process for the production of a cracker product from a hydrocarbon feedstock.In the case where the water-quench column is part of a process for the production of a cracker product from a hydrocarbon feedstock, it is preferred that the process for the production of the cracker product comprises a steam cracking process.In the case where the the process for the production of the cracker product comprises a steam cracking process, it is preferred that the steam cracking process comprises one or more steam cracking furnaces.In the case where the steam cracking process comprises one or more steam cracking furnaces, it is preferred that in the one or more cracking furnace the hydrocarbon feedstock is cracked to obtain a cracked gas.In the case where the steam cracking process comprises one or more steam cracking furnaces, it is preferred that the one or more steam cracking furnaces are heated by the combustion of a carbonaceous fuel.Further in the case where the the process for the production of the cracker product comprises a steam cracking process, it is preferred that the steam cracking process comprises an oil quench.Further in the case where the the process for the production of the cracker product comprises a steam cracking process, it is preferred that the steam cracking process comprises a water quench.Further in the case where the the process for the production of the cracker product comprises a steam cracking process, it is preferred that the steam cracking process comprises one or more post processing steps of the cracked gas.In the case where the the steam cracking process comprises one or more post processing steps of the cracked gas, it is preferred that the one or more post processing steps further comprises a step for separating ethylene from the cracked gas.Further in the case where the water-quench column is part of a process for the production of a cracker product from a hydrocarbon feedstock, it is preferred that the hydrocarbon feedstock comprises, more preferably consists of, gaseous and / or liquid hydrocarbons.In the case where the hydrocarbon feedstock comprises gaseous and / or liquid hydrocarbons, it is preferred that the hydrocarbon feedstock is selected from the group consisting of C2-C4-al- kanes, naphtha, gas oil and hydrocracker residues.Further in the case where the water-quench column is part of a process for the production of a cracker product from a hydrocarbon feedstock, it is preferred that the cracker product is selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines and aromatic compounds, and mixtures of two or more thereof.In the case where the cracker product is selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines and aromatic compounds, and mixtures of two or more thereof, it is preferred that the alkene cracker product is selected from the group consisting of ethene, propene, butenes, pentenes, hexenes, heptenes, octenes and dodecens, and mixtures of two or more thereof, wherein more preferably butenes are selected from 1 -butene, 2-butene, isobutylene and 1 ,3- butadiene; wherein more preferably hexenes are selected from 1 -hexene, 2-hexene, 3-hexene, 2-methyl-1- pentene, 3-methyl-1 -pentene, 4-methyl-1 -pentene, 2-methyl-2-pentene, 3-methyl-2-pentene, 4- methyl-2-pentene, 2, 3-dimethyl-1 -butene, 3, 3-dimethyl-1 -butene, 2,3-dimethyl-2-butene and 2- ethyl-1 -butene; wherein more preferably heptenes are selected from 1 -heptene, 2-heptene, 3-heptene, methylhexenes, dimethylpentenes, ethylpentenes and trimethylbutene; wherein more preferably octenes are selected from 1 -octene, 2-octene, 3-octene and 4-octene,isooctenes, dimethylhexenes, methylheptenes and any dimers formed from C4-alkenes; wherein more preferably isooctenes are selected from diisobutene and 2,4,4-trimethylpentene; wherein more preferably dodecenes are selected from any trimers formed from C4-alkenes.Further in the case where the cracker product is selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines and aromatic compounds, and mixtures of two or more thereof, it is preferred that the alkine cracker product is selected from the group consisting of ethine, propine and butines, and mixtures of two or more thereof, wherein more preferably butines are selected from 1-butine and 2-butine.Further in the case where the cracker product is selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines and aromatic compounds, and mixtures of two or more thereof, it is preferred that the aromatic compound cracker product is selected from the group consisting of benzenes, more preferably ethylbenzene, benzene, toluene, styrene and xylene.Further, the present invention relates to an apparatus for transferring heat from a heat source stream HS1 to a heat recpient stream HR1 according to the method according to any of the embodiments disclosed herein, comprising:A) A first heat exchanger HE1 with an inlet for a heat source stream HS1 and an outlet for a heat source stream HS2, an inlet for a heat transfer material stream HTMS1 and an outlet for a heat transfer material HTMS2a;B) Optionally, a third heat exchanger HE3 with an inlet for the heat transfer material stream HTMS2a and an outlet for a heat transfer material stream HTMS2a’ and an inlet for a heat transfer material stream HTMS4 and an outlet for heat transfer material stream HTMS5;C) Optionally, an evaporation means E1 for at least partially evaporating the heat transfer material stream HTMS2a or HTMS2a’ with an inlet for a heat transfer material stream HTMS2a or HTMS2a’ and an outlet for a gaseous heat transfer material stream HTMS2b(g) and an outlet for a liquid heat transfer material stream HTMS2(I);D) One or more compressors (CP1 On) for compressing the heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a' , wherein each compressor comprises an inlet for heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a’ from the heat exchanger HE1 or optionally from the heat exchanger HE3 or optionally from the evaporation means E1 or from the previous compressor and each with an outlet of heat transfer material stream HTMS3 to the next compressor or to the heat exchanger HE2;E) A second heat exchanger HE2 with an inlet for the heat transfer material stream HTMS3 and an outlet for the heat transfer material stream HTMS4 and an inlet for a heat recipient stream HR1 and an outlet for heat recipient stream HR2.It is preferred that the apparatus further comprises a separation means S1 for separating the heat transfer material HTMS2a or HTMSa’, preferably an at least partially gaseous heat transfer material HTMS2a or HTMSa’comprising the gaseous heat transfer material stream HTMS2b(g) and the liquid heat transfer material stream HTMS2(I), into separate streams of the gaseous heat transfer material stream HTMS2b(g) and the liquid heat transfer material stream HTMS2(I), wherein the separation means S1 comprises an inlet for a heat transfer material stream HTMS2a or HTMS2a’ and an outlet for a gaseous heat transfer material stream HTMS2b(g) and an outlet for a liquid heat transfer material stream HTMS2(I).In the case where the apparatus further comprises a separation means S1 , it is preferred that said apparatus does not comprise the evaporation means E1 .It is preferred that the apparatus further comprises a fourth heat exchanger HE4 with an inlet for the heat transfer material stream HTMS4, the heat transfer material stream HTMS5 or a heat source stream HS1 ’ and an outlet for a heat transfer material stream HTMS6 or a heat source stream HS2’ and an inlet for a second heat transfer material stream MS1 and an outlet for a second heat transfer material stream MS2.It is preferred that said apparatus does not comprise a third heat exchanger HE3.It is preferred that the evaporation means E1 in C) comprises one or more expanders (EP1 EPn).In the case where the evaporation means E1 in C) comprises one or more expanders (EP1 EPn), it is preferred that the one or more expanders (EP1 EPn) comprise a turbine, a throttle and / or a valve.It is preferred that wherein the one or more compressors in D) comprises at least two compressors (CP1 CPn).In the case where the the one or more compressors in D) comprises at least two compressors (CP1 CPn), it is preferred that the at least two compressors (CP1 CPn) comprise an inlet for the heat transfer material stream MS2 in-between each of the compressors.Yet further, the present invention relates to a use of the apparatus according to any of the embodiments disclosed herein for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 .The present invention further relates to a method as described above, preferably the method comprising (i) to (iv) or (i') to (iv’), as described above, wherein said method (further) comprises the step of converting the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method described herein or a chemical material obtainable or obtainedby the method described herein, to obtain a product Q. Said product Q is preferably selected from building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma corn-position; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acry- late hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Further regarding said product Q, it is preferred that the content of the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method described herein in the product Q is 1 weight-% or more, more preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or the content of the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method described herein in the product Q is 100 weight-% or less, more preferably 95 weight-% or less, more preferably 90 weight-% or less, more prefer-ably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and wherein the content is preferably determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the product Q referred to in the preceding paragraph is a product as described in Reference RF1 ; paragraphs

