Method for the manufacture of a cracker product with low carbon footprint

Abstract

The present invention relates to a method for the manufacture of a cracker product with low carbon footprint. Furthermore, the present invention relates to a cracker product having a low carbon footprint. Yet further, the present invention relates to a process for the manufacture of a chemical compound or material from a cracker product with a low carbon footprint, and use of said cracker product for the production of a chemical compound or material.

Description

Method for the Manufacture of a Cracker Product with Low Carbon FootprintTECHNICAL FIELDThe present invention relates to a method for the manufacture of a cracker product with low carbon footprint. Furthermore, the present invention relates to a cracker product having a low carbon footprint. Yet further, the present invention relates to a process for the manufacture of a chemical compound or material from a cracker product with a low carbon footprint, and use of said cracker product for the production of a chemical compound or material.INTRODUCTIONThe thermal cracking of petroleum hydrocarbons, commonly referred to as pyrolysis or steam cracking, represents an important process in the petrochemical industry for the production of smaller, often unsaturated hydrocarbons, in particular of e.g. ethylene or propylene, from various sources of longer-chain hydrocarbon feedstock.The cracking process in a plant generally comprises one or more cracking furnaces operated at temperatures of 500 to 900 °C, a transfer line exchanger (TLE) and oil quench, a water quench and several further post processing steps depending on the hydrocarbon feedstock and the desired cracker product. The required temperature in the furnaces is typically provided by the combustion of a carbonaceous fuel. After cracking, the resulting gas is cooled in a TLE and an oil quench and a first fraction of high-boiling pyrolysis oils is separated. In a further quench, which is operated with water, the gas is cooled down further, often close to room temperature. To increase the efficiency of the overall process, the waste heat of the oil quench is mostly recycled in the cracking process for various applications such as generating process steam or the preheating of process components. In comparison, the waste heat of the water quench is usually largely consumed by a reboiler of a propene-propane fractionation tower. However, in certain process configurations where overhead gases are compressed and condensed in the reboiler of the propene-propane fractionation tower, which leads to an increase in condenser heat to a higher temperature level, no external heat is required for reboiling. Thus, in these scenarios, large amounts of the waste heat of the water quench remains unused. After the water quench, the gas is compressed and acid gases are removed, followed by fractional separation steps into the individual products. The separation steps comprise the separation of hydrogen and methane from the compressed gas, which make up a proportion of the carbonaceous fuel used to heat the cracker furnaces. However, the combustion of methane produces a flue gas containing carbon dioxide, which is usually cooled to 100 to 150 °C and ultimately released into the environment, resulting in considerable carbon dioxide emissions.As part of the decarbonisation of such a cracker process, various options may be considered to reduce the carbon dioxide emissions associated thereto, one of which is the installation of apost combustion carbon capture unit to strip carbon dioxide from the flue gas resulting from the combustion of the carbonaceous fuel. However, this type of emission control requires a large amount of thermal energy that is often linked with additional carbon dioxide emissions.Ullmann’s Encyclopedia of Industrial Chemistry, 2012, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim, 7thedition, volume 13: “Ethylene”, pages 469--515 relates to the industrial-scale production of ethylene, in particular to the pyrolysis of hydrocarbons, the quenching of hot cracked gas, and the recovery section of said production, wherein the cracking conditions and the heat requirements for the pyrolysis, the design of the cracker components, the processing steps of the cracked gas as well as implementations for utilizing waste heat and increasing energy efficiency are described in detail.US 2024 / 150260 A1 discloses a process for producing olefins, in particular ethylene, comprising the use of an annular jet vortex chamber reactor for converting fuel gas, hydrocarbons, an oxidant gas, and steam into a cracked gas. Further, said process involves a continuous regeneration CO2 removal unit for obtaining a CC>2-lean cracked gas, wherein said removal unit may comprise CO2 removal by amine absorption.Against this background, several approaches are known to reduce the carbon footprint of cracker products and increase the energy and heat efficiency of their production. Nevertheless, there is still a need to optimize cracking processes, in particular since thermal cracking accounts for the largest part of the carbon footprint of the resulting cracker product.DETAILED DESCRIPTIONThus, it was an object of the present invention to provide a method for the preparation of a cracker product having reduced carbon dioxide emissions.Surprisingly, it was found that thermal energy from a cracking process can be transferred to a post treatment system that reduces carbon dioxide emissions produced by combusting a carbonaceous fuel to heat cracking furnaces of said cracking process. In particular, it was surprisingly found that a heated stream of heated water from a water quench of a cracking process can be transferred to a regeneration step of a post combustion capture process that can remove carbon dioxide from a fluid stream from the combustion of a carbonaceous fuel, thereby utilizing waste heat from the water quench and decreasing the carbon dioxide emissions from the post combustion capture unit. Further, it has surprisingly been found that said method can be used for the preparation of a cracker product having a reduced carbon footprint. Yet further, it was surprisingly found that by provision of said cracker product chemical compounds and materials can be manufactured that benefit from the reduced carbon dioxide emissions in the initial cracking process.Therefore, the present invention relates to a method for the manufacture of a cracker product selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines, aromatic compounds, and mixtures of two or more thereof, from a hydrocarbon feedstock, said method comprising the steps of:(1) cracking a hydrocarbon feedstock to obtain a cracked gas comprising ethylene, wherein cracking is effected in one or more crackers, wherein at least one of the crackers is, at least partially, directly or indirectly heated by combusting a carbonaceous fuel, and wherein the combustion of the carbonaceous fuel generates a carbon dioxide comprising flue gas stream FS1 ;(2.1) quenching at least a fraction of the cracked gas by contacting at least the fraction of cracked gas with water to obtain a stream HS1 of heated water, and a stream of cooled cracked gas;(2.2) subjecting the carbon dioxide comprising flue gas stream FS1 generated in step (1) to a carbon capture process comprising:(2.2. a) an absorption step in which flue gas stream FS1 is contacted with an absorbentA1 in an absorber unit to obtain an absorbent A2 laden with carbon dioxide and a flue gas stream FS2 from which carbon dioxide has been at least partly removed;(2.2. b) a regeneration step in which at least a portion of the laden absorbent A2 obtained from step b) is heated in a regenerator unit to obtain an at least partly regenerated absorbent A3 and a gaseous stream GS comprising carbon dioxide;(2.2.c) a recycling step in which at least a fraction of the regenerated absorbent A3 from step b) is recycled as absorbent A1 into the absorption step (2.2. a); wherein thermal energy is transferred from HS1 obtained in step (2.1) to the regeneration step (2.2. b).It is preferred that the cracking of the hydrocarbon feedstock in step (1) comprises catalytic cracking or steam cracking, preferably steam cracking.It is preferred that the hydrocarbon feedstock is selected from the group consisting of C2-C4-al- kanes, naphtha, gas oil and hydrocracker residues.It is preferred that at least one of the crackers is indirectly heated by combusting a carbonaceous fuel, wherein more preferably the one or more crackers are indirectly heated by combusting a carbonaceous fuel.It is preferred that wherein the one or more crackers in step (1) comprise a convection section, a fired tubular reactor and a transfer-line exchanger.It is preferred that the fired tubular reactor is located downstream of the convection section.It is preferred that the transfer-line exchanger is located downstream of the fired tubular reactor.In the case where the one or more crackers comprise a convection section, it is preferred that the hydrocarbon feedstock mixed with steam is heated in the convection section of the cracker furnace by heat exchange against flue gas to a temperature in the range from 400 to 800 °C, more preferably in the range from 500 to 680 °C, more preferably in the range from 550 to 630 °C.In the case where the one or more crackers comprise a fired tubular reactor, it is preferred that the hydrocarbon feedstock in the fired tubular reactor of the cracker is heated to a temperature in the range from 600 to 1000 °C, more preferably from 750 to 900 °C, more preferably from 800 to 875 °C over a time span of 0.05 to 2.0s, preferably of 0.1 to 1 .0 s, more preferably of 0.1 to 0.5 s.Further in the case where the one or more crackers comprise a fired tubular reactor, it is preferred that the hydrocarbon feedstock in the fired tubular reactor of the cracker is cracked to obtain cracked gas.In the case where the one or more crackers comprise a transfer-line exchanger, it is preferred that the cracked gas in the transfer-line exchanger of the cracker is cooled to temperatures of 700 °C or less, more preferably from 550 to 650 °C, more preferably from 575 to 625 °C over a time span of 0.01 to 0.2 s, preferably of 0.02 to 0.1 s, more preferably of 0.04 to 0.07 s.Further in the case where the one or more crackers comprise a transfer-line exchanger, it is preferred that the cooling of the cracked gas is carried out by vaporization of high-pressure boiler feed water having a pressure in the range from 4 to 15 MPa, preferably in the range from 6 to 12 MPa, more preferably in the range from 8 to 10 MPa.It is preferred that the method for the manufacture of a cracker product further comprises one or more steps to separate the cracker products from the cracked gas obtained in step (2.1 ) selected from the group consisting of an acid gas removal step, a hydrogen removal step, a me- thane-removal step, an