Method for controlling heat-consuming hydrocarbon conversion process

Abstract

The present invention relates to a method for controlling a process performed in an integrated production plant wherein the process comprises subjecting at least one hydrocarbon feed stream to hydrocarbon conversion in a heat-consuming hydrocarbon conversion unit, and wherein the process is controlled such that heat that cannot be supplied to the heat-consuming hydrocarbon conversion unit via one or more plant external sustainable heat sources is preferably supplied by hydrogen obtained from a light hydrocarbon conversion off-gas stream obtained from the heat-consuming hydrocarbon conversion unit.

Description

[0001] The present invention relates to a method for controlling a process carried out in an integrated production plant, wherein the process comprises subjecting at least one hydrocarbon feed stream to hydrocarbon conversion in a heat-consuming hydrocarbon conversion unit, and further relates to the process itself. Furthermore, the present invention relates to an integrated production plant in which the process and the method are carried out.

[0002] Many basic hydrocarbon conversion processes are typically endothermic, requiring heat to operate. Examples include processes conducted in plants that include crackers (e.g., steam crackers, ammonia plants, or steam reformers). If such processes were conducted in accordance with responsible, eco-driven process management, they would utilize one or more external, sustainable heat sources (e.g., solar, wind, hydro, tidal, geothermal, and biomass, ammonia obtained from renewable sources, biomethane, bio-LNG, and H2 obtained from renewable sources) to provide the necessary heat. However, the availability of such external, sustainable heat sources may vary over time, and during certain periods, the corresponding heat supply may be insufficient to meet the process's needs. Of course, in such cases, it is generally conceivable to use other, non-sustainable, external heat sources in addition to the external, sustainable heat sources, i.e., fossil heat sources such as coal, petroleum, or coal. However, based on the eco-driven process management discussed above, this is not an entirely preferred procedure. Alternatively, depending on the scenario, the hydrocarbon conversion process could be shut down and restarted only when the required heat supply via the external, sustainable heat sources is sufficiently high again; needless to say, this alternative is inherently undesirable from an economic perspective.

[0003] US Pat. No. 11,498,834 B1 discloses a method for producing H2-rich fuel gas from hydrocarbons, such as natural gas, and its use in industrial heating, such as in olefin production plants. A hydrocarbon feedstock is fed to a heat-consuming hydrocarbon conversion (e.g., a steam cracker) to obtain a product stream, which, after separation, yields, in particular, a light hydrocarbon conversion waste gas stream containing CH4. This light hydrocarbon conversion waste gas stream is reformed to obtain a product gas stream containing CO and H2. The product gas stream can be further processed in a controllable processing unit to obtain a stream rich in H2.

[0004] EP 3 249 028 A1 relates to a low-emission process for producing olefins by steam cracking, wherein a gas mixture is provided by using a plurality of tubular reactors, each of which uses a combined multiple tubular reactor.

[0005] The object of the present invention is therefore to provide a method for controlling a process which is carried out in an integrated production plant and which comprises subjecting at least one hydrocarbon feed stream to hydrocarbon conversion in a heat-consuming hydrocarbon conversion unit in such a way that the smallest possible amount of fossil heat sources external to the plant is used, in the event that the heat supply for said hydrocarbon conversion cannot be provided by sustainable heat sources external to the plant.

[0006] The present invention therefore relates to a method for controlling a process carried out in an integrated production plant, wherein the integrated production plant comprises

[0007] (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ;

[0008] (2) The unit U C The unit comprises a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2;

[0009] (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT ——The internal heat source H of the equipment INT Including H2, for the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ;

[0010] (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R ;

[0011] (5) Controllable processing unit U P , used for processing S R or its partial flow S' R To obtain S R or S' RCompared with H2-rich stream S H ;

[0012] (6) and optionally includes a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , and is used to convert S' R Send to U P middle;

[0013] The process includes

[0014] (i) one or more heat sources according to (3) are removed from M E Send to M H , which is sufficient to H Producing satisfaction U C The heat requirement E for the hydrocarbon conversion UC of calories;

[0015] (ii) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C undergoes hydrocarbon conversion to obtain the one or more product streams S and S O ;

[0016] (iii) S O Send to U R In and make S O in U R After undergoing restructuring, it obtained S R ;

[0017] Wherein the method for controlling the process comprises

[0018] (a) Determine U C The hydrocarbon conversion in M H Provided caloric demand E UC ;

[0019] (b) determining a sustainable heat source H external to the one or more devices EXT-S Available for U C The amount of calories E EXT-S ;

[0020] (c) Determine ΔE = E UC –E EXT-S ,and

[0021] (c.1) If ΔE>0, then

[0022] (c.1.1) Determine H2N , that is, in M H The amount of H2 required to produce ΔE in

[0023] (c.1.2) Determine H 2P , which is used to H Production volume E H2P The calories in U R and U P can be generated to be included in S H The maximum amount of H2 in

[0024] (c.1.3) Determine ΔH = H 2N –H 2P ;and

[0025] (c.1.3.1) If ΔH > 0, then

[0026] Control the processing unit U P , the supply device M E And optionally the supply device M R , so that H 2P Via S H Send to M H middle;

[0027] The process further comprises

[0028] (iv) Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100;

[0029] (v) The stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0030] (vi) Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where y = 100;

[0031] (vii) will be from M E The obtained stream S' H As H INT Send to M H middle;

[0032] (viii) the external fossil heat source H of the one or more devices EXT-F At least one of them is passed through M E Send to M H In the amount sufficient to H Production (ΔE-E H2P ) calories;

[0033] (c.1.3.2) If ΔH ≤ 0, then

[0034] Control the processing unit U P , the supply device M E And optionally the supply device M R , so that it will be sufficient to H The amount of H2 produced in ΔE is S H Send to M H middle;

[0035] The process further comprises

[0036] (iv') Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0 <x≤100;

[0037] (v') the stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0038] (vi') Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where 0 <y≤100;

[0039] (vii') will be from M E The obtained stream S' H As H INT Send to M H middle;

[0040] (c.2) If ΔE≤0, then

[0041] Control the processing unit U P , the supply device M E And optionally the supply device M R , so that H2 is not transferred through S H Send to MH middle;

[0042] The process further comprises

[0043] (iv") Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x≤100;

[0044] (v") R Or if (iv') is performed and x≠0, then the stream S' R Send to U P In, get S H ;

[0045] (vi”) Make the flow S H If from U P If you get it, through M E , and get S H 100 vol-% flow S" H ;

[0046] (vii”) From M E Remove the stream S from H .

[0047] Unit U C

[0048] Typically, for a unit U for heat-consuming hydrocarbon conversion according to (1) C is part of the equipment, without any specific restrictions, provided that C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O Preferably, the unit U for heat-consuming hydrocarbon conversion C Including lysis unit U CC .

[0049] Cracking is a petrochemical process in which saturated hydrocarbons with long molecular structures are broken down (i.e., cracked) into smaller saturated or unsaturated molecules. Typically, crackers are designed to produce light olefins, especially ethylene and propylene, as valuable products. Cracking processes include fluid catalytic cracking (FCC) and steam cracking.

[0050] Conventional steam cracking utilizes a pyrolysis furnace having two main sections: a convection section and a radiant section. The hydrocarbon feedstock typically enters the convection section of the furnace as a liquid or, in the case of light feedstocks, as a vapor, where it is typically heated and, if necessary, vaporized by indirect contact with hot exhaust gases from the radiant section and by direct contact with steam. The vaporized feedstock and steam mixture is then introduced into the radiant section where cracking occurs. The resulting stream, typically having a temperature in the range of 500°C to 650°C, enters a fired tubular reactor and is heated to a temperature typically in the range of 750°C to 875°C for 0.1 to 0.5 seconds, with control of residence time, temperature profile, and partial pressure. During this short reaction time, the hydrocarbons in the feedstock are cracked into smaller molecules, producing light olefins such as ethylene, propylene, butenes, other small molecule olefins, and diolefins as the main products in addition to methane. These reaction products suitably leave the radiant tube at a temperature typically in the range of 800°C to 850°C and are preferably cooled within 0.02 to 0.1 seconds to a temperature typically in the range of 550°C to 650°C in order to prevent degradation of the highly reactive compounds by secondary reactions. The resulting stream then leaves the furnace for further downstream processing.