[1000] to

[8005] , Preferably, the method described herein is further a method for the production of a product referred to in the preceding paragraph.The converting step to obtain the product Q preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and / or steam cracking; and / or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1 ; paragraphs

[1000] to

[8005] ,The term “building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a high-er structural complexity and / or higher molecular weight than the building block on which the sec-ondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas compris-ing a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic com-pounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term “monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acry- lates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term “intermediate compound”, as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI).The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term “polymer A”, as used in the context of the product Q herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1.The term “polymer composition A”, as used in the context of the product Q herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and / or flame retardant, and is defined in more detail in paragraph

[2008] of Reference RF1 .The term “polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1 .The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1.The term “industrial use polymer”, as used in the context of the product Q herein, comprises rhe-ology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, poly- ether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1 . The term “industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1. The term “industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1. The term “industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lac-tate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aro-matic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1 . The term “industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Ref-erence RF1 . The term “composition and / or formulation thereof’ with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Refer-ence RF1 . The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1 . The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1 .The term “agrochemical composition”, as used in the context of the product Q herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph

[4001] ,The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grube- mann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof’ may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used in the context of the product Q herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used in the context of the product Q herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1.The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used in the con-text of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any com-binations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls includ-ing their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate,propionic acid and am-monium propionate, formic acid and propionic acid, formic acid and sodium formiate and propi-onic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrroli- done-copolymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1.The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used in the context of the product Q here-in, comprise a volatile organic substance with a molecular weight between 70-250 g / mol com-prising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more de-tail in paragraph

[5003] of Reference RF1.The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term “aqueous polymer dispersion”, as used in the context of the product Q herein, com- pris-es aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled “aqueous polymer dispersion” of Reference RF1. The dispersed polymers) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsion polymer”, as used herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersions) are defined in more detail in the section

[6002] entitled “Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth)acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term “polymeric dispersant”, as used in the context of the product Q herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled “Polymeric dispersant” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled “Emulsion polymerization” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled “Process for the preparation of aqueous poly-urethane dispersions” and section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1. Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section

[6004] entitled “Uses of aqueous polymer dispersions”, section

[6005] entitled “Binders for architectural and construction coatings” section

[6006] entitled “Binders for paper coating” section

[6007] entitled “Binders for fiber bonding” section

[6008] entitled “Adhesive polymers and adhesive compositions” section

[6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section

[6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” section

[6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositionsUV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled “UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hot melt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1 .Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled “Polyisocyanates” of Reference RF1 .Hyperbranched polyester polyol(s) and its / their uses are defined in more detail in section

[6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating com-positions” of Reference RF1 . The converting step(s) to obtain the hyperbranched polyester poly-ols is / are defined in more detail in the section