ethane removal step, a propane-removal step, a C4-fractionation step, a hydrogenation step where acetylene comprised in the cracked gas is hydrogenated to ethylene, an ethylene-removal step, a propylene-removal step, a C4-olefine fractionation step, and a step for the separation of aromatic cracker products.It is preferred that the alkene cracker products are selected from the group consisting of ethene, propene, butenes, pentenes, hexenes, heptenes, octenes, dodecenes, 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-me- thyl-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-trimethylpen- tene; wherein more preferably dodecenes are selected from any trimers formed from C4-al- kenes.It is preferred that the alkine cracker products are selected from the group consisting of ethine, propine, butines, and mixtures of two or more thereof, wherein more preferably butines are selected from 1-butine and 2-butine.It is preferred that the aromatic compound cracker products are selected from the group consisting of benzenes, more preferably ethylbenzene, benzene, toluene, styrene and xylene.It is preferred that the heat source stream HS1 has a temperature in the range of 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.It is preferred that the heat source stream HS1 has a flow rate in the range of from 500 to 5000 t / h, more preferably in the range of from 1000 to 4000 t / hr, more preferably in the range of from 1500 to 3500 t / hr, more preferably in the range of from 1800 to 3000 t / hr, more preferably in the range of from 2200 to 2600 t / hr.It is preferred that the flue gas stream FS1 after step (1) and prior to step (2.2) has a temperature in the range of from 20 to 800 °C, more preferably in the range of from 30 to 600 °C, more preferably in the range of from 30 to 450 °C, more preferably in the range of from 300 to 380 °C.It is preferred that the absorbent A1 has a temperature in the range of from 25 to 65 °C, more preferably in the range of from 28 to 57 °C, more preferably in the range of from 30 to 50 °C.It is preferred that the absorbent A2 has a temperature in the range of from 30 to 70 °C, more preferably in the range of from 33 to 65 °C, more preferably in the range of from 35 to 60 °C.It is preferred that the absorbent A3 has a temperature in the range of from 25 to 140 °C, more preferably in the range of from 50 to 135 °C, more preferably in the range of from 80 to 130 °C, more preferably in the range of from 115 to 125 °C.It is preferred that the gaseous stream GS has a temperature in the range of from 20 to 120 °C, more preferably in the range of from 30 to 100 °C, more preferably in the range of from 35 to 90 °C,It is preferred that after step (2.1 ) and prior to the carbon capture process step (2.2) the method further comprises(2.1 ’.a) feeding the stream FS1 to a means for removing nitrogen oxides, obtaining a flue gas stream FS1 dn comprising a lower amount of nitrogen oxides compared to FS1 ;(2.1 ’.b) feeding the stream FS1 dn as FS1 to the absorption step (2.2. a).It is preferred that after step (2.1 ) or step (2.1 ’.a) and prior to the carbon capture process step (2.2) the method further comprises(2.1 ”. a) feeding the flue gas stream FS1 or the flue gas stream FS1 dn obtained in (2.1 ’.a) to a cooling unit, obtaining a cooled flue gas stream FS1 c having a reduced thermal energy compared to FS1 or FS1 dn;(2.1 ”.b) feeding the stream FS1c as FS1 to the absorption step (2.2. a).In the case where the method further comprises the steps (2.1 ”. a) and (2.1 ”.b), it is preferred that the cooling unit in (2.1 ”. a) comprises a direct contact-cooler.In the case where the cooling unit comprises a direct contact-cooler, it is preferred that the direct contact cooler comprises a basic aqueous solution.Further in the case where the cooling unit comprises a direct contact-cooler, it is preferred that the direct contact cooler comprises a basic aqueous NaOH solution for removing sulfur dioxide from FS1 or FS1 dn.Further in the case where the method further comprises the steps (2.1 ”. a) and (2.1 ”.b), it is preferred that the flue gas stream FS1 c has a temperature in the range of from 20 to 80 °C, more preferably in the range of from 30 to 65 °C, more preferably in the range of from 35 to 60 °C.It is preferred that the absorbents A1 , A2 and A3 comprise a basic absorber solution, preferably an aqueous basic amine absorber solution.In the case where the absorbents A1 , A2 and A3 comprise an aqueous basic amine absorber solution, it is preferred that the basic amine absorber solution is selected from the group consisting of amines of the formula (I): NR1(R2)2, amines of the formula (II): R3R4N-X-NR5R6, 5- to 7-membered saturated heterocycles having one or more nitrogen atoms incorporated in thering, and mixtures of two or more thereof, wherein more preferably R1is selected from C2-C6-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-al- kyl groups, hydroxy-Ci-C6-alkoxy-C2-C6-alkyl groups and 1-piperazinyl-C2-C6-alkyl groups; wherein more preferably R2is selected from H, Ci-Ce-alkyl groups and C2-Ce-hydroxyalkyl groups; wherein more preferably R3, R4, R5and R6are independently selected from H, Ci-C6-alkyl groups, C2-Ce-hydroxyalkyl groups, Ci-C6-alkoxy-C2-C6-alkyl groups and C2-Ce-aminoalkyl groups; wherein more preferably X is a C2-Ce-alkylene group, -X1-NR7-X2- or -X1-O-X2; wherein more preferably X1and X2are independently selected from C2-Ce-alkylene groups; wherein more preferably R7is selected from H, Ci-Ce-alkyl groups, C2-Ce-hydroxyalkyl groups or C2-Ce-aminoalkyl groups; wherein more preferably the 5- to 7-membered saturated heterocyles further comprise one or two heteroatoms selected from nitrogen and oxygen incorporated in the ring.It is preferred that the absorber unit in the absorption step (2.2. a) comprises an absorber column.In the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an inlet for the flue gas stream FS1 at the bottom of the column.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an inlet for the absorbent A1 in the upper section of the column.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises absorption beds.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an interstage cooler optionally driven by a pump, and more preferably not driven by a pump.Further in the case where the absorber unit comprises an absorber column, it is preferred that the interstage cooler is installed between the absorption beds.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column is operated in a counter-current flow, and wherein FS1 is contacted with A1.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an outlet of the absorbent A2 at the bottom of the column.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an outlet of the flue gas stream FS2 at the head of the column.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises an emission control system in the upper section of the column.Further in the case where the absorber unit comprises an absorber column, it is preferred that the absorber column comprises a washing section at the head of the column.In the case where the absorber column comprises a washing section, it is preferred that the washing section comprises an inlet for make-up water.It is preferred that the regenerator unit in the regeneration step (2.2. b) comprises a desorber column.In the case where the regenerator unit comprises a desorber column, it is preferred that thermal energy is transferred from HS1 obtained in step (2.1) to a reboiler stream RS1 originating from a reboiler unit of the regenerator unit to obtain a reboiler stream RS2 having a higher thermal energy than RS1 .Further in the case where the regenerator unit comprises a desorber column, it is preferred that thermal energy is transferred from the reboiler stream RS2 to the absorbent A2 in the desorber column.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the desorber column comprises an inlet of the absorbent A2 in the upper section of the column.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the desorber column comprises an inlet of the reboiler stream RS2 at the lower section of the column.In the case where the desorber column comprises an an inlet of the reboiler stream RS2 at the lower section of the column, it is preferred that the reboiler stream RS2 comprises steam.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the desorber column is operated in a counter-current flow, and wherein RS2 is contacted with A2.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the desorber column comprises an outlet of the absorbent A3 at the bottom of the column.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the desorber column comprises an outlet of the gaseous stream GS at the head of the column.Further in the case where the regenerator unit comprises 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 A3 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 column, it is preferred that the desorber column comprises a further heat exchanger, wherein heat is exchanged from the absorbent A3 downstream of the additional heat exchanger to the absorbent A2 upstream of the first of the two regeneration columns.Further in the case where the regenerator unit comprises a desorber column, it is preferred that the absorbent A2 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 transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2. b) comprises one or more open loop and / or closed loop heat pumps.In the case where the transfer of thermal energy comprises one or more open loop and / or closed loop heat pumps, it is preferred that independently from one another, the one or more open loop and / or closed loop heat pumps comprise a heat transfer material selected from the group of water, ammonia, carbon dioxide, n-propane, n-butane, isobutene, n-pentane, trans-1- chloro-3,3,3-trifluoropropene, 1 ,1 ,1 ,3,3-pentafluoropropane, 1 ,1 ,1 ,2-tetrafluoroethane, (1 E)- 1 ,3,3,3-tetrafluoroprop-1-ene, (1 Z)-1 ,3,3,3-tetrafluoroprop-1-ene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-bu- tene or mixtures of two or more thereof. Suitable heat transfer materials are known to the skilled person and are disclosed, for example, in C. Arpagaus et al. (C. Arpagaus et aL, Energy 152 (2018), pages 985 to 1010).As a first alternative, it is preferred that the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2. b) comprises a closed loop heat pump CHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn), a second heat exchanger HE2 and an expander E1 , wherein the transfer of thermal energy comprises the steps of: i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM 1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfermedium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfer medium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1 ; iv) expanding the heat transfer medium stream HTMS4 to obtain a heat transfer medium stream HTMS5 having a lower pressure than the heat transfer medium stream HTMS4 and recycling the heat transfer medium stream HTMS5 as the heat transfer medium stream HTMS1 to step i).In the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that the expansion step iv) is performed under adiabatic conditions.