[0051] In fluid catalytic cracking (FCC), particulate catalyst (typically having a particle size in the range of 20 to 100 μm) circulates between a cracking reactor and a catalyst regenerator. In the reactor, the hydrocarbon feed contacts a hot regenerated catalyst. The hot catalyst typically vaporizes and cracks the feed at 425°C to 600°C. The cracking reaction deposits carbonaceous hydrocarbons, which eventually become coke on the catalyst, thereby deactivating the catalyst. Usually with the aid of a catalyst stripper, the cracked product is separated from the coked catalyst, and the stripped catalyst is then regenerated in the regenerator. The catalyst regenerator burns the coke from the catalyst with an oxygen-containing gas (typically air). Catalyst regeneration is restored to catalyst activity by oxidation and the catalyst is typically heated to 500°C to 900°C at the same time. The heated catalyst is recycled to the cracking reactor to crack more fresh hydrocarbon feed.

[0052] According to the present invention, the cracking unit U CC Preferably it is a thermal cracking unit, more preferably a steam cracking unit.

[0053] Feed flow S F

[0054] wherein according to (ii) at least one is sent to U C One or more hydrocarbon feed streams S in which hydrocarbon conversion is carried out FThe hydrocarbon feed streams S may be derived, for example, from upstream refinery processes such as atmospheric distillation columns, hydrocrackers, cokers, etc., and typically contain naphtha, liquefied petroleum gas (LPG), ethane, propane and / or butane. Alternatively or additionally, one or more hydrocarbon feed streams S F Comprising at least one of: a hydrocarbon feed stream comprising, preferably consisting of, fossil hydrocarbons; a hydrocarbon feed stream comprising, preferably consisting of, recycled hydrocarbons; and a hydrocarbon feed stream comprising, preferably consisting of, biohydrocarbons.

[0055] As used herein, the term "fossil hydrocarbons" encompasses, for example, natural gas, such as a mixture of naturally occurring gaseous hydrocarbons that consists primarily of methane, in addition to small amounts of other higher alkanes (e.g., ethane, propane, etc.). Further, as used herein, the term "fossil hydrocarbons" encompasses naphtha, such as a liquid hydrocarbon mixture produced from natural gas condensate, petroleum distillates, and distillates of coal tar and peat. Still further, as used herein, the term "fossil hydrocarbons" encompasses liquefied petroleum gas (LPG), such as a fuel gas containing a flammable mixture of hydrocarbon gases, particularly propane and butane, produced by refining petroleum or "wet" natural gas.

[0056] The term "recycled hydrocarbons" as used herein encompasses pyrolysis oils obtained, for example, by pyrolysis of recycled plastic waste.

[0057] As used herein, the term "biohydrocarbons" encompasses, for example, bio-based gases, such as a mixture of gases consisting primarily of methane in addition to carbon dioxide and hydrogen sulfide, produced from raw materials such as agricultural waste, manure, municipal waste, plant material, sewage, green waste, food waste, etc. Further, as used herein, the term "biohydrocarbons" encompasses bio-naphtha, such as naphtha produced from a complex mixture of naturally occurring fats and oils. Still further, as used herein, the term "biohydrocarbons" encompasses bio-liquefied petroleum gas (bio-LPG), such as liquefied petroleum gas produced from a complex mixture of naturally occurring fats and oils.

[0058] According to the present invention, one or more hydrocarbon feed streams S F Preferably, the feed stream comprises at least one of: a hydrocarbon feed stream comprising, preferably consisting of, fossil hydrocarbons; a hydrocarbon feed stream comprising, preferably consisting of, recycled hydrocarbons; and a hydrocarbon feed stream comprising, preferably consisting of, biogenic hydrocarbons. Thus, mixtures of two or more of the above are also encompassed.

[0059] According to the present invention, the unit UC further comprises a heating device M for providing heat for the hydrocarbon conversion. H The heating device M H including a heat source H S , i.e., from one or more sustainable heat sources H outside the device EXT-S , and / or one or more external fossil heat sources HEXT-F , and / or one or more internal heat sources H INT A device for generating heat. Further, at least one heat source H S including hydrogen (H2), which is contained in H EXT-S , and / or H EXT-F and / or H INT Therefore, included in U C Heating device M H It comprises at least means for burning H2 and providing the resulting heat to hydrocarbon conversion.

[0060] U C Calorie needs

[0061] According to (i), one or more heat sources according to (3) are removed from M E Send to M H , which is sufficient to H Producing satisfaction U C Heat requirement E for hydrocarbon conversion UC of calories.

[0062] According to the present invention, in the unit U of the integrated device C The heat requirement E of the hydrocarbon conversion process carried out in UC Typically via one or more external sustainable heat sources H EXT-S However, in the case that H EXT-S Supply heat demand E UC In the case that additional heat is required, the additional heat is at least partially supplied by the process unit U P The obtained flow S H In addition to the heat source H2 contained in the flow S H In addition to the H2 in the device, one or more other internal heat sources H INT By means of a controllable device M E To U C Heat supply, for example hydrogen generated within the device from other sources, and / or fuel and / or electric heat generated within other devices can be used. Preferably, according to the present invention, the heat contained in the stream S H The heat source H2 is the only internal heat source of the device. INT , which is used to replace H EXT or except H EXT In addition to meeting U C Calorie requirement E UC If and only if H EXT-S With H INT The combination cannot satisfy U C Calorie requirement E UCThe remaining energy demand will be met by one or more external fossil heat sources H EXT-F supply.

[0063] In order to H The hydrogen is preferably burned based on the flow S H And through device M E Provided stream S' H Mixed with oxygen and included in U C Burns in a burner or heating coil.

[0064] Typically, for the use of sustainable heat sources H EXT-S No specific restrictions. Preferably, according to the present invention, one or more devices according to (3) have an external sustainable heat source H EXT-S The invention relates to one or more of solar energy, wind energy, hydroelectric energy, tidal energy, geothermal energy, biomass energy, ammonia obtained from renewable sources, biomethane, bio-LNG and H2 obtained externally from renewable sources. Depending on their respective physical properties, the external sustainable heat source H EXT-S For example, it is used to provide heat via direct electrical heating or via combustion, as in the case of hydrogen, where the heat energy is provided to a heat-consuming hydrocarbon conversion process. Typically, the combustion of hydrogen produces water as the only by-product. Therefore, it is advantageous, especially if hydrogen is used as a sustainable heat source H external to the plant. EXT-S , then the process of the present invention allows for reduced emission operation of a hydrocarbon conversion process, preferably a cracking process. As used herein, the term "reduced emission operation" relates to a process that is performed in a manner that avoids or at least reduces the emission of greenhouse gases (such as carbon dioxide), i.e., with a reduced carbon footprint.

[0065] Processing of cracking gas

[0066] Especially when unit U C Including lysis unit U CC In the case of the above, the gas stream obtained directly from hydrocarbon conversion (ie cracking process) (said stream is referred to herein as cracking gas stream S) is C ) is subjected to one or more downstream process stages, from which one or more product streams S and a light hydrocarbon conversion offgas stream S are obtained in particular O .

[0067] Typically, a stream S containing light olefins such as ethylene, propylene, butenes, other lower olefins other than methane, and diolefins is converted to a slurry by using a series of separation and chemical treatment stages. CSeparation into several different streams. In hydrocarbon conversion processes, light by-products such as hydrogen, carbon oxides, light saturated hydrocarbons and water are typically obtained. Suitably, one or more product streams S, in particular ethylene and propylene, are used directly in downstream processes, optionally or preferably in part of an integrated plant, or stored in storage vessels for subsequent use or long-term storage (either internally or externally to the plant).