[6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1. Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled “Organic solvent based twocompo-nent coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1 .Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1 .100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1 .Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1. The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1. The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1 . The term “inorganic binder composition” comprising the polymeric dispersants), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Refer-ence RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1.The term “cosmetic surfactant”, as used in the context of the product Q herein, comprises nonionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1 . The term “emollient”, as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1 . The term “wax”, as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1 . The term “cosmetic polymer”, as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term “UV filter”, as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1. The term “further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Com-mission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredi-ents. The term “composition and / or formulation thereof’ with reference to the cosmetic surfac-tant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to per-sonal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1. The converting step(s) to obtain the cosmetic surfactant,emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1.The terms “polymer B”, “polymer composition B”, “coating composition”, “other functional composition”, “foil”, “molded body”, “coating” and “coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The catalyst of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The catalyst of any one of embodiments 1 , 2, 3, and 4". Further, it is explicitly noted that the following set of embodiments is not the set of claims determining the extent of protection, but represents a suitably structured part of the description directed to general and preferred aspects of the present invention.1 . A method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain a liquid heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii) Expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l); iii) Compressing the stream HTMS2b(g) to obtain a stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .2. A method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i’) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain an at least partially gaseous heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii') Optionally, expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l);iii’) Compressing the stream HTMS2a from step i) or the stream HTMS2b(g) from step ii) to obtain a heat transfer material stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv’) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .3. The method according to embodiment 1 , comprising after step i) and prior to step ii) the additional steps of i.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain a liquid heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii).4. The method according to embodiment 2, comprising after step i') and prior to step ii’) the additional steps of i'.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain an at least partially gaseous heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii’) or step iii’).5. The method according to any of embodiments 1 to 4, wherein step ii) or ii’) further comprises a separation of the gaseous stream HTMS2b(g) and the liquid stream HTMS2b(l).6. The method according to any of embodiments 1 to 5, comprising the additional steps of v) Separating prior to step i) or step i') at least part of the heat source stream HS1 , obtaining the additional heat source stream HS1 ’; vi) Transferring heat from the additional heat source stream HS1 ’ to a liquid heat transfer material stream MS1 , obtaining an additional heat source stream HS2’ having a lower thermal energy than the heat source stream HS1 ’ and a liquid heat transfer material stream MS2 having a higher thermal energy than the liquid heat transfer material stream MS1 ; vii) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii’), step i.a) or step i'.a).7. The method according to any of embodiments 1 to 5, comprising the additional steps of v’) Transferring heat from the stream HTMS4 after step iv) or step iv’) or HTMS5 to a liquid heat transfer material stream MS1 to obtain a heat transfer material stream HTMS6 having a reduced thermal energy than the stream HTMS4 or the stream HTMS5 and a liquid heat transfer material stream MS2 having a higher thermal energy thanstream MS1 ; vi’) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii ’), step i.a) or step i'.a).8. The method according to any of embodiments 1 to 7, wherein the streams HTMS1 , HTMS2a, HTMS2a’, HTMS2b(g), HTMS2b(l), HTMS3, HTMS4, HTMS5, MS1 and MS2 are streams of a heat transfer material HTM1 .9. The method according to embodiment 8, wherein the heat transfer material HTM 1 is selected from the group consisting of water, ammonia, carbon dioxide, n-propane, n-bu- tane, isobutene, n-pentane, trans-1-chloro-3,3,3-trifluoropropene, 1 ,1 ,1 ,3,3-pentafluoro- propane, 1 ,1 ,1 ,2-tetrafluoroethane, (1 E)-1 ,3,3,3-tetrafluoroprop-1-ene, (1 Z)- 1 ,3,3, 3-tetra- fluoroprop-1-ene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-butene or mixtures of two or more thereof.10. The method according to embodiment 8 or 9, wherein the heat transfer material HTM 1 is water.11 . The method according to any of embodiments 1 to 10, wherein the stream HTMS1 has a temperature in the range of from 20 to 130 °C, preferably in the range of from 30 to 120 °C, more preferably in the range of from 40 to 100 °C.12. The method according to any of embodiments 1 to 11 , wherein the stream HTMS1 has a pressure in the range of from from 0.025 bara to 2.9 bara, preferably in the range of from 0.045 bara to 2.0 bara, more preferably in the range of from 0.075 to 1.1 bara.13. The method according to any of embodiments 1 to 11 , wherein the stream HTMS1 has a pressure in the range of from from 0.025 bara to 20 bara, preferably in the range of from 0.045 bara to 15 bara, more