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that the expander E1 comprises a turbine, a throttle or a valve.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that HTM1 comprises water, ammonia, carbon dioxide, n-propane, n-bu- tane, 1 ,1 ,1 ,2-tetrafluoroethane, trans-1-chloro-3,3,3-trifluoropropene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor- 2-butene, or mixtures of two or more thereof, more preferably ammonia.In the case where HTM 1 of the closed loop heat pump CHP1 comprises ammonia, it is preferred that the stream HTMS1 has a pressure in the range of from 15 bara to 30 bara, more preferably in the range of from 18 bara to 25 bara, more preferably in the range of from 20 to 24 bara.Further in the case where HTM1 of the closed loop heat pump CHP1 comprises ammonia, it is preferred that the stream HTMS3 has a pressure in the range of from 20 to 100 bara, more preferably in the range of from 50 to 90 bara, more preferably in the range of from 70 to 80 bara.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that the stream HTMS5 has a temperature in the range of from 20 to 115 °C, preferably in the range of from 30 to 100 °C, more preferably in the range of from 40 to 80 °C, more preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that the stream HTMS5 has the same temperature as HTMS1 .Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 , it is preferred that the stream HTMS5 has the same pressure as HTMS1 .As a second alternative, it is preferred that the transfer of thermal energy from HS1 obtained in step (2.1) to the regeneration step (2.2.b) comprises an open loop heat pump OHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn) and a second heat exchanger HE2, wherein the transfer of thermal energy comprises the steps of: i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfer medium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1.Further in the case where the transfer of thermal energy comprises an open loop heat pump OHP1 , it is preferred that HTM1 comprises water, ammonia, carbon dioxide, n-propane, n-bu- tane, trans-1-chloro-3,3,3-trifluoropropene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-butene, or mixtures of two or more thereof, more preferably water.In the case where HTM1 of the open loop heat pump OHP1 comprises water, it is preferred that the stream HTMS1 has a pressure in the range of from 0.05 bara to 2.0 bara, preferably in the range of from 0.1 bara to 1 bara, more preferably in the range of from 0.15 to 0.25 bara.Further in the case where HTM1 of the open loop heat pump OHP1 comprises water, it is preferred that the stream HTMS3 has a pressure in the range of from 2.00 to 5.00 bara, more preferably in the range of from 3.00 to 3.80 bara, more preferably in the range of from 3.35 to 3.45 bara.In the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the respective compression step is performed under adiabatic conditions.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the respective compression step is performed in at least two compressors (CP1 CPn) connected in series.In the case where the respective compression step is performed in at least two compressors (CP1 CPn), it is preferred that in-between each of the at least two compressors (CP1 CPn) a stream of the heat transfer material HTM 1 is added.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the heat source stream HS2 has a temperature in the range of from 40 to 120 °C, more preferably in the range of from 45 to 105 °C, more preferably in the range of from 50 to 90 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS1 has a temperature in the range of from 20 to 115 °C, more preferably in the range of from 30 to 100 °C, more preferably in the range of from 40 to 80 °C, more preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS1 has a pressure equal to the vapour pressure of HTM1 at the temperature of HTMS1 .Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS2 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 transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the temperature of the stream HTMS2 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.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS2 has the same pressure as the stream HTMS1 .Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS3 has a temperature in the range of from 80 to 200 °C, more preferably in the range of from 90 to 190 °C, more preferably in the range of from 120 to 160 °C, more preferably in the range of from 140 to 150 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS3 has a pressure equal to the vapour pressure of HTM1 at the temperature of HTMS3.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS4 has a temperature in the range of from 75 to 195 °C, more preferably in the range of from 90 to 180 °C, more preferably in the range of from 115 to 150 °C, more preferably in the range of from 135 to 145 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HTMS4 has the same pressure as the stream HTMS3.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HRS1 has a temperature in the range of from 105 to 160 °C, preferably in the range of from 110 to 135 °C, more preferably in the range of from 115 to 125 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HRS1 has a pressure in the range of from 1.1 to 5 bara, more preferably in the range of from 1 .3 to 3 bara, more preferably in the range of 1 .5 to 2.5 bara.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HRS2 has a temperature in the range of from 106 to 165 °C, more preferably in the range of from 111 to 138 °C, more preferably in the range of from 116 to 130 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the temperature of the stream HRS2 is in the range of from >0.5 to <10 °C higher than the temperature of the stream HRS1 , more preferably in the range of from >0.75 to <7.0 °C, more preferably in the range of from >1.0 to <5.0 °C.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the stream HRS2 has the same pressure as the stream HRS1 .In the case where the transfer of thermal energy comprises an open loop heat pump OHP1 , it is preferred that the open loop heat pump OHP1 further comprises a third heat exchanger HE3 located downstream of the second heat exchanger HE2, wherein the transfer of thermal energycomprises the additional steps of iv) transferring thermal energy from the heat transfer medium stream HTMS4 to the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS5’ having a reduced thermal energy compared to the heat transfer medium stream HTMS4 and a heat transfer medium stream HTMS2’ having an increased thermal energy compared to the heat transfer medium stream HTMS2; v) feeding the heat transfer medium stream HTMS2’ as the heat transfer medium stream HTMS2 in step ii).In the case where the open loop heat pump OHP1 further comprises a third heat exchanger HE3, it is preferred that the stream HTMS2’ 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 open loop heat pump OHP1 further comprises a third heat exchanger HE3, it is preferred that the stream HTMS2’ has the same pressure as the stream HTMS2.Further in the case where the open loop heat pump OHP1 further comprises a third heat exchanger HE3, it is preferred that 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 open loop heat pump OHP1 further comprises a third heat exchanger HE3, 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 HTMS2, more preferably in the range of from >1.0 to <15 °C, more preferably in the range of from >2.0 to <10 °C.Further in the case where the open loop heat pump OHP1 further comprises a third heat exchanger, it is preferred that the stream HTMS5’ has the same pressure as the stream HTMS4.Further in the case where the open loop heat pump OHP1 further comprises a third heat exchanger, it is preferred that the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4 located downstream of the third heat exchanger HE3, wherein the transfer of thermal energy comprises the additional steps of vi) transferring thermal energy from the heat transfer medium stream HTMS5’ to a heat transfer material stream MS1 of heat transfer material HTM1 to obtain a heat transfer material stream MS2 having an increased thermal energy compared to the material stream MS1 and a heat transfer medium stream HTMS6 having a reduced thermal energy compared to the heat transfer medium stream HTMS5’;vii) feeding the material stream MS2 into the heat transfer medium stream HTMS2 prior to its compression in step ii).In the case where the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, it is preferred that at least two compressors (CP1 CPn) are used, wherein at least part of the material stream MS2 is added in-between each of the at least two compressors in the compression step ii).Further in the case where the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, 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 open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, 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 open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, 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 open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, it is preferred that the stream MS2 has the same pressure as MS1 .Further in the case where the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, 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 open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, 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.Further in the case where the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4, it is preferred that the stream HTMS6 has the same pressure as HTMS5’.