[0068] The recovery of the various olefin products (i.e., product streams) from the cracked gas is typically performed by fractionating the gas using a series of distillation steps to separate the various components. The unit that separates the hydrocarbons with one carbon atom (C1) from the lighter fractions is typically called a "demethanizer." The unit that separates the hydrocarbons with two carbon atoms (C2) from the heavier components is called a "deethanizer." The unit that separates the hydrocarbon fraction with three carbon atoms (C3) from the heavier components is called a "depropanizer." The unit that separates the hydrocarbon fraction with four carbon atoms (C4) from the heavier components is called a "debutanizer."

[0069] With higher carbon number fraction (C 5+ The remaining heavier components of the pyrolysis reactor can be used as gasoline or recycled back to the cracker. Alternatively, they can be sent to a suitable hydrocarbon hydrogenation process.

[0070] The various fractionation units can be arranged in various sequences to provide the desired results based on the various feedstocks. For this reason, a sequence in which the demethanizer is used first is often referred to as a "front-end demethanizer" sequence. Similarly, when the deethanizer is used first, it is often referred to as a "front-end deethanizer" sequence. And, when the depropanizer is used first, it is often referred to as a "front-end depropanizer" sequence.

[0071] In a conventional front-end demethanizer sequence, hydrocarbons (C1 to C 5+ ) first enters a demethanizer where methane and lighter fractions (hydrogen) are separated as overhead streams. The demethanizer is typically operated at relatively low temperatures, typically in the range of -100°C to about 25°C.

[0072] The top distillate stream of the front-end demethanizer is sent to the reforming unit U according to (iii). R Alternatively, the hydrogen contained in the front-end demethanizer overhead stream may be removed first and the remaining gas consisting mainly of methane as stream S according to (iii). O Sent to reforming unit U R .

[0073] The heavy fraction leaving the demethanizer is mainly composed of C2 to C 5+These heavy fractions are then preferably sent to a deethanizer where the C2 hydrocarbons are removed overhead and the C3 to C 5+ The compounds leave the deethanizer as the bottoms. The C2 components exiting the deethanizer overhead can be fed to an acetylene converter or acetylene removal unit. Since some methane remains dissolved in the heavy fractions leaving the deethanizer and ultimately in the C2 components leaving the deethanizer, the C2 component stream can then be sent to a demethanizer to remove the remaining methane. This residual demethanizer overhead stream will then constitute a suitable light hydrocarbon waste gas stream S O According to (iii) sent to the reforming unit U R .

[0074] Therefore, unit U C Preferably further comprising a separation unit U S , wherein according to (ii), the process comprises

[0075] (ii.1) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C The cracked gas stream S is obtained by hydrocarbon conversion. C ;

[0076] (ii.2) The cracked gas stream S obtained according to (ii.1) C Sent to a separation unit U comprising at least one demethanation unit S , the stream S is obtained from the demethanation unit O , from U S The one or more product streams S are obtained.

[0077] As mentioned above, the separation unit U S Preferably, a distillation column is included from which an overhead stream comprising methane and hydrogen is obtained. The overhead stream comprises methane and hydrogen as major components. The ratio of methane to hydrogen in the overhead stream can be adjusted according to the cracking operating conditions and the hydrocarbon feed stream S, respectively. FThe methane content of the overhead product varies depending on the cracking yield of the feedstock. For example, reference can be made to Ullmann's Encyclopedia of Industrial Chemistry, Ethylene 5.1.3 Commercial Cracking Yields, DOI: 10.1002 / 14356007.a10_045.pub3, for information on different cracking yields depending on the feedstock. Typically, the methane concentration in the overhead product is in the range of 40 to 95 wt. % methane, preferably in the range of 90 to 95 wt. % methane, with the remainder primarily being hydrogen.

[0078] Still further preferred is a separation unit comprising, in addition to and downstream of the distillation column, a gas separation unit from which a methane-rich stream and a hydrogen-rich stream are obtained based on the overhead stream comprising methane and hydrogen. O Direct access to U R In contrast, separating the overhead stream and making only the methane-rich stream as stream S O Enter U R A higher total hydrogen yield is obtained because R The reforming process carried out in is based on equilibrium reaction and if sent to U R Stream S O If significant amounts of hydrogen are included, the reforming process may adversely affect the overall yield of hydrogen.

[0079] Therefore, the demethanation step according to (ii.2) preferably comprises a distillation step from which an overhead stream S comprising CH4 and H2 is obtained. O1 , and further preferably, the demethanation step according to (ii.2) comprises a separation step, wherein S O1 Separated into a H2-rich stream and a CH4-rich stream S O2 , where according to (iii) S O1 or a partial flow thereof, preferably S O2 or a portion thereof as flow S O Enter U R .

[0080] Among them, S O1 Separated into a H2-rich stream and a CH4-rich stream S O2As far as the separation step of the present invention is concerned, there are no particular restrictions as to the suitable unit in which this separation is performed. As an example, the separation can be performed using a pressure swing adsorption unit. Preferably, the H2-rich stream exhibits an H2 content in the range of 90 to 100 vol-%, more preferably in the range of 95 to 100 vol-%. Alternatively, according to the present invention, the H2-rich stream can be suitably separated from the stream S' H combination, in this case, determine the amount of H2 according to (c.1.1) 2P And control the processing unit U according to (c.1.3) P , supply device M E and optionally supply means M R The H 2 content of the H 2 rich stream will be taken into account.

[0081] It is waiting to be sent to U R Stream S O In terms of the composition, preferably 96 to 100 volume-% S O More preferably, 97 to 100 vol-%, more preferably 98 to 100 vol-%, more preferably 99 to 100 vol-%, more preferably 99.5 to 100 vol-%, more preferably 99.9 to 100 vol-% of S O Composed of CH4. Further preferably, 0 to 4 volume % of S O More preferably, 0 to 3 vol-%, more preferably 0 to 2 vol-%, more preferably 0 to 1 vol-%, more preferably 0 to 0.5 vol-%, more preferably 0 to 0.1 vol-% of S O Composed of H2.

[0082] The C2 components from which methane has been removed are then preferably sent to a C2 splitter which produces ethylene as a light product and ethane as a heavy product. 5+ The stream is routed to a depropanizer from which the C3 components are obtained as overheads and the C4 to C5 components are obtained as bottoms. 5+ The C3 product may be hydrotreated to remove C3 acetylenes and dienes before being fed to a C3 splitter where it is separated into propylene at the top and propane at the bottom. 5+ The stream is fed to a debutanizer from which the C4 components are obtained at the top and the remaining C 5+ The components are obtained as the bottom distillate. 5+ Both streams are separately hydrotreated to remove undesirable acetylenes and dienes.

[0083] In a conventional front-end deethanizer sequence, the C1 to C5+ Component cracking gas S C First enters the deethanizer. The light fraction leaving the deethanizer consists of C2 and C1 components and any hydrogen. These light fractions are usually fed to a demethanizer where hydrogen and C1 are removed as light components and C2 components are removed as heavy components. The C2 stream leaving the bottom of the demethanizer can be fed to an acetylene converter and then to a C2 separator which produces ethylene as a light product and ethane as a heavy product. The C3 to C1 stream leaving the deethanizer is usually fed to a demethanizer where hydrogen and C1 are removed as light components and C2 components are removed as heavy components. 5+ The heavy fraction consisting of the components is routed to a depropanizer, from which the C3 components are obtained as overheads and the C4 to C4 components are obtained as bottoms. 5+ The C3 product is typically fed to a C3 splitter where it is separated into propylene at the top and propane at the bottom, while the C4 to C 5+ The stream is fed to a debutanizer which produces C4 compounds at the top, with the remainder leaving as bottoms to be used for gasoline or recycled as feed to the cracking process. As with the front-end demethanizer sequence, C3, C4 and C 5+ The stream is separately hydrotreated to remove undesirable acetylenes and dienes.