preferably in the range of from 0.05 to 10 bara, more preferably in the range of from 0.075 to 1.1 bara.14. The method according to any of embodiments 1 to 13, wherein the stream HTMS2a has a temperature in the range of from 50 to 150 °C, preferably in the range of from 60 to 120 °C, more preferably in the range of from 65 to 90 °C, more preferably in the range of from 70 to 80 °C.15. The method according to any of embodiments 1 to 14, wherein the temperature of the stream HTMS2a is in the range of from >0 to <30 °C lower than the temperature of the stream HS1 , preferably in the range of from >2.0 to <20 °C, more preferably in the range of from >3.0 to <10 °C.16. The method according to any of embodiments 3 to 15 wherein the stream HTMS2a’ has a temperature in the range of from 50 to 180 °C, preferably in the range of from 60 to 135 °C, more preferably in the range of from 65 to 100 °C, more preferably in the rangeof from 70 to 80 °C. The method according to any of embodiments 1 to 16, wherein the temperature of the stream HTMS2a’ is in the range of from >0 to <30 °C higher than the temperature of the stream HTMS2a, preferably in the range of from >2.0 to <15 °C, more preferably in the range of from >3.0 to <10°C. The method according to any of embodiments 1 to 17, wherein the stream HTMS2b(g) has a temperature in the range of from 40 to 130 °C, preferably in the range of from 50 to 120 °C, more preferably in the range of from 55 to 100 °C.[60 °C] The method according to any of embodiments 1 to 18, wherein the stream HTMS2b(g) has a pressure in the range of from from 0.074 to 2.7 bara, more preferably in the range of from 0.12 to 1.98 bara, more preferably in the range of from 0.15 to 1.0 bara. The method according to any of embodiments 1 to 19, wherein the stream HTMS3 has a temperature in the range of from 80 to 200 °C, preferably in the range of from 90 to 170 °C, more preferably in the range of from 120 to 160 °C, more preferably in the range of from 130 to 150 °C. The method according to any of claims 1 to 20, wherein the stream HTMS3 has a pressure in the range of from 0.4 to 15.0 bara, preferably in the range of from 0.6 to 7.5 bara, more preferably in the range of from 1 .5 to 6.0 bara. The method according to any of embodiments 1 to 21 , wherein the stream HTMS4 has a temperature in the range of from 75 to 195 °C preferably in the range of from 85 to 165 °C, more preferably in the range of from 115 to 155 °C, more preferably in the range of from 120 to 145 °C. The method according to any of embodiments 3 to 22, wherein the stream HTMS5 has a temperature in the range of from 50 to 120 °C, preferably in the range of from 60 to 90 °C, more preferably in the range of from 70 to 80 °C. The method according to any of embodiments 3 to 23, wherein the temperature of the stream HTMS5 is in the range of from >0 to <20 °C higher than the temperature of the stream HTMS2a, preferably in the range of from >1 .0 to <15 °C, more preferably in the range of from >2.0 to <10 °C. The method according to any of embodiments 6 to 24, wherein the stream MS1 has a temperature in the range of from 10 to 50 °C, preferably in the range of from 15 to 40 °C,more preferably in the range of from 20 to 30 °C.26. The method according to any of embodiments 6 to 25, wherein the stream MS1 has a pressure higher than the vapour pressure of HTM1 at the temperature of MS1 , preferably in the range of from 0.1 to 5 bar higher than the vapour pressure, more preferably in the range of from 0.5 to 3 bar higher than the vapour pressure, more preferably 1 to 2 bar higher than the vapour pressure.27. The method according to any of embodiments 6to 26, wherein the stream MS2 has a temperature in the range of from 50 to 120 °C, preferably in the range of from 60 to 90 °C, more preferably in the range of from 65 to 75 °C.28. The method according to any of embodiments 6 to 27, wherein the stream HTSM6 has a temperature in the range of from 15 to 60 °C, preferably in the range of from 20 to 45 °C, more preferably in the range of from 25 to 35 °C.29. The method according to any of embodiments 6 to 28, wherein the temperature of the stream HTMS6 is in the range of from >0 to <30 °C higher than the temperature of the stream MS1 , preferably in the range of from >2.0 to <15 °C, more preferably in the range of from >3.0 to <10°C.30. The method according to any of embodiments 1 to 29, wherein the compression in step iii) or step iii’) comprises compressing the stream HTMS2a or HTMS2b(g) in at least two subsequent compression steps.31 . The method according to embodiment 30, wherein additional heat transfer material HTM1 is added in-between each compression step.32. The method according to embodiment 31 , wherein at least part of the heat transfer material stream MS2 is used as the source for the heat transfer material HTM1.33. The method according to any of embodiments 1 to 32, wherein the stream HTMS5 after step i.a) or step i'.a) or HTMS6 after step v’) is released to the environment.34. The method according to any of embodiments 1 to 33, wherein the stream HTMS5 after step i.a) or step i'.a) or HTMS6 after step v’) is recycled to step i) or step i') as at least part of the stream HTMS1 and / or as at least part of the stream MS1 in step vi) or v’).35. The method according to any of embodiments 1 to 34, wherein the liquid stream HTMS2b(l) is obtained, wherein the liquid stream HTMS2b(l) is recycled to step i) or step i') as at least part of the stream HTMS1.36. The method according to any of embodiments 1 to 35, wherein the heat recipient stream HR1 has a temperature in the range of from 50 to 190 °C, preferably in the range of from 60 to 160 °C, more preferably in the range of from 75 to 140 °C.37. The method according to any of embodiments 1 to 36, wherein the heat recipient stream HR1 has a pressure in the range of from 0.1 to 100 bara, preferably in the range of from 0.2to 50 bara, more preferably in the range of 0.3 to 10 bara, more preferably in the range of from 1.5 to 2.5 bara.38. The method according to any of embodiments 1 to 37, wherein the heat recipient stream HR2 has a temperature in the range of from 51 to 330 °C, preferably in the range of from 80 to 250 °C, more preferably in the range of from 90 to 200 °C, more preferably in the range of from 100 to 150 °C.39. The method according to any of embodiments 1 to 38, wherein