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the heat transfer medium stream HTMS2 or HTMS2’ is a liquid heat transfer material stream IHTMS2a, wherein the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn) located downstream of the first heat exchanger HE1 or optionally downstream of the third heat exchanger HE3 and upstream of the one or more compressors (CP1 CPn), wherein the transfer of thermal energy comprises the additional steps of1.1) expanding the liquid heat transfer medium stream IHTMS2a to obtain a heat transfer medium stream HTMS2b having a lower pressure than the heat transfer material stream IHTMS2a comprising a gaseous and a liquid phase;1.2) separating the gaseous phase from the heat transfer medium stream HTMS2b to obtain a gaseous heat transfer medium stream gHTMS2b and a liquid heat transfer medium stream IHTMS2b;1.3) feeding the gaseous heat transfer medium stream gHTMS2b as the heat transfer medium stream HTMS2 in step ii);1.4) optionally recycling the liquid heat transfer medium stream IHTMS2b as the heat transfer medium stream HTMS1 in step i).In the case where the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn), it is preferred that the expansion step i.1) is performed under adiabatic conditions.Further in the case where the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn), it is preferred that the one or more expanders (EP1 EPn) comprise a turbine, a throttle, a valve or a mixture thereof.In the case where the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn), it is preferred that wherein the respective expansion step is performed in at least two expanders (EP1 EPn) connected in series.In the case where the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn), it is preferred that the stream gHTMS2b has a temperature in the range of from 40 to 100 °C, more preferably in the range of from 50 to 80 °C, more preferably in the range of from 55 to 65 °C.In the case where the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn), it is preferred that the stream IHTMS2b has the same temperature as the stream gHTMS2b.Further in the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 and / or an open loop heat pump OHP1 , it is preferred that the heat exchanger HE2 is comprised in the regenerator unit of the regeneration step (2.2. b).In the case where the heat exchanger HE2 is comprised in the regenerator unit, it is particularly preferred that the heat exchanger HE2 is comprised in the reboiler unit of the regenerator unit.In the case where the heat exchanger HE2 is comprised in the reboiler unit of the regenerator unit, it is particularly preferred that the reboiler stream RS1 is the heat recipient stream HRS1 and the reboiler stream RS2 is the heat recipient stream HRS2.Further in the case where the transfer of thermal energy comprises one or more open loop and / or closed loop heat pumps, it is preferred that the transfer of thermal energy from the heated stream HS1 obtained in step (2.1) to the regeneration step (2.2. b) comprises at least two closed loop and / or open loop heat pumps, which are connected in series.In the case where the transfer of thermal energy comprises at least two open loop and / or closed loop heat pumps, it is preferred that the heat transfer medium stream HTMS1 of the respective heat pump is the heat recipient stream HRS1 of the previous heat pump and the heat transfer medium stream HTMS2 of the respective heat pump is the heat recipient stream HRS2 of the previous heat pump.Further in the case where the transfer of thermal energy comprises at least two open loop and / or closed loop heat pumps, it is preferred that the last heat pump of the series is an open loop heat pump OH P1 , wherein the heat transfer medium stream HTMS4 of the last heat pump is fed to a heat exchanger to transfer heat to the heat transfer medium stream HTMS2 of the first heat pump of the series.Further in the case where the transfer of thermal energy comprises at least two open loop and / or closed loop heat pumps, it is preferred that the heat exchanger HE2 of the last heat pump of the series is comprised in the regenerator unit of the regeneration step (2.2.b).In the case where the heat exchanger HE2 of the last heat pump of the series is comprised in the regenerator unit, it is particularly preferred that the heat exchanger HE2 of the last heat pump of the series is comprised in the reboiler unit of the regenerator unit.It is preferred that the regenerator unit has a coefficient of performance (COP) of >1.5, preferably of >2, more preferably in the range of from 2 to 4, more preferably in the range of from 2.5 to 3.8.Further in the case where the transfer of thermal energy comprises at least two open loop and / or closed loop heat pumps, it is preferred that the heat transfer materials HTM1 comprised independently from one another in each of the at least two heat pumps comprise the same heat transfer material and / or different heat transfer materials.Further in the case where the transfer of thermal energy comprises at least two open loop and / or closed loop heat pumps, it is preferred that the transfer of thermal energy comprises a closed loop heat pump CHP1 as a first heat pump and an open loop heat pump OHP1 as a second heat pump connected in series.In the case where the transfer of thermal energy comprises a closed loop heat pump CHP1 as a first heat pump and an open loop heat pump OHP1 as a second heat pump connected in series, it is particularly preferred that HTM1 of the closed loop heat pump CHP1 is ammonia and HTM 1 of the open loop heat pump OHP1 is water.It is preferred that the carbonaceous fuel comprises alkanes, more preferably methane, and ethane.The method according to any of embodiments 1 to 120 wherein the stream of the cooled cracked gas obtained in (2.1) is subjected to one or more post processing steps.In the case where the cooled cracked gas is subjected to one or more post processing steps, it is preferred that the one or more post processing steps comprises a step for separating methane from the stream of the cooled cracked gas.In the case where the one or more post processing steps comprises a step for separating methane, it is particularly preferred that the separated methane constitutes at least a part of the carbonaceous fuel used to heat at least one of the one or more crackers.Further in the case where the cooled cracked gas is subjected to one or more post processing steps, it is preferred that the one or more post processing steps further comprises a step for separating ethylene from the stream of the cooled cracked gas.In the case where the one or more post processing steps further comprises a step for separating ethylene, it is particularly preferred that the separated ethylene is further subjected to one or more chemical conversion steps.Further, the present invention relates to a cracker product obtained or obtainable by the method according to any one of the embodiments disclosed herein having a lower carbon footprint.Yet further, the present invention relates to a process for the manufacture of one or more chemical compounds or materials comprising:(A) providing a cracker product obtained or obtainable by the method according to any one of the embodiments disclosed herein;(B) subjecting the cracker product provided in step (A) to one or more chemical conversion reactions, obtaining one or more chemical compounds or materials.Yet further, the present invention relates to the use of a cracker product obtained or obtainable by the method according to any one of the embodiments disclosed herein for the production of a chemical compound or material.Within the meaning of the present invention, the term “expander” preferably designates any means for reducing the pressure of a stream, more preferably any component used as a means for reducing the pressure of a stream, and more preferably any component used as a means for reducing the pressure of a stream passed through said component.”The present invention further relates to a process as described above, preferably the method comprising (1) to (2.2.c) as described above, wherein said process (further) comprises the step of converting the stream of the cooled cracked gas obtainable or obtained by the process described herein, or a chemical material obtainable or obtained by the process 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 composition; 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 stream of the cooled cracked gas 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 stream of the cooled cracked gas 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 preferably 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 process described herein is further a process 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 higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. 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 at-oms. 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 rheology, 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 usesolvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic 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 Reference 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 Reference 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 Grubemann, 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 ingredientsand / 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 context 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 combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including 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 ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic 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 / polyvinylpyrrolidone-co- polymer. 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 herein, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising 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 detail 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, comprises 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 polyurethane 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 compositions” of Reference RF1. The converting step(s) to obtain the hyperbranched polyester polyols 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 two component 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 Reference 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 Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Perstonal Care Products Council (PCPC), discloses cosmetic ingredients. The term “composition and / or formulation thereof’ with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal 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”, ‘Toil”, “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 the manufacture of a cracker product selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines, aromatic compounds, and mixtures of two or more thereof, from a hydrocarbon feedstock, said method comprising the steps of:(1 ) cracking a hydrocarbon feedstock to obtain a cracked gas comprising ethylene, wherein cracking is effected in one or more crackers, wherein at least one of the crackers is, at least partially, directly or indirectly heated by combusting a carbonaceous fuel, and wherein the combustion of the carbonaceous fuel generates a carbon dioxide comprising flue gas stream FS1 ;(2.1 ) quenching at least a fraction of the cracked gas by contacting at least the fraction of cracked gas with water to obtain a stream HS1 of heated water, and a stream of cooled cracked gas;(2.2) subjecting the carbon dioxide comprising flue gas stream FS1 generated in step (1) to a carbon capture process comprising:(2.2. a) an absorption step in which flue gas stream FS1 is contacted with an absorbent A1 in an absorber unit to obtain an absorbent A2 laden with carbon dioxide and a flue gas stream FS2 from which carbon dioxide has been at least partly removed;(2.2. b) a regeneration step in which at least a portion