[0084] In a conventional front-end depropanizer sequence, hydrocarbons (C1 to C 5+ The quenched and acid-free gas first enters the depropanizer. The heavy fractions leaving the depropanizer range from C4 to C 5+ Component composition. Usually these are sent to debutanizer, in which C4 component and lighter material are extracted on the top, and the remainder of wherein feed leaves as tower bottoms, and these tower bottoms can be used for gasoline or other chemical recovery. These streams can be hydrotreated separately to remove undesirable acetylene and dienes. The light fraction containing C1 to C3 component of depropanizer can be fed to acetylene converter and then fed to demethanizer system, in which C1 component and any remaining hydrogen are usually removed as tower overhead. Usually the heavy fraction containing C2 and C3 component leaving demethanizer system is sent to deethanizer, wherein C2 component is removed from the top and C3 compound is obtained as tower bottoms. And then usually C2 component is fed to C2 separator, and this separator produces ethylene as light product and ethane as heavy product. The C3 stream is fed to a C3 splitter which separates the C3 materials, sending propylene to the top and propane to the bottom.

[0085] As with the front-end demethanizer sequence, the saturated C2 hydrocarbons and / or saturated C3 hydrocarbons obtained in the front-end deethanizer sequence or the front-end depropanizer sequence, or a partial stream thereof, can be recycled as feed to the cracking process.

[0086] Reforming unit U R

[0087] According to the present invention, the light hydrocarbon waste gas stream S is O Sent to the reforming unit U according to (4) R in which it is subjected to reforming in the reforming unit and wherein a product gas stream S is obtained from said reforming R .

[0088] Preferably, the reforming unit U R The method comprises one or more of an autothermal reforming (ATR) unit, a steam reforming (STR) unit and a partial oxidation (POX) unit, preferably one or more of an autothermal reforming (ATR) unit and a steam reforming (STR) unit.

[0089] Steam reforming is a catalytic reaction suitable for converting hydrocarbons into synthesis gas containing hydrogen and carbon monoxide in the presence of steam. The reaction is typically carried out in a multi-tubular reactor that is usually filled with a catalyst. Most commercial catalysts are nickel-based and utilize supports such as aluminum oxide and / or zirconium oxide. Generally, it is desirable that the raw material does not contain sulfur compounds because these compounds are strong poisons for the catalysts used in steam reforming. For catalysts, process parameters and reaction settings including reactor types, reference may be made, for example, to Ullmann's Encyclopedia of Industrial Chemistry, Hydrogen, 2. Production, 1.3 Catalytic reforming of Hydrocarbons, DOI: 10.1002 / 14356007.o13_o03 or Ullmann's Encyclopedia of Industrial Chemistry, Gas Production, 2. Processes, 1. Steam Reforming of Natural Gas and other Hydrocarbons, DOI: 10.1002 / 14356007.o12_o01. O Steam reforming of methane, the main component of the gas, proceeds according to the following main reactions:

[0090] CH4+H2O→CO+3H2

[0091] The reaction is endothermic and requires high temperatures, typically above 800°C, at the reactor outlet. The methane reforming process is preferably carried out in tubes filled with catalyst within a combustion furnace. Suitably, steam is used in excess of the stoichiometric requirements of the reaction in order to prevent coking of the catalyst.

[0092] Partial oxidation is a non-catalytic process in which a substoichiometric amount of oxygen is allowed to react with a carbonaceous material like natural gas, liquid feeds (eg, fuel oil, gas oil), and / or coal at high temperatures to produce a synthesis gas containing hydrogen and carbon monoxide. For process parameters and reaction setup including reactor type, reference is made, for example, to Ullmann's Encyclopedia of Industrial Chemistry, Hydrogen, 2. Production, 1.2 Gasification of Coal and Hydrocarbons, DOI: 10.1002 / 14356007.o13_o03 or Ullmann's Encyclopedia of Industrial Chemistry, Gas Production, 2. Processes, 2. Noncatalytic Partial Oxidation and Special Gasification Processes for Higher-Boiling Hydrocarbons, DOI: 10.1002 / 14356007.o12_o01. O The partial oxidation of methane, the main component in the reaction, proceeds according to the following main reactions:

[0093] 2CH4+O2→2CO+4H2

[0094] CO2+H2→CO+H2O

[0095] For these partial oxidation reactions, it is preferred to convert the stream S O The syngas is mixed with air, oxygen-enriched air and / or molecular oxygen and introduced into a partial oxidation reactor at a generally high temperature of at least 1200° C. and reacted thermally in the absence of a catalyst. Typically, the temperature of the syngas leaving the partial oxidation reactor is in the range of 1200° C. to 1300° C. or higher. In principle, the partial oxidation reaction can be carried out without the addition of any steam.

[0096] Autothermal reforming is a variant of the partial oxidation process described above, using oxygen and steam and optionally carbon dioxide with the O The reaction of methane in the stream to form synthesis gas containing hydrogen and carbon monoxide. O Contains any hydrocarbon higher than methane, then can be pre-reformed. This avoids the potential problem of olefin formation from higher hydrocarbons in the ATR and reduces the possibility of coking on the main reformer catalyst. In the pre-reformer (typically a steam reformer), all higher hydrocarbons (C 2+ ) is converted into a mixture of methane, hydrogen, carbon monoxide and carbon dioxide according to the following reaction:

[0097] C n H m +n H2O→n CO+(n+m / 2)H2(n≥2)

[0098] Typically, for methane, the above reactions also occur in autothermal reforming along with the following reaction

[0099] 4CH4+O2+2H2O→10H2+4CO

[0100] In autothermal reforming, a catalyst is preferably used to allow reforming to occur at lower temperatures than in partial oxidation processes. A suitable amount of steam is typically used to prevent coking of the catalyst. For information on catalysts, process parameters, and reaction setup including reactor types, reference may be made, for example, to Ullmann's Encyclopedia of Industrial Chemistry, Hydrogen, 2. Production, 1.3 Catalytic reforming of Hydrocarbons, DOI: 10.1002 / 14356007.o13_o03 or Ullmann's Encyclopedia of Industrial Chemistry, Gas Production, 2. Processes, 1. Steam Reforming of Natural Gas and other Hydrocarbons, 1.5 Autothermal Catalytic Reforming, DOI: 10.1002 / 14356007.o12_o01. Typically, for an autothermal reforming process, the feed stream S is heated to 100°C. O For this purpose, the feed stream S OThe vaporizer is typically heated by hot combustion gases supplied from a burner, so that the vaporizer can convert the feed stream S O and the water directed therethrough is vaporized. The vaporized feed stream, steam, and air are then mixed using a mixing unit, and the resulting mixture is introduced into an autothermal reformer. Preferably, the main components of the autothermal reformer are a burner, a combustion chamber, and a catalyst bed contained within a refractory-lined pressure shell. The catalyst is typically nickel-based. In the autothermal reformer, partial combustion of the hydrocarbon feed stream by a substoichiometric amount of oxygen is followed by a reaction of the partially burned feedstock with steam in a fixed bed of steam reforming catalyst. Due to the high temperature, the reaction of methane with steam also occurs to a certain extent in the combustion chamber. The steam reforming reaction may be accompanied by a water-gas shift reaction. Typically, synthesis gas leaves the autothermal reformer with an outlet temperature in the range of 850°C to 1100°C and an outlet pressure of up to 100 bar.

[0101] Preferably, from the reforming unit U R The obtained product gas stream S R A molar ratio CO:H2 in the range of 1:2 to 1:3 was exhibited.

[0102] Optionally, downstream of the reforming unit and the processing unit U P Upstream of the controllable supply device M according to (6) is arranged R Preferably, the supply device M R For the reformer unit U R The obtained product gas stream is split into two or more gas streams, preferably having the same gas flow as that from the reforming unit U R The obtained product gas stream has the same chemical composition as the gas stream S' R and flow S" R Then one of these streams S' R Sent to downstream processing unit U P Suitable supply device M R These include, for example, controllable valves.

[0103] Processing unit U P

[0104] According to the present invention, the stream S R or its partial flow S' R In the controllable processing unit U P Properly processed, the controllable processing unit obtains R or S' R Compared with H2-rich stream S H .

[0105] Generally, regarding the processing unit U PThere is no particular limitation on the specific setting of , provided that a suitable gas flow S can be obtained. H Preferably, the processing unit U according to (5) P Including gas separation unit U PG and water-gas shift reaction unit U PW One or more of .