the temperature of the stream HR2 is in the range of from >0.5 to <140 °C higher than the temperature of the stream HR1 , preferably in the range of from >0.75 to <80 °C, more preferably in the range of from >1 to <50 °C, more preferably in the range of from >1 to <25 °C, more preferably in the range of from >1.0 to <5.0 °C.40. The method according to any of embodiments 1 to 39, wherein the heat recipient stream HR1 is a process stream of a process, wherein preferably said process is a chemical process.41 . The method according to any one of embodiments 1 to 40, wherein said method has a coefficient of performance (COP) of >1 .5, preferably of >2, more preferably in the range of from 2.5 to 5, more preferably in the range of from 3.5 to 4.42. The method according to any one of embodiments 1 to 41 , wherein the heat recipient stream HR1 is an absorbent regeneration stream ARS1 originating from a regenerator of an acid gas removal unit and the heat recipient stream HR2 is an absorbent regeneration stream ARS2 directed to the regenerator of the acid gas removal unit.43. The method according to embodiment 42, wherein the acid gas removal unit is a means for performing the following steps: a) an absorption step, wherein a fluid stream FS1 is contacted with an absorbent stream AS1 in an absorber to obtain an absorbent stream AS2 laden with acid gases and an at least partly deacidified fluid stream;b) a regeneration step, wherein at least a portion of the laden absorbent stream AS2 obtained from step a) is regenerated in a regenerator to obtain an at least partly regenerated absorbent stream AS3 and a gaseous stream GS comprising at least one acid gas; c) a recycling step, wherein at least a fraction of the regenerated absorbent A3 from step b) is recycled into the absorption step a).44. The method according to embodiment 43, wherein the at least one acid gas comprises carbon dioxide.45. The method according to embodiment 43 or 44, wherein the fluid stream FS1 is a flue gas stream from a combustion unit, wherein preferably FS1 comprises carbon dioxide.46. The method according to any of embodiments 43 to 45, wherein the absorbent streams AS1 , AS2 and AS3 comprise an absorbent material AM1 .47. The method according to embodiment 46, wherein the absorbent material AM1 comprises, preferably consists of, a basic absorber solution, preferably an aqueous basic amine absorber solution.48. The method according to any of embodiments 43 to 47, wherein the absorber in absorption step a) comprises an absorber column.49. The method according to embodiment 48, wherein the absorber column comprises an inlet for the fluid stream FS1 at the bottom of the column.50. The method according to embodiment 48 or 49, wherein the absorber column comprises an inlet for the absorbent stream AS1 in the upper section of the column.51 . The method according to any of embodiments 48 to 50, wherein the absorber column comprises absorption beds.52. The method according to any of embodiments 48 to 51 , wherein the absorber column comprises an interstage cooler optionally driven by a pump, and preferably not driven by a pump.53. The method according to embodiment 52, wherein the interstage cooler is installed between the absorption beds.54. The method according to any of embodiments 48 to 53, wherein the absorber column is operated in a counter-current flow, and wherein FS1 is contacted with AS1 .55. The method according to any of embodiments 48 to 54, wherein the absorber column comprises an outlet of the absorbent stream AS2 at the bottom of the column.56. The method according to any of embodiments 48 to 55, wherein the absorber column comprises an outlet of a fluid stream FS2 at the head of the column.57. The method according to any of embodiments 43 to 56, wherein the regenerator in the regeneration step b) comprises a reboiler and a desorber column.58. The method according to embodiment 57, wherein thermal energy is transferred from the heat source stream HS1 to the reboiler of the regenerator, wherein the reboiler comprises the absorbent regeneration streams ARS1 and ARS2.59. The method according to embodiment 57 or 58, wherein thermal energy is transferred from the reboiler to the desorber column.60. The method according to any of embodiments 57 to 59, wherein the desorber column comprises an inlet of the absorbent stream AS2 in the upper section of the column.61 . The method according to any of embodiments 57 to 60, wherein the desorber column comprises an inlet of the absorbent regeneration stream ARS2 at the lower section of the column.62. The method according to embodiment 61 , wherein the absorbent regeneration stream ARS2 comprises steam.63. The method according to any of embodiments 57 to 62, wherein the desorber column is operated in a counter-current flow, and wherein ARS2 is contacted with AS2.64. The method according to any of embodiments 57 to 63, wherein the desorber column comprises an outlet of the absorbent stream AS3 at the bottom of the column.65. The method according to any of embodiments 57 to 64, wherein the desorber column comprises an outlet of the absorbent regeneration stream ARS1 in the middle section of the column.66. The method according to any of embodiments 57 to 65, wherein the desorber column comprises an outlet of the gaseous stream GS at thehead of the column.67. The method according to any of embodiments 57 to 66, wherein the desorber column comprises two separate regeneration columns connected in series, optionally with an additional heat exchanger between the two columns, wherein the heat exchanger can beoperated by external heat or by exchanging heat from the absorbent AS3 to the partly regenerated absorption solution obtained from the first of the two regeneration columns.68. The method according to embodiment 67, wherein the desorber column comprises a further heat exchanger, wherein heat is exchanged from the absorbent AS3 downstream of the additional heat exchanger to the absorbent AS2 upstream of the first of the two regeneration columns.69. The method according to any of embodiments 57 to 68, wherein the absorbent AS2 is an aqueous basic amine absorber solution, and wherein the gaseous stream GS is subjected to a cooling step to obtain a liquid stream comprising water and a gaseous stream comprising carbon dioxide, wherein the cooling step is conducted in a condenser