of the laden absorbent A2 obtained from step b) is heated in a regenerator unit to obtain an at least partly regenerated absorbent A3 and a gaseous stream GS comprising carbon dioxide;(2.2.c) a recycling step in which at least a fraction of the regenerated absorbent A3 from step b) is recycled as absorbent A1 into the absorption step (2.2. a); wherein thermal energy is transferred from HS1 obtained in step (2.1 ) to the regeneration step (2.2. b).2. The method according to embodiment 1 , wherein the cracking of the hydrocarbon feedstock in step (1) comprises catalytic cracking or steam cracking, preferably steam cracking.3. The method according to embodiment 1 or 2, wherein the hydrocarbon feedstock is selected from the group consisting of C2-C4-alkanes, naphtha, gas oil and hydrocracker residues.4. The method according to any one of embodiments 1 to 3, wherein at least one of the crackers is indirectly heated by combusting a carbonaceous fuel, wherein preferably the one or more crackers are indirectly heated by combusting a carbonaceous fuel.5. The method according to any of embodiments 1 to 4, wherein the one or more crackers in step (1) comprise a convection section, a fired tubular reactor and a transfer-line exchanger.6. The method according to embodiment 5, wherein the fired tubular reactor is located downstream of the convection section.7. The method according to embodiment 5 or 6, wherein the transfer-line exchanger is located downstream of the fired tubular reactor.8. The method according to any of embodiments 5 to 7, wherein the hydrocarbon feedstock mixed with steam is heated in the convection section of the cracker furnace by heat exchange against flue gas to a temperature in the range from 400 to 800 °C, preferably in the range from 500 to 680 °C, more preferably in the range from 550 to 630 °C.9. The method according to any of embodiments 5 to 8, wherein the hydrocarbon feedstock in the fired tubular reactor of the cracker is heated to a temperature in the range from 600 to 1000 °C, preferably from 750 to 900 °C, more preferably from 800 to 875 °C over a time span of 0.05 to 2.0s, preferably of 0.1 to 1 .0 s, more preferably of 0.1 to 0.5 s.10. The method according to embodiment 9, wherein the hydrocarbon feedstock in the fired tubular reactor of the cracker is cracked to obtain cracked gas.11 . The method according to any of embodiments 5 to 10, wherein the cracked gas in the transfer-line exchanger of the cracker is cooled to temperatures of 700 °C or less, preferably from 550 to 650 °C, more preferably from 575 to 625 °C over a time span of 0.01 to 0.2 s, preferably of 0.02 to 0.1 s, more preferably of 0.04 to 0.07 s.12. The method according to embodiment 11 , wherein the cooling of the cracked gas is carried out by vaporization of high-pressure boiler feed water having a pressure in the range from 4 to 15 MPa, preferably in the range from 6 to 12 MPa, more preferably in the range from 8 to 10 MPa.13. The method according to any of embodiments 1 to 12, further comprising one or more steps to separate the cracker products from the cracked gas obtained in step (2.1 ) selected from the group consisting of an acid gas removal step, a hydrogen removal step, a methane-removal step, an ethane removal step, a propane-removal step, a C4-fractiona- tion step, a hydrogenation step where acetylene comprised in the cracked gas is hydrogenated to ethylene, an ethylene-removal step, a propylene-removal step, a C4-olefine fractionation step, and a step for the separation of aromatic cracker products.14. The method according to any of embodiments 1 to 13, wherein the alkene cracker products are selected from the group consisting of ethene, propene, butenes, pentenes, hexenes, heptenes, octenes, dodecenes, 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-pen- tene, 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 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-octene, isooctenes, dimethylhexenes, methylheptenes 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. The method according to any of embodiments 1 to 14, wherein the alkine cracker products are selected from the group consisting of ethine, propine, butines, and mixtures of two or more thereof, wherein preferably butines are selected from 1-butine and 2-butine. The method according to any of embodiments 1 to 15, wherein the aromatic compound cracker products are selected from the group consisting of benzenes, preferably ethylbenzene, benzene, toluene, styrene and xylene. The method according to any of embodiments 1 to 16, wherein the heat source stream HS1 has a temperature in the range of 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. The method according to any of embodiments 1 to 17, wherein the heat source stream HS1 has a flow rate in the range of from 500 to 5000 t / h, preferably in the range of from 1000 to 4000 t / hr, more preferably in the range of from 1500 to 3500 t / hr, more preferably in the range of from 1800 to 3000 t / hr, more preferably in the range of from 2200 to 2600 t / hr. The method according to any of embodiments 1 to 18, wherein the flue gas stream FS1 after step (1 ) and prior to step (2.2) has a temperature in the range of from 20 to 800 °C, preferably in the range of from 30 to 600 °C, more preferably in the range of from 30 to 450 °C, more preferably in the range of from 30 to 380 °C. The method according to any of embodiments 1 to 19, wherein the absorbent A1 has a temperature in the range of from 25 to 65 °C, preferably in the range of from 28 to 57 °C, more preferably in the range of from 30 to 50 °C. The method according to any of embodiments 1 to 20, wherein the absorbent A2 has a temperature in the range of from 30 to 70 °C, preferably in the range of from 33 to 65 °C, more preferably in the range of from 35 to 60 °C.22. The method according to any of embodiments 1 to 21 , wherein the absorbent A3 has a temperature in the range of from 25 to 140 °C, preferably in the range of from 50 to 135 °C, more preferably in the range of from 80 to 130 °C, more preferably in the range of from 115 to 125 °C.23. The method according to any of embodiments 1 to 22, wherein the gaseous stream GS has a temperature in the range of from 20 to 120 °C, preferably in the range of from 30 to 100 °C, more preferably in the range of from 35 to 90 °C,24. The method according to any of embodiments 1 to 23, wherein after step (2.1) and prior to the carbon capture process step (2.2) the method further comprises(2.1’.a) feeding the stream FS1 to a means for removing nitrogen oxides, obtaining a flue gas stream FS1dn comprising a lower amount of nitrogen oxides compared to FS1 ; (2.1’.b) feeding the stream FS1dn as FS1 to the absorption step (2.2. a).25. The method according to any of embodiments 1 to 24, wherein after step (2.1 ) or step (2.1’.a) and prior to the carbon capture process step (2.2) the method further comprises (2.1 ”. a) feeding the flue gas stream FS1 or the flue gas stream FS1dn obtained in (2.T. a) to a cooling unit, obtaining a cooled flue gas stream FS1c having a reduced thermal energy compared to FS1 or FS1dn;(2.1 ”.b) feeding the stream FS1c as FS1 to the absorption step (2.2. a).26. The method according to embodiment 25, wherein the cooling unit in (2.1 ”. a) comprises a direct contact-cooler.27. The method according to embodiment 26, wherein the direct contact cooler comprises a basic aqueous solution.28. The method of embodiments 26 or 27, wherein the direct contact cooler comprises a basic aqueous NaOH solution for removing sulfur dioxide from FS1 or FS1dn.29. The method according to any of embodiments 25 to 28, wherein the flue gas stream FS1 c has a temperature in the range of from 20 to 80 °C, preferably in the range of from 30 to 65 °C, more preferably in the range of from 35 to 60 °C.30. The method according to any of embodiments 1 to 29, wherein the absorbents A1 , A2 and A3 comprise a basic absorber solution, preferably an aqueous basic amine absorber solution.31 . The method according to embodiment 30, wherein the basic amine absorber solution is selected from the group consisting of amines of the formula (I): NR1(R2)2, amines of the formula (II): R3R4N-X-NR5R6, 5- to 7-membered saturated heterocycles having one ormore nitrogen atoms incorporated in the ring, and mixtures of two or more thereof, wherein preferably R1is selected from C2-C6-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-al- kyl groups, hydroxy-Ci-C6-alkoxy-C2-Ce-alkyl groups and 1-piperazinyl-C2-Ce-alkyl groups; wherein preferably R2is selected from H, Ci-Ce-alkyl groups and C2-Ce-hydroxyalkyl groups; wherein preferably R3, R4, R5and R6are independently selected from H, Ci-Ce-alkyl groups, C2-Ce-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-alkyl groups and C2-Ce-aminoalkyl groups; wherein preferably X is a C2-Ce-alkylene group, -X1-NR7-X2- or -X1-O-X2; wherein preferably X1and X2are independently selected from C2-Ce-alkylene groups; wherein preferably R7is selected from H, Ci-Ce-alkyl groups, C2-Ce-hydroxyalkyl groups or C2-Ce-aminoalkyl groups; wherein preferably the 5- to 7-membered saturated heterocyles further comprise one or two heteroatoms selected from nitrogen and oxygen incorporated in the ring.32. The method according to any of embodiments 1 to 31 , wherein the absorber unit in the absorption step (2.2. a) comprises an absorber column.33. The method according to embodiment 32, wherein the absorber column comprises an inlet for the flue gas stream FS1 at the bottom of the column.34. The method according to embodiment 32 or 33, wherein the absorber column comprises an inlet for the absorbent A1 in the upper section of the column.35. The method according to any of embodiments 32 to 34, wherein the absorber column comprises absorption beds.36. The method according to any of embodiments 32 to 35, wherein the absorber column comprises an interstage cooler optionally driven by a pump, and preferably not driven by a pump.37. The method according to embodiment 36, wherein the interstage cooler is installed between the absorption beds.38. The method according to any of embodiments 32 to 37, wherein the absorber column is operated in a counter-current flow, and wherein FS1 is contacted with A1.39. The method according to any of embodiments 32 to 38, wherein the absorber column comprises an outlet of the absorbent A2 at the bottom of the column.40. The method according to any of embodiments 32 to 39, wherein the absorber column comprises an outlet of the flue gas stream FS2 at the head of the column.41 . The method according to any of embodiments 32 to 40, wherein the absorber column comprises an emission control system in the upper section of the column.42. The method according to any of embodiments 32 to 41 , wherein the absorber column comprises a washing section at the head of the column.43. The method according to embodiment 42, wherein the washing section comprises an inlet for make-up water.44. The