[0106] U including gas separation unit P

[0107] According to the first embodiment of the present invention, the processing unit U P Including gas separation unit U PG , the flow S R or stream S' R is sent to the gas separation unit, and a stream S is obtained from the gas separation unit H and CO-rich stream S CO For stream S R or stream S' R This gas separation preferably first removes high boiling point impurities such as water, carbon dioxide and / or optionally C 2+ Alkanes (if present). C 2+ The separation of alkanes can be achieved by condensation or distillation processes. The separation of water can be achieved by, for example, washing with glycols. The separation of CO2 can be achieved by gas scrubbing, for example, by acid gas removal. The mixture comprising hydrogen, carbon dioxide and methane can be separated, for example, by cryogenic processes, pressure swing absorption and / or methane scrubbing. Two or more methods can be combined to increase the purity of the hydrogen obtained. For hydrogen purification processes, reference can be made to, for example, Ullmann's Encyclopedia of Industrial Chemistry, Hydrogen, 3. Purification, DOI: 10.1002 / 14356007.o13_o04.

[0108] Therefore, the present invention relates to a method,

[0109] The process stage (v) includes

[0110] (v) The stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0111] The process stage (v') includes

[0112] (v') the stream S R Or the stream S'R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0113] The process stage (v") includes

[0114] (v") R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO .

[0115] If, according to the process according to the invention, a CO-rich stream S is obtained CO , then it is preferred to flow S CO For another purpose. Preferably, the other purpose includes using S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0116] U including water gas shift reaction unit and gas separation unit P

[0117] According to the second embodiment of the present invention, the processing unit U P Including gas separation unit U PG and the water-gas shift reaction unit U upstream thereof PW According to this embodiment,

[0118] Process stage (v) preferably comprises

[0119] (v.1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0120] (v.2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0121] The process stage (v') includes

[0122] (v'.1) the stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0123] (v'.2) the stream SW Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0124] The process stage (v") includes

[0125] (v".1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0126] (v".2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 .

[0127] According to this second embodiment, the R or stream S' R The carbon monoxide in the stream S is at least partially converted into additional hydrogen. R or stream S' R CO in the stream reacts with H2O to produce H2 and CO2. R or stream S' R In comparison, the shifted product stream obtained from the water-gas shift process has a higher concentration of H2 and CO2. Preferably, the water-gas shift reaction uses steam to convert CO2 and produce H2 according to the following reaction:

[0128] CO+H2O→CO2+H2

[0129] The water-gas shift reaction is mildly exothermic and a favorable balance is achieved on the CO2 and H2 sides at low temperatures. Generally, it is convenient to operate a single shift process at high temperature to produce a shifted gas mixture with a low CO content (typically <10 mol-% based on dry gas). In order to achieve acceptable conversion rates, iron-containing catalysts have found widespread use as so-called high-temperature shift (HTS) catalysts. These catalysts are typically provided as a fixed bed of particles in axial or radial flow shift converters that are operated at inlet temperatures above 340°C in order to achieve acceptable activity. Alternatively, cobalt-molybdenum catalysts that can be used in so-called "sour shift" processes can be operated at inlet temperatures above 220°C. In addition to being a reactant, steam also helps to shift the equilibrium of the water-gas shift reaction towards H2, controlling the temperature increase of the exothermic water-gas shift reaction, which, if not controlled, can deactivate the catalyst. Steam is also required to prevent coking on the catalyst surface, which also deactivates the catalyst. Typically, the water gas shift process uses two reactors in series to perform a high temperature shift (HTS) followed by a low temperature shift (LTS). Steam is added to the gas fed to the first reactor, stream S R or stream S' R The gas from the outlet of the first reactor is preferably cooled to the desired shift inlet temperature by adding more steam, and the cooled gas is then fed to the second reactor. From this second reactor, a shifted product stream (stream S) comprising additional hydrogen and carbon dioxide is obtained. W ). Subsequently, according to (v.2), the product stream S contained in the transformation is separated W to produce a hydrogen product stream S H and CO2-rich stream S CO2 Remaining carbon monoxide or other impurities in the shifted product stream, respectively in the hydrogen product stream, can be separated by gas separation as described above in the context of the first embodiment.

[0130] If done in the context of the first embodiment, from the reformed stream S R or S' R or from the product stream S of the conversion according to the second embodiment W Separating carbon dioxide from natural gas has the advantage that CO₂ can be separated from gas streams with significantly higher CO₂ concentrations than flue gas streams derived from natural gas combustion. This results in the advantage that smaller gas volumes can be processed to capture the emitted CO₂. Processing smaller gas volumes and higher CO₂ concentrations reduces the energy input required for CO₂ capture.

[0131] If, according to the method of the invention, a stream S rich in CO2 is obtained CO2, then it is preferred to flow S CO2 For another purpose. Preferably, the other purpose includes using S CO2 , including one or more of carbon capture and storage (CCS) and carbon capture and utilization (CCU).

[0132] Typically, carbon capture involves removing carbon from a stream S R or S' R or from the transformed product stream S W CO2 can be separated from the atmosphere. This can include capturing the CO2 in a liquid solvent. Subsequently, the capture medium needs to be regenerated without releasing the CO2 into the atmosphere. Typically, the liquid solvent used for CO2 capture is a solution of an inorganic or organic base. When the acid gas is dissolved in the solvent, ion pairs are formed with the base. The solvent can be regenerated by expanding to a lower pressure or by stripping, the ionic species reacting to form acid gas and / or stripping away with steam. After the regeneration process, the solvent can be reused.

[0133] Typically, if CO2 constitutes only a small percentage of a large volume gas stream to be processed (such as flue gas), it is wasteful and expensive to process the large flow stream to recover a small portion of it as CO2. Unlike flue gas, the reformed stream S R or S' R and / or transformed product stream S W are streams that exhibit high CO2 concentrations, and therefore, capturing CO2 from these streams is more efficient given the energy input for CO2 separation.

[0134] Suitably, the absorption liquid medium is an aqueous solution of at least one amine having a total amine content in the range of 30 to 70 wt.-%, preferably in the range of 40 to 60 wt.-%. Preferably, the amine is selected from monoethanolamine (MEA), methylaminopropylamine (MAPA), piperazine, diethanolamine (DEA), triethanolamine (TEA), diethylethanolamine (DEEA), diisopropylamine (DIPA), aminoethoxyethanol (AEE), dimethylaminopropanol (DIMAP), methyldiethanolamine (MDEA), methyldiisopropanolamine (MDIPA), 2-amino-1-butanol (2-AB), or mixtures thereof. Preferred absorption media contain at least one alkanolamine having 4 to 12 carbon atoms. Particularly preferred absorption media contain at least one tertiary alkanolamine and an activator, preferably in the form of a primary or secondary amine. Preferred activators are saturated 5- to 7-membered heterocyclic compounds having at least one NH group and, if appropriate, additional heteroatoms selected from oxygen and nitrogen atoms in the ring. For example, suitable activators are selected from piperazine, 1-methylpiperazine, 2-methylpiperazine, 1-aminoethylpiperazine, morpholine and piperidine. Other preferred activators are selected from methylaminopropylamine, 2-amino-1-butanol or aminoethoxyethanol.

[0135] In order to avoid problems in downstream processes such as CCS or CCU, the obtained aqueous (i.e. wet) CO2-containing stream is preferably treated to remove H2O. Therefore, it is preferred to make the CO2-containing stream, in particular S CO2 The dry stream containing carbon dioxide is subjected to a drying step to obtain a dry stream containing carbon dioxide. Typically, this drying step is carried out using at least one container containing at least one desiccant for adsorbing H2O from the wet stream containing carbon dioxide. For this purpose, the wet stream containing carbon dioxide is preferably passed through the desiccant in one direction. Subsequently, the desiccant is preferably regenerated. For desiccant regeneration, the flow through the desiccant bed is preferably carried out in the opposite direction. A preferred arrangement includes two dryers, one of which is in operating mode and the other dryer is in standby mode and regeneration mode, respectively. Preferably, the dry stream containing carbon dioxide is suitably liquefied or reaches its supercritical stage and is subsequently subjected to carbon dioxide sequestration. Carbon dioxide sequestration of CO2 derived from renewable resources is a so-called "negative emission technology". Negative emission technology removes (i.e. captures) carbon dioxide equivalents from the atmosphere by long-term sequestration (i.e. storage) of carbon dioxide. In other words, CO2 can be removed from the atmosphere by carbon dioxide sequestration. These negative emission technologies aim to curb the current level of the greenhouse gas carbon dioxide and its projected growth rate. Therefore, negative emission technologies can include enhanced carbon sinks that provide long-term storage of the removed carbon dioxide.