unit located downstream of the desorber column.70. The method according to any of embodiments 1 to 69, wherein the heat source stream HS1 comprises a process or product stream of a chemical process.71 . The method according to embodiment 70, wherein the heat source stream HS1 has a temperature in the range of from from 50 to 120 °C, preferably in the range of from 50 to 100 °C, more preferably in the range of from 60 to 90 °C, more preferably in the range of from 70 to 80 °C.72. The method according to embodiment 70 or 71 , wherein the heat source stream HS1 has a flow rate in the range of from 1 to 5000 t / h, preferably in the range of from 5 to 4000 t / hr, more preferably in the range of from 10 to 3500 t / hr, more preferably in the range of from 100 to 3000 t / hr, more preferably in the range of from 200 to 2600, more preferably in the range of from 500 to 1500 t / h, more preferably in the range of from 800 to 1200 t / h.73. The method according to any of embodiments 70 to 72, wherein the chemical process is selected from the group consisting of oil refining, natural gas processing, food processing and manufacturing of chemical compounds, polymers, and materials.74. The method according to embodiment 73, wherein oil refining comprises one or more selected from the group consisting of catalytic cracking, steam cracking, catalytic reforming, and hydrocracking.75. The method according to embodiment 73 or 74, wherein natural gas processing comprises one or more selected from the group consisting of adsorption operations, absorption operations, and fractionation operations.76. The method according to any of embodiments 73 to 75, wherein food processing comprises one or more selected from the group consisting of primary, secondary, and tertiary food processing.77. The method according to any of embodiments 73 to 76, wherein manufacturing of chemical compounds comprises one or more selected from the group consisting of production and formulation of pharmaceutical compounds and production of basic, fine, and specialty chemicals.78. The method according to any of embodiments 73 to 77, wherein manufacturing of polymers comprises one or more selected from the group consisting of synthesis of polymers, pre-shaping operations, shaping operations, and post-shaping operations.79. The method according to any of embodiments 73 to 78, wherein material manufacturing comprises one or more selected from the group consisting of the production of metals, alloys, glass, and paper.80. The method according to any of embodiments 70 to 79, wherein the heat source stream HS1 is a water stream from a water quench column.81 . The method according to embodiment 80, wherein the water-quench column is part of a process for the production of a cracker product from a hydrocarbon feedstock.82. The method according to embodiment 81 , wherein the process for the production of the cracker product comprises a steam cracking process.83. The method according to embodiment 82, wherein the steam cracking process comprises one or more steam cracking furnaces.84. The method according to embodiment 83, wherein in the one or more cracking furnace the hydrocarbon feedstock is cracked to obtain a cracked gas.85. The method according to embodiment 83 or 84, wherein the one or more steam cracking furnaces are heated by the combustion of a carbonaceous fuel.86. The method according to any of embodiments 83 to 85, wherein the steam cracking process comprises an oil quench.87. The method according to any of embodiments 82 to 86, wherein the steam cracking process comprises a water quench.88. The method according to any of embodiments 82 to 87, wherein the steam cracking process comprises one or more post processing steps of the cracked gas.89. The method according to embodiment 88, wherein the one or more post processing steps further comprises a step for separating ethylene from the cracked gas.90. The method according to any of embodiments 81 to 89, wherein the hydrocarbon feedstock comprises, preferably consists of, gaseous and / or liquid hydrocarbons.91 . The method according to embodiment 90, wherein the hydrocarbon feedstock is selected from the group consisting of C2-C4-alkanes, naphtha, gas oil and hydrocracker residues.92. The method according to any of embodiments 81 to 91 , wherein the cracker product is selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines and aromatic compounds, and mixtures of two or more thereof.93. The method according to embodiment 92, wherein the alkene cracker product is selected from the group consisting of ethene, propene, butenes, pentenes, hexenes, heptenes, octenes and dodecens, and mixtures of two or more thereof, wherein preferably butenes are selected from 1 -butene, 2-butene, isobutylene and 1 ,3- butadiene; wherein preferably hexenes are selected from 1 -hexene, 2-hexene, 3-hexene, 2-methyl- 1 -pentene, 3-methyl-1 -pentene, 4-methyl-1 -pentene, 2-methyl-2-pentene, 3-methyl-2- pentene, 4-methyl-2-pentene, 2, 3-dimethyl-1 -butene, 3, 3-dimethyl-1 -butene, 2,3-dime- thyl-2-butene and 2-ethyl-1 -butene; wherein preferably heptenes are selected from 1 -heptene, 2-heptene, 3-heptene, methylhexenes, dimethylpentenes, ethylpentenes and trimethylbutene; wherein preferably octenes are selected from 1 -octene, 2-octene, 3-octene and 4-oc- tene, isooctenes, dimethylhexenes, methyl heptenes and any dimers formed from C4- alkenes; wherein preferably isooctenes are selected from diisobutene and 2,4,4-trimethylpentene; wherein preferably dodecenes are selected from any trimers formed from C4-alkenes.94. The method according to any of embodiments 92 or 93, wherein the alkine cracker product is selected from the group consisting of ethine, propine and butines, and mixtures of two or more thereof, wherein preferably butines are selected from 1-butine and 2-butine.95. The method according to any of embodiments 92 to 94, wherein the aromatic compound cracker product is selected from the group consisting of benzenes, preferably ethylbenzene, benzene, toluene, styrene and xylene.96. An apparatus for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 according to the method of any of embodiments 1 to 95, comprising:A) A first heat exchanger HE1 with an inlet for a heat source stream HS1 and an outlet for a heat source stream HS2, an inlet for a heat transfer material stream HTMS1 and an outlet for a