method according to any of embodiments 1 to 43, wherein the regenerator unit in the regeneration step (2.2. b) comprises a desorber column.45. The method according to embodiment 44, wherein thermal energy is transferred from HS1 obtained in step (2.1) to a reboiler stream RS1 originating from a reboiler unit of the regenerator unit to obtain a reboiler stream RS2 having a higher thermal energy than RS1 .46. The method according to embodiment 44 or 45, wherein thermal energy is transferred from the reboiler stream RS2 to the absorbent A2 in the desorber column.47. The method according to any of embodiments 44 to 46, wherein the desorber column comprises an inlet of the absorbent A2 in the upper section of the column.48. The method according to any of embodiments 44 to 47, wherein the desorber column comprises an inlet of the reboiler stream RS2 at the lower section of the column.49. The method according to embodiment 48, wherein the reboiler stream RS2 comprises steam.50. The method according to any of embodiments 44 to 49, wherein the desorber column is operated in a counter-current flow, and wherein RS2 is contacted with A2.51 . The method according to any of embodiments 44 to 50, wherein the desorber column comprises an outlet of the absorbent A3 at the bottom of the column.52. The method according to any of embodiments 44 to 51 , wherein the desorber column comprises an outlet of the gaseous stream GS at the head of the column.53. The method according to any of embodiments 44 to 52, wherein the desorber column comprises two separate regeneration columns connected in series, optionally with an ad-ditional heat exchanger between the two columns, wherein the heat exchanger can be operated by external heat or by exchanging heat from the absorbent A3 to the partly regenerated absorption solution obtained from the first of the two regeneration columns.54. The method according to embodiment 53, wherein the desorber column comprises a further heat exchanger, wherein heat is exchanged from the absorbent A3 downstream of the additional heat exchanger to the absorbent A2 upstream of the first of the two regeneration columns.55. The method according to any of embodiments 44 to 54, wherein the absorbent A2 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.56. The method according to any of embodiments 1 to 55, wherein the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2.b) comprises one or more open loop and / or closed loop heat pumps.57. The method according to embodiment 56, wherein independently from one another, the one or more open loop and / or closed loop heat pumps comprise a heat transfer material selected from the group of water, ammonia, carbon dioxide, n-propane, n-butane, isobutene, n-pentane, trans-1-chloro-3,3,3-trifluoropropene, 1 ,1 ,1 ,3,3-pentafluoropropane,1 ,1 ,1 ,2-tetrafluoroethane, (1 E)-1 ,3,3,3-tetrafluoroprop-1-ene, (1 Z)-1 ,3,3,3-tetrafluoroprop- 1-ene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-butene or mixtures of two or more thereof.58. The method according to embodiment 56 or 57, wherein the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2. b) comprises a closed loop heat pump CHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 , ..., CPn), a second heat exchanger HE2 and an expander E1 , wherein the transfer of thermal energy comprises the steps of: i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM 1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfermedium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1 ; iv) expanding the heat transfer medium stream HTMS4 to obtain a heat transfer medium stream HTMS5 having a lower pressure than the heat transfer medium stream HTMS4 and recycling the heat transfer medium stream HTMS5 as the heat transfer medium stream HTMS1 to step i).59. The method according to embodiment 58, wherein the expansion step iv) is performed under adiabatic conditions.60. The method according to embodiments 58 or 59, wherein the expander E1 comprises a turbine, a throttle or a valve.61 . The method according to any of embodiments 58 to 60, wherein HTM1 comprises water, ammonia, carbon dioxide, n-propane, n-butane, 1 ,1 ,1 ,2-tetrafluoroethane, trans-1-chloro- 3,3,3-trifluoropropene, (Z)-1 ,1 ,1 ,4,4,4-hexafluor-2-butene, or mixtures of two or more thereof, preferably ammonia.62. The method according to embodiment 61 , wherein the stream HTMS1 has a pressure in the range of from 15 bara to 30 bara, preferably in the range of from 18 bara to 25 bara, more preferably in the range of from 20 to 24 bara.63. The method according to embodiments 61 or 62, wherein the stream HTMS3 has a pressure in the range of from 20 to 100 bara, preferably in the range of from 50 to 90 bara, more preferably in the range of from 70 to 80 bara.64. The method according to any of embodiments 58 to 63, wherein the stream HTMS5 has a temperature in the range of from 20 to 115 °C, preferably in the range of from 30 to 100 °C, more preferably in the range of from 40 to 80 °C, more preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C.65. The method according to embodiment 64, wherein the stream HTMS5 has the same temperature as HTMS1 .66. The method according to any of embodiments 58 to 65, wherein the stream HTMS5 has the same pressure as HTMS1 .67. The method according to embodiment 56 or 57, wherein the transfer of thermal energy from HS1 obtained in step (2.1) to the regeneration step (2.2. b) comprises an open loop heat pump OHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 , ..., CPn) and a second heat exchanger HE2, wherein the transfer of thermal energy comprises the steps of:i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM 1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfer medium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1.68. The method according to embodiment 67, wherein HTM1 comprises water, ammonia, carbon dioxide, n-propane, n-butane, trans-1-chloro-3,3,3-trifluoropropene, (Z)-1, 1 ,1 , 4,4,4- hexafluor-2-butene, or mixtures of two or more thereof, preferably water.69. The method according to embodiment 68, wherein the stream HTMS1 has a pressure in the range of from 0.05 bara to 2.0 bara, preferably in the range of from 0.1 bara to 1 bara, more preferably in the range of from 0.15 to 0.25 bara.70. The method according to embodiments 68 or 69, wherein the stream HTMS3 has a pressure in the range of from 2.00 to 5.00 bara, preferably in the range of from 3.00 to 3.80 bara, more preferably in the range of from 3.35 to 3.45 bara.71 . The method according to any of embodiments 58 to 70, wherein the respective compression step is performed under adiabatic conditions.72. The method according to any of embodiments 58 to 71 , wherein the respective compression step is performed in at least two compressors (CP1 CPn) connected in series.73. The method according to embodiment 72, wherein in-between each of the at least two compressors (CP1 CPn) a stream of the heat transfer material HTM1 is added.74. The method according to any of embodiments 58 to 73, wherein the heat source stream HS2 has a temperature in the range of from 40 to 120 °C, preferably in the range of from 45 to 105 °C, more preferably in the range of from 50 to 90 °C.75. The method according to any of embodiments 58 to 74, wherein the stream HTMS1 has a temperature in the range of from 20 to 115 °C, preferably in the range of from 30 to 100°C, more preferably in the range of from 40 to 80 °C, more preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C.76. The method according to any of embodiments 58 to 75, wherein the stream HTMS1 has a pressure equal to the vapour pressure of HTM1 at the temperature of HTMS1 .77. The method according to any of embodiments 58 to 76 wherein the stream HTMS2 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.78. The method according to embodiment 77, wherein the temperature of the stream HTMS2 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.79. The method according to any of embodiments 58 to 78, wherein the stream HTMS2 has the same pressure as the stream HTMS1.80. The method according to any of embodiments 58 to 79, wherein the stream HTMS3 has a temperature in the range of from 80 to 200 °C, preferably in the range of from 90 to 190 °C, more preferably in the range of from 120 to 160 °C, more preferably in the range of from 140 to 150 °C.81 . The method according to any of embodiments 58 to 80, wherein the stream HTMS3 has a pressure equal to the vapour pressure of HTM1 at the temperature of HTMS3.82. The method according to any of embodiments 58 to 81 , wherein the stream HTMS4 has a temperature in the range of from 75 to 195 °C, preferably in the range of from 90 to 180 °C, more preferably in the range of from 115 to 150 °C, more preferably in the range of from 135 to 145 °C.83. The method according to any of embodiments 58 to 82, wherein the stream HTMS4 has the same pressure as the stream HTMS3.84. The method according to any of embodiments 58 to 83, wherein the stream HRS1 has a temperature in the range of from 105 to 160 °C, preferably in the range of from 110 to 135 °C, more preferably in the range of from 115 to 125 °C.85. The method according to any of embodiments 58 to 84, wherein the stream HRS1 has a pressure in the range of from 1.1 to 5 bara, preferably in the range of from 1.3 to 3 bara, more preferably in the range of 1 .5 to 2.5 bara.86. The method according to any of embodiments 58 to 85, wherein the stream HRS2 has a temperature in the range of from 106 to 165 °C, preferably in the range of from 111 to 138 °C, more preferably in the range of from 116 to 130 °C.87. The method according to embodiment 86, wherein the temperature of the stream HRS2 is in the range of from >0.5 to <10 °C higher than the temperature of the stream HRS1 , preferably in the range of from >0.75 to <7.0 °C, more preferably in the range of from >1.0 to <5.0 °C.88. The method according to any of embodiments 58 to 87, wherein the stream HRS2 has the same pressure as the stream HRS1 .89. The method according to any of embodiments 67 to 88, wherein the open loop heat pump OHP1 further comprises a third heat exchanger HE3 located downstream of the second heat exchanger HE2, wherein the transfer of thermal energy comprises the additional steps of iv) transferring thermal energy from the heat transfer medium stream HTMS4 to the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS5’ having a reduced thermal energy compared to the heat transfer medium stream HTMS4 and a heat transfer medium stream HTMS2’ having an increased thermal energy compared to the heat transfer medium stream HTMS2; v) feeding the heat transfer medium stream HTMS2’ as the heat transfer medium stream HTMS2 in step ii).90. The method according to embodiment 89, wherein the stream HTMS2’ 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.91 . The method according to embodiment 89 or 90, wherein the stream HTMS2’ has the same pressure as the