[0136] For example, carbon dioxide sequestration, also known as "carbon capture and storage" (CCS) can involve "geological carbon sequestration" such as hydrodynamic trapping, solution trapping, or mineralized trapping. Geological carbon sequestration involves storing a captured and dried stream containing carbon dioxide below the surface, such as by pumping it into pores in underground geological formations or into deep-sea layers. Other examples of negative emissions technologies include terrestrial carbon sequestration, coastal blue carbon capture, and mineral carbonation of carbon dioxide. Typically, terrestrial carbon sequestration requires increasing forest cover and the carbon content of agricultural soils, while coastal blue carbon sequestration focuses on similar processes in tidal or wetland areas. Mineral carbonation involves bringing atmospheric or captured carbon dioxide into contact with basalt or ultramafic rocks to undergo a chemical reaction to convert the carbon dioxide into a chemical solid.

[0137] Preferably, according to the present invention, the dry stream containing carbon dioxide is subjected to carbon dioxide utilization (CCU). Carbon dioxide utilization (also referred to as "carbon dioxide capture and utilization") is intended to recycle the captured carbon dioxide to convert it into useful solid or liquid materials, such as methanol, olefins, plastics, carbon fiber, biomass such as biofuels ("bioenergy carbon capture and storage"), carbon-based chemicals, etc. Bioenergy carbon capture requires capturing the dry stream containing carbon dioxide and using the captured carbon dioxide in the biomass used in the fuel. In the case where CO2 is derived from renewable resources, carbon dioxide capture and utilization is also an example of "negative emissions technology".

[0138] Methods for controlling the process

[0139] According to the method of the invention, the process carried out in the integrated device is controlled in a suitable manner so that the heat generated by the external and sustainable heat source H EXT-S If the amount of heat supplied is too low, C The heat requirement E of the hydrocarbon conversion process carried out in UC This can be achieved at least in part by using hydrogen as U C The heat source is satisfied, the hydrogen being contained in a gas stream which in turn is suitably taken from the unit U C of exhaust gas flow.

[0140] According to a further aspect of the present invention, the method comprises determining in unit U C The heat requirement E for hydrocarbon conversion in UC . Depends on e.g. being sent to U C At least one hydrocarbon feed stream S F The specific chemical composition and / or C The specific reaction conditions of the hydrocarbon conversion process carried out in the process, said composition and / or conditions may vary over time during the hydrocarbon conversion process, said heat requirement E UC It can also change with time. Further, as shown above, it can be provided by a sustainable heat source H outside the device. EXT-S The amount of heat provided may vary over time, for example due to general supply issues such as purchasing a suitable heat source H EXT-S The costs involved, or supply interruptions due to maintenance intervals. All of these different possible influences can be handled by the control method of the invention, which makes the process highly flexible.

[0141] According to the method of the present invention, according to (a), U is appropriately determined C Calorie requirement E UC This determination can be performed continuously or semi-continuously at corresponding intervals depending on the above-mentioned CThe hydrocarbon conversion process in the present invention has a variable parameter that affects the process. Further according to the method of the present invention, according to (b), from one or more external sustainable heat sources H EXT-S Available for U C The amount of calories E EXT-S Continuously or semi-continuously determined at corresponding intervals, these corresponding intervals depend on the above-mentioned C The hydrocarbon conversion process in the present invention has a variable parameter that affects the hydrocarbon conversion process. As E determined according to (a) and (b) UC and E EXT-S As a result of the value of , at each desired time point during the hydrocarbon process, ΔE = E UC –E EXT The value of (i.e., by direct calculation) can be known from E EXT-S Can the caloric requirements be met? UC .

[0142] ΔE>0

[0143] If the determination of ΔE as described above yields a positive value (ΔE>0), then at least a certain amount of additional internal device heat is required to properly meet U C The energy demand of the hydrocarbon conversion process and thus maintain U C Medium hydrocarbon conversion process.

[0144] In particular, according to the invention, the amount of hydrogen H is then determined 2N , this amount of hydrogen needs to be provided to M as a heat source H In order to generate heat of the amount ΔE. Still further, according to the present invention, the amount of hydrogen H is then determined. 2P , that is, you can R and U P The maximum amount of H2 produced in the stream S H The maximum amount of H2 achieved in 2P , you can H E H2P The amount of calories.

[0145] ΔE>0 and ΔH>0

[0146] If the value H 2N and H 2P The comparison of ΔH=H 2N –H 2P Greater than zero (i.e., the heat demand ΔE cannot be determined by H alone) 2P The conclusion that the maximum amount H is satisfied is particularly preferred. 2P Via stream S' H Send to M H Appropriately control the supply device ME , processing unit U P and optionally supply means M R To maximize H 2P Via S' H Provided to M H , so that it can be H E H2P It should be noted that, also in the case of ΔH>0, it may not be necessary to set the maximum amount H 2P Send to M H In the case where other internal sustainable heat sources may be available, these other internal sustainable heat sources may be fed to the M H H can be appropriately replaced in the middle 2P However, the maximum amount of H 2P Send to M H It is usually particularly preferred.

[0147] According to this scenario, it depends on whether the device includes the device M R , the process includes

[0148] (iv) Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100;

[0149] (v) The stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0150] (vi) Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where y = 100;

[0151] (vii) will be from M E The obtained stream S' H As H INT Send to M H middle.

[0152] As mentioned above, since H 2P To meet the energy demand ΔE, at least one additional heat source must be sent to M HIn order to generate sufficient heat to maintain the hydrocarbon conversion process. Although it is generally conceivable that the at least one additional heat source may be available internally to the plant, the at least one additional heat source is typically provided via a fossil heat source external to the plant. Therefore, the process preferably further comprises, following (iv), (v), (vi) and (vii) above,

[0153] (viii) the external fossil heat source H of the one or more devices EXT-F At least one of them is passed through M E Send to M H In the amount sufficient to H Production (ΔE-E H2P ) calories.

[0154] If according to the above, ΔE>0 and ΔH>0, the processing unit U P Including gas separation unit U PG , then the process stage (v) includes

[0155] (v) The stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0156] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0157] Within the possible limits of the respective gas separation method applied in (v), the flow S can be controlled H composition, so that it can be passed through S' H Provide the maximum possible amount of H2 to M H .

[0158] If the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , then the process stage (v) includes

[0159] (v.1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0160] (v.2) The stream S W Sent to the gas separation unit UPG In, get S H and CO2-rich stream S CO2 .

[0161] In this case, it is preferred to convert the stream S CO2 or a portion thereof for another use, wherein the other use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilization (CCU).

[0162] Within the possible limitations of the corresponding water-gas shift reaction and the corresponding gas separation process applied in (v), the flow S can be controlled H composition, so that it can be passed through S' H Provide the maximum possible amount of H2 to M H .

[0163] Then according to (vi) make P The obtained hydrogen-rich stream S H Through the supply device M E To obtain S H y volume-% flow S' H , where y=100.

[0164] ΔE>0 and ΔH≤0

[0165] If the value H 2N and H 2P The comparison of ΔH=H 2N –H 2P Less than or equal to zero (ie, the heat demand ΔE can be determined solely by H 2P If the conclusion is satisfied, the supply device M is appropriately controlled. E , processing unit U P and optionally supply means M E Through S' H To M H Provide the necessary amount of H2 inside the device so that it can H ΔE is produced in the process.