heat transfer material HTMS2a;B) Optionally, a third heat exchanger HE3 with an inlet for the heat transfer material stream HTMS2a and an outlet for a heat transfer material stream HTMS2a’ and an inlet for a heat transfer material stream HTMS4 and an outlet for heat transfer material stream HTMS5;C) Optionally, an evaporation means E1 for at least partially evaporating the heat transfer material stream HTMS2a or HTMS2a’ with an inlet for a heat transfer material stream HTMS2a or HTMS2a’ and an outlet for a gaseous heat transfer material stream HTMS2b(g) and an outlet for a liquid heat transfer material stream HTMS2(I);D) One or more compressors (CP1 On) for compressing the heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a' , wherein each compressor comprises an inlet for heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a’ from the heat exchanger HE1 or optionally from the heat exchanger HE3 or optionally from the evaporation means E1 or from the previous compressor and each with an outlet of heat transfer material stream HTMS3 to the next compressor or to the heat exchanger HE2;E) A second heat exchanger HE2 with an inlet for the heat transfer material stream HTMS3 and an outlet for the heat transfer material stream HTMS4 and an inlet for a heat recipient stream HR1 and an outlet for heat recipient stream HR2. The apparatus according to embodiment 96, wherein the apparatus further comprises a separation means S1 for separating the heat transfer material HTMS2a or HTMSa’, preferably an at least partially gaseous heat transfer material HTMS2a or HTMSa’ comprising the gaseous heat transfer material stream HTMS2b(g) and the liquid heat transfer material stream HTMS2(I), into separate streams of the gaseous heat transfer material stream HTMS2b(g) and the liquid heat transfer material stream HTMS2(I), wherein the separation means S1 comprises an inlet for a heat transfer material stream HTMS2a or HTMS2a’ and an outlet for a gaseous heat transfer material stream HTMS2b(g) and an outlet for a liquid heat transfer material stream HTMS2(I). The apparatus according to embodiment 97, wherein said apparatus does not comprise the evaporation means E1. The apparatus according to any one of embodiments 96 to 98 further comprising a fourth heat exchanger HE4 with an inlet for the heat transfer material stream HTMS4, the heat transfer material stream HTMS5 or a heat source stream HST and an outlet for a heat transfer material stream HTMS6 or a heat source stream HS2’ and an inlet for a second heat transfer material stream MS1 and an outlet for a second heat transfer material stream MS2.100. The apparatus according to any one of embodiments 96 to 99, wherein said apparatus does not comprise a third heat exchanger HE3.101 . The apparatus according to any of embodiments embodiments 96 to 100, wherein the evaporation means E1 in C) comprises one or more expanders (EP1 EPn).102. The apparatus according to embodiment 101 , wherein the one or more expanders (EP1 EPn) comprise a turbine, a throttle and / or a valve.103. The apparatus according to any of embodiments 96 to 102, wherein the one or more compressors in D) comprises at least two compressors (CP1 CPn).104. The apparatus according to embodiment 103, wherein the at least two compressors (CP1 CPn) comprise an inlet for the heat transfer material stream MS2 in-between each of the compressors.105. Use of the apparatus according to any of embodiments 96 to 104 for transferring heat from a heat source stream HS1 to a heat recipient stream HR1.106. A method, preferably according to any one of embodiments 1 to 95, comprising the step of converting the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method of any one of embodiments 1 to 95 to obtain a product Q.107. The method of embodiment 106, wherein the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder composi-tions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; orpolymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.108. The method of embodiment 106 or 107, wherein the content of the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method of any one of embodiments 1 to 95 in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight- % or more; and / or wherein the content of the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the process of any one of embodiments 1 to 95 in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.Description of figuresFigure 1 : shows a simplified depiction of an apparatus for transferring thermal energy from a heat source stream HS1 to a heat recipient stream HR1 , in particular comprising a first heat exchanger HE1 , an evaporations means E1 , one or more compressors (CP1 CPn), a second heat exchanger HE2, a third heat exchanger HE3 and a fourth heat exchanger HE4.Figure 2: shows a simplified scheme for transferring thermal energy from a heat from a heat source stream HS1 (“Quench water”) to a heat recipient stream in a heat recipient (“Reboiler PCC”), comprising a first heat exchanger HE1 (“Quench cooler”) for obtaining an at least partially gaseous heat transfer material stream HTMS2a (comprising a “vapor” and a “liquid”), a separation means S1 (“Separation of liquid and vapor”) for separating the vapor and the liquid obtained from HE1 , a compressor CP1 having 7 stages, and a second heat exchanger comprised in the heat recipient “Reboiler PCC” for obtaining a heated heat recipient stream and a heat transfer material stream HTMS4 (“Condensate”). The liquid obtained from the separation means S1 is partly recycled as the heat transfer material stream HTMS1 and partly added inbetween each compression stage in the compressor.Figure 3: shows a simplified scheme for transferring thermal energy from a heat from a heat source stream HS1 (“Quench water”) to a heat recipient stream in a heat recipient(“Reboiler PCC”) according to Figure 2, further comprising a third heat exchanger HE3 (“Condensate cooler”) located in-between and in flow communication with the first heat exchanger HE1 and the separation means S1 for obtaining an at least partially gaseous heat transfer material stream HTMS2a’, wherein the heat transfer material stream HTMS4 “Condensate” is fed to the third heat exchanger HE3 “Condensate cooler”.Cited literatureLinde & BASF, 2019, “Carbon capture, storage and utilisation”, page 05Prior Art Disclosure; Issue 684; paragraphs