stream HTMS2.92. The method according to any of embodiments 89 to 91 , 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.93. The method according to embodiment 92, wherein the temperature of the stream HTMS5’ is in the range of from >0 to <20 °C higher than the temperature of the stream HTMS2, preferably in the range of from >1.0 to <15 °C, more preferably in the range of from >2.0 to <10 °C.94. The method according to any of embodiments 89 to 93, wherein the stream HTMS5’ has the same pressure as the stream HTMS4.95. The method according to any of embodiments 89 to 94, wherein the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4 located downstream of the third heat exchanger HE3, wherein the transfer of thermal energy comprises the additional steps of vi) transferring thermal energy from the heat transfer medium stream HTMS5’ to a heat transfer material stream MS1 of heat transfer material HTM1 to obtain a heat transfer material stream MS2 having an increased thermal energy compared to the material stream MS1 and a heat transfer medium stream HTMS6 having a reduced thermal energy compared to the heat transfer medium stream HTMS5’; vii) feeding the material stream MS2 into the heat transfer medium stream HTMS2 prior to its compression in step ii).96. The method according to embodiment 95, wherein at least two compressors (CP1 CPn) are used, wherein at least part of the material stream MS2 is added in-between each of the at least two compressors in the compression step ii).97. The method according to embodiment 95 or 96, 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.98. The method according to any of embodiments 95 to 97, 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.99. The method according to any of embodiments 95 to 98, 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.100. The method according to any of embodiments 95 to 99, wherein the stream MS2 has the same pressure as MS1 .101 . The method according to any of embodiments 95 to 100, 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.102. The method according to embodiment 101 , 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.103. The method according to any of embodiments 95 to 102, wherein the stream HTMS6 has the same pressure as HTMS5’.104. The method according to any of embodiments 58 to 103, wherein the heat transfer medium stream HTMS2 or HTMS2’ is a liquid heat transfer material stream IHTMS2a, wherein the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn) located downstream of the first heat exchanger HE1 or optionally downstream of the third heat exchanger HE3 and upstream of the one or more compressors (CP1 CPn), wherein the transfer of thermal energy comprises the additional steps of1.1 ) expanding the liquid heat transfer medium stream IHTMS2a to obtain a heat transfer medium stream HTMS2b having a lower pressure than the heat transfer material stream IHTMS2a comprising a gaseous and a liquid phase;1.2) separating the gaseous phase from the heat transfer medium stream HTMS2b to obtain a gaseous heat transfer medium stream gHTMS2b and a liquid heat transfer medium stream IHTMS2b;1.3) feeding the gaseous heat transfer medium stream gHTMS2b as the heat transfer medium stream HTMS2 in step ii);1.4) optionally recycling the liquid heat transfer medium stream IHTMS2b as the heat transfer medium stream HTMS1 in step i).105. The method according to embodiments 104, wherein the expansion step i.1) is performed under adiabatic conditions.106. The method of embodiment 104 or 105, wherein the one or more expanders (EP1 EPn) comprise a turbine, a throttle, a valve or a mixture thereof.107. The method according to any of embodiments 104 to 106, wherein the respective expansion step is performed in at least two expanders (EP1 EPn) connected in series.108. The method according to any of embodiments 104 to 107, wherein the stream gHTMS2b has a temperature in the range of from 40 to 100 °C, preferably in the range of from 50 to 80 °C, more preferably in the range of from 55 to 65 °C.109. The method according to any of embodiments 104 to 108, wherein the stream IHTMS2b has the same temperature as the stream gHTMS2b.110. The method according to any of embodiments 58 to 109, wherein the heat exchanger HE2 is comprised in the regenerator unit of the regeneration step (2.2.b).111. The method according to embodiment 110, wherein the heat exchanger HE2 is comprised in the reboiler unit of the regenerator unit.112. The method according to embodiment 111 wherein the reboiler stream RS1 is the heat recipient stream HRS1 and the reboiler stream RS2 is the heat recipient stream HRS2.113. The method according to any of embodiments 56 to 112, wherein the transfer of thermal energy from the heated stream HS1 obtained in step (2.1) to the regeneration step (2.2. b) comprises at least two closed loop and / or open loop heat pumps, which are connected in series.114. The method according to embodiment 113, wherein the heat transfer medium stream HTMS1 of the respective heat pump is the heat recipient stream HRS1 of the previous heat pump and the heat transfer medium stream HTMS2 of the respective heat pump is the heat recipient stream HRS2 of the previous heat pump.115. The method according to embodiment 113 or 114, wherein the last heat pump of the series is an open loop heat pump OHP1 , wherein the heat transfer medium stream HTMS4 of the last heat pump is fed to a heat exchanger to transfer heat to the heat transfer medium stream HTMS2 of the first heat pump of the series.116. The method according to any of embodiments 113 to 115, wherein the heat exchanger HE2 of the last heat pump of the series is comprised in the regenerator unit of the regeneration step (2.2. b).117. The method according to embodiment 116, wherein the heat exchanger HE2 of the last heat pump of the series is comprised in the reboiler unit of the regenerator unit.118. The method according to any one of embodiments 1 to 117, wherein the regenerator unit has a coefficient of performance (COP) of >1 .5, preferably of >2, more preferably in the range of from 2 to 4, more preferably in the range of from 2.5 to 3.8.119. The method according to any of embodiments 113 to 118, wherein the heat transfer materials HTM 1 comprised independently from one another in each of the at least two heat pumps comprise the same heat transfer material and / or different heat transfer materials.120. The method according to any of embodiments 113 to 119, wherein the transfer of thermal energy comprises a closed loop heat pump CHP1 as a first heat pump and an open loop heat pump OHP1 as a second heat pump connected in series.121. The method according to embodiment 120, wherein HTM1 of the closed loop heat pump CHP1 is ammonia and HTM1 of the open loop heat pump OHP1 is water.122. The method according to any of embodiments 1 to 121 wherein the carbonaceous fuel comprises alkanes, preferably methane, and ethane.123. The method according to any of embodiments 1 to 122 wherein the stream of the cooled cracked gas obtained in (2.1) is subjected to one or more post processing steps.124. The method according to embodiment 123, wherein the one or more post processing steps comprises a step for separating methane from the stream of the cooled cracked gas.125. The method according to embodiment 124, wherein the separated methane constitutes at least a part of the carbonaceous fuel used to heat at least one of the one or more crackers.126. The method according to any of embodiments 123 to 125, wherein the one or more post processing steps further comprises a step for separating ethylene from the stream of the cooled cracked gas.127. The method according to embodiment 126, wherein the separated ethylene is further subjected to one or more chemical conversion steps.128. A cracker product obtained or obtainable according to the method of any of embodiments 1 to 127 having a lower carbon footprint.129. A process for the manufacture of one or more chemical compounds or materials comprising:(A) providing a cracker product according to embodiment 128;(B) subjecting the cracker product provided in step (A) to one or more chemical conversion reactions, obtaining one or more chemical compounds or materials.130. Use of a cracker product according to embodiment 128 for the production of a chemical compound or material.131. A process, preferably according to any of embodiments 1 to 127, comprising the step of converting the stream of the cooled cracked gas obtainable or obtained by the method of any of embodiments 1 to 127 to obtain a product Q.130. The process of embodiment 131 , 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 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.131 . The process of embodiment 131 or 132, wherein the content of the stream of the cooled cracked gas obtainable or obtained by the method of any one of embodiments 1 to 127 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 stream of the cooled cracked gas obtainable or obtained by the method of any one of embodiments 1 to 127 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 a closed loop heat pump CHP1 , in particular comprising a first heat exchanger HE1 , one or more compressors (CP1 Cn), a second heat exchanger HE2 and an expander E1.Figure 2: shows a simplified depiction of an open loop heat pump OHP1 , in particular comprising a first heat exchanger HE1 , one or more compressors (CP1 Cn), and a second heat exchanger HE2.Figure 3: shows a simplified depiction of an open loop heat pump OHP1 further comprising one additional heat exchanger, in particular comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn), a second heat exchanger HE2 and a third heat exchanger HE3.Figure 4: shows a simplified depiction of an open loop heat pump OHP1 further comprising two additional heat exchangers, in particular comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn), a second heat exchanger HE2, a third heat exchanger HE3 and a fourth heat exchanger HE4.Figure 5: shows a simplified depiction of a closed loop heat pump CHP1 further comprising one or more additional expanders, in particular comprising a first heat exchanger HE1 , one or more expanders (EP1 EPn), one or more compressors (CP1 CPn), a second heat exchanger HE2 and an expander E1.Figure 6: shows a simplified depiction of an open loop heat pump OHP1 further comprising one or more additional expanders, in particular comprising a first heat exchanger HE1 , one or more expanders (EP1 EPn), one or more compressors (CP1 CPn) and a second heat exchanger HE2.Cited literatureUllmann’s Encyclopedia of Industrial Chemistry, 2012, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim, 7thedition, volume 13: “Ethylene”, pages 469-515C. Arpagaus et aL, Energy 152 (2018), pages 985 to 1010Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[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 ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC)- US 2024 / 150260 A1