[0166] According to this scenario, it depends on whether the device includes the device M R , the process includes

[0167] (iv') Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0 <x≤100;

[0168] (v') the stream S Ror if (iv) is carried out, then the stream S’ R is sent to U P wherein S is obtained H ;

[0169] (vi’) making the stream S obtained from U P pass through M H to obtain a stream S’ which is y volume-% of S E where 0 < y ≤ 100; H H E H

[0170] (vii’) sending the stream S’ obtained from M E as H H to M INT H H R

[0171] Since for ΔE > 0, H2 contained in S must be provided, the stream S’ obtained from the device M according to process step (iv’) H (if it exists) needs to be x volume-% of S R where 0 < x ≤ 100, i.e., x must not be zero. The exact value of x will depend on the one hand on the value of ΔE and additionally on the parameters at which the processing unit U R (if it exists) needs to be x volume-% of S R where 0 < x ≤ 100, i.e., x must not be zero. The exact value of x will depend on the one hand on the value of ΔE and additionally on the parameters at which the processing unit U P and the device M E can or should operate, i.e., the stream S’ R must be provided to U P in order to achieve a specific stream S H which is then sent to the device M E to obtain the final desired stream S’ H to be provided to the device M<e H . In particular, the stream S R can be made to pass through M R without any change in composition and / or volume, in which case x = 100. However, also in this case, the presence of M R is not useless because it can be used to separate the stream S” whenever the overall control requires x < 100 R for which case the process stage (iv’) includes

[0172] (iv’) making the S obtained from U R pass through M R to obtain a stream S’ which is x volume-% of S R where 0 < x < 100, and a stream S” which is (100 - x) volume-% of S R R R R ​​​.

[0173] Preferably, stream S" R for another purpose, wherein said other purpose more preferably comprises the use of S" R As synthesis gas, more preferably including the use of S" R The synthesis gas can be used to produce one or more of methanol, liquid fuels, hydrocarbons, lubricants, oxo alcohols and ammonia.

[0174] Then according to (v') R The corresponding obtained flow S' R , or flow S R Sent to processing unit U P , a hydrogen-rich stream S is obtained from the process unit H Then appropriately control the U P One or more process stages are carried out in such a way that the stream S finally obtained H Contains sufficient hydrogen to H ΔE is produced in the process.

[0175] If according to the above, ΔE>0 and H≤0, the processing unit U P Including gas separation unit U PG , then the process stage (v) includes

[0176] (v') the stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0177] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0178] Within the possible limits of the respective gas separation method applied in (v'), the flow S can be controlled H The composition of the gas is such that its hydrogen content is sufficient to H ΔE is produced in the process.

[0179] If the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , then the process stage (v') includes (v'.1) converting the stream S R Or the stream S' R Sent to the water gas shift reaction unit U PWIn this process, a stream S containing CO2 and H2 is obtained W ;

[0180] (v’.2) This stream S W is sent to the gas separation unit U PG to obtain S H and a stream S rich in CO2 CO2 CO2 .

[0181] In this case, it is preferred that the stream S CO2 or a part thereof is used for another purpose, where the said another purpose preferably includes one or more of carbon capture and storage (CCS) and carbon capture and utilization (CCU).

[0182] Within the possible limitations of the corresponding water-gas shift reaction and the corresponding gas separation method applied in (v’), the composition of the stream S H can be controlled such that its hydrogen content is sufficient to generate ΔE in M H .

[0183] Then, according to (vi’), the hydrogen-rich stream S P obtained from U H is passed through the supply device M E to obtain a stream S' H which is y volume-% of S H , where 0 < y ≤ 100. Since ΔE to be generated in M H is greater than zero, y must be greater than zero. The exact value of y will depend on the amount of hydrogen required to generate ΔE in M [[ID=A1]] H . According to this scenario, the entire stream S H can be used as the stream S’ H to be supplied to M H , in which case y = 100. If S H contains more hydrogen than required to generate ΔE in M H , it is preferred that the device M E is controlled in such a way that the process stage (vi’) includes

[0184] (vi’) passing the stream S P obtained from U H through M E to obtain a stream S' H which is y volume-% of S H , where 0 < y < 100, and a stream S” H which is (100 - y) volume-% of S H .

[0185] Preferably, according to the present invention, 60 to 100 vol-%, more preferably 70 to 100 vol-%, more preferably 80 to 100 vol-%, more preferably 90 to 100 vol-%, more preferably 95 to 100 vol-%, more preferably 99 to 100 vol-% of the H2-rich stream S H Composed of H2.

[0186] In this case, it is preferred that the flow S" H or a portion thereof for another purpose, wherein the other purpose preferably comprises the use of S" H As a U C More preferably, in the heat source of one or more units other than U C In one or more units other than H Or a partial stream thereof is used as a heat source for one or more endothermic processes carried out at a temperature of at least 800° C., for steam generation or generally for combustion.

[0187] If the flow S H Send to M E and there separated into H Stream S' H , and flow S" H , the separation can be performed, for example, using one or more controllable valves.

[0188] ΔE≤0

[0189] If the determination of ΔE yields a non-positive value (ΔE ≤ 0), no additional internal heating of the device is required to maintain U C In this scenario, the processing unit U P , supply device M E and optionally supply means M R is controlled in such a way that H2 is not passed through S H Send to M H middle.

[0190] According to this scenario, it depends on whether the device includes the device M R , the process includes

[0191] (iv") Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x≤100;

[0192] (v") R Or if (iv') is performed and x≠0, then the stream S'R Send to U P In, get S H ;

[0193] (vi”) Make the flow S H If from U P If you get it, through M E , and get S H 100 vol-% flow S" H ;

[0194] (vii”) From M E Remove the stream S from H .

[0195] Therefore, it is possible that if x=0, there is no R Get stream S' (if it exists) R , the flow will be sent to the processing unit U P In this case, make the entire stream S R By M R To obtain S R Same stream S" R Alternatively, it is possible that if x = 100, then there is no R Get stream S (if any) R , the flow will be from S R In this case, the entire flow S R By M R To obtain S R The same stream S' R . For obtaining stream S" R In all cases, process stage (iv") includes

[0196] (iv) R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x<100, and obtained as S R (100-x) volume-% flow S" R ,

[0197] Preferably, flow S" R for another purpose, wherein said other purpose more preferably comprises the use of S" R As synthesis gas, more preferably including the use of S" R The synthesis gas can be used to produce one or more of methanol, liquid fuels, hydrocarbons, lubricants, oxo alcohols and ammonia.

[0198] If x≠0, then according to (v') R The corresponding obtained flow S' R , or flow S R Sent to processing unit U P , a hydrogen-rich stream S is obtained from the process unit H .

[0199] If according to the first embodiment, the processing unit U P Including gas separation unit U PG , then the process stage (v') for x≠0 includes

[0200] (v') the stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0201] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0202] If according to the above, ΔE≤0 In the case of processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , then the process stage (v") for x≠0 includes

[0203] (v".1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0204] (v".2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 .

[0205] In this case, it is preferred to convert the stream S CO2 or a portion thereof for further use, wherein the further use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilization (CCU).

[0206] Further, for x≠0, then from U P The obtained flow SH Sent to supply device M E . Since in addition to H EXT In addition, it is not necessary to include H The hydrogen in the UC , so there is no E To M H Supply flow S' H , and with the entire stream S H As a stream S" H Get the way to control the device M E In this case, the preferred flow is S" H or a portion thereof for another purpose, wherein the other purpose more preferably comprises the use of S" H As a U C More preferably, in the heat source of one or more units other than U C In one or more units other than H Or a partial stream thereof is used as a heat source for one or more endothermic processes carried out at a temperature of at least 800° C., for steam generation or generally for combustion.

[0207] Preferably, the method for controlling a process according to the present invention utilizes a computer-supported control system, by which one or more of the above-mentioned parameters are determined, and based on the one or more parameters, one or more of the above-mentioned units and / or devices and / or processes are controlled in order to achieve the desired process design.