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[8005] ; ISSN: 2198-4786; published: February 12, 2024Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005Database Cosing on the internet pages of the European Commission discloses cosmetic ingre-dients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC)- EP 2 587 005 A1- US 2007 / 017242 A1- DE 102 20870 A1- US 4 033 141 A- AT 522615 A1- US 2019 / 323704A1

Claims

Claims1 . A method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain a liquid heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii) Expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l); iii) Compressing the stream HTMS2b(g) to obtain a stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .

2. A method for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 , comprising the steps of: i’) Transferring heat from the heat source stream HS1 to a heat transfer material stream HTMS1 to obtain an at least partially gaseous heat transfer material stream HTMS2a having a higher thermal energy than the heat transfer material stream HTMS1 and a heat source stream HS2 having a lower thermal energy than the heat source stream HS1 ; ii') Optionally, expanding the stream HTMS2a, obtaining a gaseous stream HTMS2b(g) and a liquid stream HTMS2b(l); iii’) Compressing the stream HTMS2a from step i) or the stream HTMS2b(g) from step ii) to obtain a heat transfer material stream HTMS3 having a higher pressure than the stream HTMS2b(g); iv’) Transferring heat from the stream HTMS3 to a heat recipient stream HR1 obtaining a heat transfer material stream HTMS4 having a lower thermal energy than the stream HTMS3 and a heat recipient stream HR2 having a higher thermal energy than the stream HR1 .

3. The method according to claim 1 , comprising after step i) and prior to step ii) the additional steps of i.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain a liquid heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii).

4. The method according to claim 2, comprising after step i') and prior to step ii’) the additional steps of i'.a) Transferring heat from the stream HTMS4 to the stream HTMS2a to obtain an at least partially gaseous heat transfer material stream HTMS2a’ having a higher thermal energy than stream HTMS2a and a heat transfer material stream HTMS5 having a lower thermal energy than the stream HTMS4; wherein the stream HTMS2a’ is fed as HTMS2a into step ii’) or step iii’).

5. The method according to any of claims 1 to 4, comprising the additional steps of v) Separating prior to step i) or step i') at least part of the heat source stream HS1 , obtaining the additional heat source stream HST; vi) Transferring heat from the additional heat source stream HS1 ’ to a liquid heat transfer material stream MS1 , obtaining an additional heat source stream HS2’ having a lower thermal energy than the heat source stream HST and a liquid heat transfer material stream MS2 having a higher thermal energy than the liquid heat transfer material stream MS1 ; vii) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii’), step i.a) or step i'.a).

6. The method according to any of claims 1 to 4, comprising the additional steps of v’) Transferring heat from the stream HTMS4 after step iv) or step iv’) or HTMS5 to a liquid heat transfer material stream MS1 to obtain a heat transfer material stream HTMS6 having a reduced thermal energy than the stream HTMS4 or the stream HTMS5 and a liquid heat transfer material stream MS2 having a higher thermal energy than stream MS1 ; vi’) Feeding the stream MS2 to the stream HTMS2a prior to the heat transfer in step ii), step ii’), step i.a) or step i'.a).

7. The method according to any of claims 1 to 6, wherein the streams HTMS1 , HTMS2a, HTMS2a’, HTMS2b(g), HTMS2b(l), HTMS3, HTMS4, HTMS5, MS1 and MS2 are streams of a heat transfer material HTM1 .

8. The method according to any of claims 1 to 7, wherein the compression in step iii) or step iii’) comprises compressing the stream HTMS2a or HTMS2b(g) in at least two subsequent compression steps.

9. The method according to claim 8, wherein additional heat transfer material HTM 1 is added in-between each compression step.

10. The method according to claim 9, wherein at least part of the heat transfer material stream MS2 is used as the source for the heat transfer material HTM1 .11 . The method according to any of claims 1 to 10, wherein the liquid stream HTMS2b(l) is obtained, wherein the liquid stream HTMS2b(l) is recycled to step i) or step i') as at least part of the stream HTMS1 .

12. The method according to any of claims 1 to 11 , wherein the temperature of the stream HR2 is in the range of from >0.5 to <140 °C higher than the temperature of the stream HR1.

13. An apparatus for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 according to the method of any of claims 1 to 12, comprising:A) A first heat exchanger HE1 with an inlet for a heat source stream HS1 and an outlet for a heat source stream HS2, an inlet for a heat transfer material stream HTMS1 and an outlet for a heat transfer material HTMS2a;B) Optionally, a third heat exchanger HE3 with an inlet for the heat transfer material stream HTMS2a and an outlet for a heat transfer material stream HTMS2a’ and an inlet for a heat transfer material stream HTMS4 and an outlet for heat transfer material stream HTMS5;C) Optionally, an evaporation means E1 for at least partially evaporating the heat transfer material stream HTMS2a or HTMS2a’ with an inlet for a heat transfer material stream HTMS2a or HTMS2a’ and an outlet for a gaseous heat transfer material stream HTMS2b(g) and an outlet for a liquid heat transfer material stream HTMS2(I);D) One or more compressors (CP1 On) for compressing the heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a' , wherein each compressor comprises an inlet for heat transfer material stream HTMS2b(g), HTMS2a or HTMS2a’ from the heat exchanger HE1 or optionally from the heat exchanger HE3 or optionally from the evaporation means E1 or from the previous compressor and each with an outlet of heat transfer material stream HTMS3 to the next compressor or to the heat exchanger HE2;E) A second heat exchanger HE2 with an inlet for the heat transfer material stream HTMS3 and an outlet for the heat transfer material stream HTMS4 and an inlet for a heat recipient stream HR1 and an outlet for heat recipient stream HR2.

14. The apparatus according to claim 13 further comprising a fourth heat exchanger HE4 with an inlet for the heat transfer material stream HTMS4, the heat transfer material stream HTMS5 or a heat source stream HS1 ’ and an outlet for a heat transfer material stream HTMS6 or a heat source stream HS2’ and an inlet for a second heat transfer material stream MS1 and an outlet for a second heat transfer material stream MS2.

15. Use of the apparatus according to claim 13 or 14 for transferring heat from a heat source stream HS1 to a heat recipient stream HR1 .

16. A method, preferably according to any one of claims 1 to 12, comprising the step of converting the heat source stream HS2 and / or the heat recipient stream HR2 obtainable or obtained by the method of any one of claims 1 to 12 to obtain a product Q.

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