Claims

Claims1 . A method for the manufacture of a cracker product selected from the group consisting of C1-C3 alkanes, C2-C12 alkenes, C2-C4 alkines, aromatic compounds, and mixtures of two or more thereof, from a hydrocarbon feedstock, said method comprising the steps of:(1 ) cracking a hydrocarbon feedstock to obtain a cracked gas comprising ethylene, wherein cracking is effected in one or more crackers, wherein at least one of the crackers is, at least partially, directly or indirectly heated by combusting a carbonaceous fuel, and wherein the combustion of the carbonaceous fuel generates a carbon dioxide comprising flue gas stream FS1 ;(2.1 ) quenching at least a fraction of the cracked gas by contacting at least the fraction of cracked gas with water to obtain a stream HS1 of heated water, and a stream of cooled cracked gas;(2.2) subjecting the carbon dioxide comprising flue gas stream FS1 generated in step (1) to a carbon capture process comprising:(2.

2. a) an absorption step in which flue gas stream FS1 is contacted with an absorbent A1 in an absorber unit to obtain an absorbent A2 laden with carbon dioxide and a flue gas stream FS2 from which carbon dioxide has been at least partly removed;(2.2.b) a regeneration step in which at least a portion of the laden absorbent A2 obtained from step b) is heated in a regenerator unit to obtain an at least partly regenerated absorbent A3 and a gaseous stream GS comprising carbon dioxide;(2.2.c) a recycling step in which at least a fraction of the regenerated absorbent A3 from step b) is recycled as absorbent A1 into the absorption step (2.

2. a); wherein thermal energy is transferred from HS1 obtained in step (2.1 ) to the regeneration step (2.

2. b).

2. The method according to claim 1 , wherein the cracking of the hydrocarbon feedstock in step (1) comprises steam cracking.

3. The method according to claim 1 or 2, wherein at least one of the crackers is indirectly heated by combusting a carbonaceous fuel.

4. The method according to any one of claims 1 to 3, wherein the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.

2. b) comprises one or more open loop and / or closed loop heat pumps.

5. The method according to claim 4, wherein the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2.b) comprises a closed loop heat pump CHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn), a second heat exchanger HE2 and an expander E1 , wherein the transfer of thermal energy comprises the steps of:i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM 1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfer medium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1 ; iv) expanding the heat transfer medium stream HTMS4 to obtain a heat transfer medium stream HTMS5 having a lower pressure than the heat transfer medium stream HTMS4 and recycling the heat transfer medium stream HTMS5 as the heat transfer medium stream HTMS1 to step i).

6. The method according to claim 4, wherein the transfer of thermal energy from HS1 obtained in step (2.1 ) to the regeneration step (2.2.b) comprises an open loop heat pump OHP1 comprising a first heat exchanger HE1 , one or more compressors (CP1 CPn) and a second heat exchanger HE2, wherein the transfer of thermal energy comprises the steps of: i) transferring thermal energy from HS1 in the first heat exchanger HE1 to a heat transfer medium stream HTMS1 of a heat transfer material HTM 1 to obtain a heat transfer medium stream HTMS2 having an increased thermal energy compared to the heat transfer medium stream HTMS1 and a stream HS2 having a reduced thermal energy compared to HS1 ; ii) compressing the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS3 having a higher pressure than the heat transfer medium stream HTMS2; iii) transferring thermal energy from the heat transfer medium stream HTMS3 in the second heat exchanger to the heat recipient stream HRS1 to obtain a heat transfer medium stream HTMS4 having a reduced thermal energy compared to the heat transfer medium stream HTMS3 and the heat recipient stream HRS2 having an increased thermal energy compared to the heat recipient stream HRS1 .

7. The method according to claim 5 or 6, wherein the stream HRS2 has a temperature in the range of from 106 to 165 °C, preferably in the range of from 111 to 138 °C, more preferably in the range of from 116 to 130 °C.

8. The method according to claim 6 or 7, wherein the open loop heat pump OHP1 further comprises a third heat exchanger HE3 located downstream of the second heat exchanger HE2, wherein the transfer of thermal energy comprises the additional steps of iv) transferring thermal energy from the heat transfer medium stream HTMS4 to the heat transfer medium stream HTMS2 to obtain a heat transfer medium stream HTMS5’ having a reduced thermal energy compared to the heat transfer medium stream HTMS4 and a heat transfer medium stream HTMS2’ having an increased thermal energy compared to the heat transfer medium stream HTMS2; v) feeding the heat transfer medium stream HTMS2’ as the heat transfer medium stream HTMS2 in step ii).

9. The method according to claim 8, wherein the open loop heat pump OHP1 further comprises a fourth heat exchanger HE4 located downstream of the third heat exchanger HE3, wherein the transfer of thermal energy comprises the additional steps of vi) transferring thermal energy from the heat transfer medium stream HTMS5’ to a heat transfer material stream MS1 of heat transfer material HTM1 to obtain a heat transfer material stream MS2 having an increased thermal energy compared to the material stream MS1 and a heat transfer medium stream HTMS6 having a reduced thermal energy compared to the heat transfer medium stream HTMS5’; vii) feeding the material stream MS2 into the heat transfer medium stream HTMS2 prior to its compression in step ii).

10. The method according to any of claims 5 to 9, wherein the heat transfer medium stream HTMS2 or HTMS2’ is a liquid heat transfer material stream IHTMS2a, wherein the closed loop heat pump CHP1 or the open loop heat pump OHP1 further comprises one or more expanders (EP1 EPn) located downstream of the first heat exchanger HE1 or optionally downstream of the third heat exchanger HE3 and upstream of the one or more compressors (CP1 CPn), wherein the transfer of thermal energy comprises the additional steps of1.1 ) expanding the liquid heat transfer medium stream IHTMS2a to obtain a heat transfer medium stream HTMS2b having a lower pressure than the heat transfer material stream IHTMS2a comprising a gaseous and a liquid phase;1.2) separating the gaseous phase from the heat transfer medium stream HTMS2b to obtain a gaseous heat transfer medium stream gHTMS2b and a liquid heat transfer medium stream IHTMS2b;1.3) feeding the gaseous heat transfer medium stream gHTMS2b as the heat transfer medium stream HTMS2 in step ii);1.4) optionally recycling the liquid heat transfer medium stream IHTMS2b as the heat transfer medium stream HTMS1 in step i).11 . The method according to any of claims 5 to 10, wherein the heat exchanger HE2 is comprised in the regenerator unit of the regeneration step (2.

2. b).

12. The method according to any of claims 5 to 11 , wherein the transfer of thermal energy from the heated stream HS1 obtained in step (2.1) to the regeneration step (2.

2. b) comprises at least two closed loop and / or open loop heat pumps, which are connected in se- ries.

13. The method according to any of claims 1 to 12, wherein the stream of the cooled cracked gas obtained in (2.1) is subjected to one or more post processing steps.

14. A cracker product obtained or obtainable according to the method of any of claims 1 to 13 having a lower carbon footprint.

15. A process, preferably according to any one of claims 1 to 13, comprising the step of converting the stream of the cooled cracked gas obtainable or obtained by the process of any one of claims 1 to 14 to obtain a product Q.

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