[0208] Still further, the present invention relates to an integrated production device comprising

[0209] (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , wherein the supply device M F with U C Connect to the hydrocarbon feed stream S F At least one of them is sent to U C In, from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ;

[0210] (2) The unit U C The unit comprises a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2;

[0211] (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external sustainable fossil heat sources H EXT-F , and one or more internal heat sources H INT , the internal heat source H of the device INT comprising H2, wherein the supply means M E with U C Connect the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ;

[0212] (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R , where U R Arranged in U C Downstream and connected with U C Connect to S O Send to U R middle;

[0213] (5) Controllable processing unit U P , used for processing S R To generate S R Compared with H2-rich stream S H , where U P Arranged in U R Downstream and connected with U R Connect to S R Send to U P middle;

[0214] (6) and optionally a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , where M R Arranged in U R Downstream and U P Upstream, and U R Connect to S R Send to M R and with U P Connect to S' R or S" R Send to U P middle.

[0215] Preferably, the unit U for heat-consuming hydrocarbon conversion C Including lysis unit U CC , preferably a thermal cracking unit, more preferably a steam cracking unit. More preferably, the unit U C Further comprising a method for treating the cracking gas stream S C Separation unit U S , where U S comprising at least one demethanation unit, wherein a stream S is obtained from said demethanation unit O , and where from U S One or more product streams are obtained.

[0216] According to the first embodiment, the unit U P Including for S R or S' R Get Stream S H and CO-rich stream S CO Gas separation unit U PG According to the second embodiment, the unit U P Including for S R or S' R Obtain a stream S containing CO2 and H2 W Water-gas shift reaction unit U PW , and further comprising arranging in U PW Downstream for S W Get the stream S H and CO2-rich stream S CO2 Gas separation unit U PG .

[0217] Preferably, in another embodiment, the integrated production equipment includes a method for converting H2 into H Send to M H The device preferably allows the processing unit U to P The obtained flow S H The additional heat is at least partially provided by the heat source H2 in .

[0218] Furthermore, the present invention also relates to the use of the integrated production device as described above for carrying out the method as described above.

[0219] The present invention is further illustrated by the following group of examples and the combination of examples obtained by the dependencies and back-references as shown. In particular, it should be noted that in each case where a series of examples is mentioned, for example, in the context of a term such as "a method as described in any one of Examples 1 to 4", each embodiment in this series is intended to be clearly disclosed to the skilled person, that is, the wording of this term should be understood by the skilled person as synonymous with "a method as described in any one of Examples 1, 2, 3 and 4". Further, it should be clearly pointed out that the following group of examples represents a suitable structural part of the general description of the preferred aspects of the present invention, and therefore appropriately supports but does not represent the claims of the present invention.

[0220] 1. A method for controlling a process carried out in an integrated production facility, wherein the integrated production facility comprises

[0221] (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ;

[0222] (2) The unit U C The unit comprises a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2;

[0223] (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT ——The internal heat source H of the equipment INT Including H2, for the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ;

[0224] (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R ;

[0225] (5) Controllable processing unit U P , used for processing S R or its partial flow S' R To obtain S R or S' R Compared with H2-rich stream S H ;

[0226] (6) and optionally includes a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , and is used to convert S' R Send to U P middle;

[0227] The process includes

[0228] (i) one or more heat sources according to (3) are removed from M E Send to M H , which is sufficient to H Producing satisfaction U C The heat requirement E for the hydrocarbon conversion UC of calories;

[0229] (ii) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C undergoes hydrocarbon conversion to obtain the one or more product streams S and S O ;

[0230] (iii) S O Send to U R In and make S O in U R After undergoing restructuring, it obtained S R ;

[0231] Wherein the method for controlling the process comprises

[0232] (a) Determine U C The hydrocarbon conversion in M H Provided caloric demand E UC ;

[0233] (b) determining a sustainable heat source H external to the one or more devices EXT-S Available for U C The amount of calories E EXT-S ;

[0234] (c) Determine ΔE = E UC –EEXT-S ,and

[0235] (c.1) If ΔE>0, then

[0236] (c.1.1) Determine H 2N , that is, in M H The amount of H2 required to produce ΔE in

[0237] (c.1.2) Determine H 2P , which is used to H Production volume E H2P The calories in U R and U P can be generated to be included in S H The maximum amount of H2 in

[0238] (c.1.3) Determine ΔH = H 2N –H 2P ;and

[0239] (c.1.3.1) If ΔH > 0, then

[0240] Control the processing unit U P , the supply device M E And optionally the supply device M R , so that H 2P Via S H Send to M H middle;

[0241] The process further comprises

[0242] (iv) Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100;

[0243] (v) The stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0244] (vi) Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where y = 100;

[0245] (vii) will be from M EThe obtained stream S' H As H INT Send to M H middle;

[0246] (viii) the external fossil heat source H of the one or more devices EXT-F At least one of them is passed through M E Send to M H In the amount sufficient to H Production (ΔE-E H2P ) calories;

[0247] (c.1.3.2) If ΔH ≤ 0, then

[0248] Control the processing unit U P , the supply device M E And optionally the supply device M R , so that it will be sufficient to H The amount of H2 produced in ΔE is S H Send to M H middle;

[0249] The process further comprises

[0250] (iv') Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0 <x≤100;

[0251] (v') the stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0252] (vi') Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where 0 <y≤100;

[0253] (vii') will be from M E The obtained stream S' H As H INT Send to M H middle;

[0254] (c.2) If ΔE≤0, then

[0255] Control the processing unit UP , the supply device M E And optionally the supply device M R , so that H2 is not transferred through S H Send to M H middle;

[0256] The process further comprises

[0257] (iv") Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x≤100;

[0258] (v") R Or if (iv') is performed and x≠0, then the stream S' R Send to U P In, get S H ;

[0259] (vi”) Make the flow S H If from U P If you get it, through M E , and get S H 100 vol-% flow S" H ;

[0260] (vii”) From M E Remove the stream S from H .

[0261] 2. The method of embodiment 1, wherein 40 to 100 volume %, preferably 60 to 100 volume %, more preferably 80 to 100 volume %, more preferably 90 to 100 volume %, more preferably 95 to 100 volume % of S O Composed of CH4.

[0262] 3. The method of embodiment 1 or 2, wherein the unit U for heat-consuming hydrocarbon conversion C Including lysis unit U CC , preferably a thermal cracking unit, more preferably a steam cracking unit.

[0263] 4. The method of embodiment 3, wherein U C Further comprising a separation unit U S , wherein according to (ii), the process comprises

[0264] (ii.1) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream SF in U C The cracked gas stream S is obtained by hydrocarbon conversion. C ;

[0265] (ii.2) The cracked gas stream S obtained according to (ii.1) C Sent to a separation unit U comprising at least one demethanation unit S , the stream S is obtained from the demethanation unit O , from U S The one or more product streams S are obtained.

[0266] 5. The process of embodiment 4, wherein the demethanation step according to (ii.2) comprises a distillation step from which an overhead stream S comprising CH4 and H2 is obtained. O1 , and preferably further comprising a separation step, wherein S O1 Separated into a H2-rich stream and a CH4-rich stream S O2 , where according to (iii) S O1 or a partial flow thereof, preferably S O2 or a portion thereof as the flow S O Enter U R .

[0267] 6. The method according to any one of embodiments 1 to 5, preferably any one of embodiments 3 to 5, wherein 96 to 100 volume-%, preferably 98 to 100 volume-%, more preferably 99 to 100 volume-%, more preferably 99.9 to 100 volume-% of S O Composed of CH4.

[0268] 7. The method according to any one of embodiments 1 to 6, preferably embodiment 6, wherein 0 to 4 volume %, preferably 0 to 2 volume %, more preferably 0 to 1 volume %, more preferably 0 to 0.1 volume % of S O Composed of H2.

[0269] 8. The process of any one of embodiments 1 to 7, wherein the one or more hydrocarbon feed streams S F Comprising at least one of: a hydrocarbon feed stream comprising, preferably consisting of, fossil hydrocarbons; a hydrocarbon feed stream comprising, preferably consisting of, recycled hydrocarbons; and a hydrocarbon feed stream comprising, preferably consisting of, biohydrocarbons.

[0270] 9. The method of any one of embodiments 1 to 8, wherein the one or more devices according to (3) are external to a sustainable heat source H EXT-Sincluding one or more of solar energy, wind energy, hydropower, tidal energy, geothermal energy, and biomass energy, ammonia obtained from renewable sources, biomethane, bio-LNG, and H2 obtained from renewable sources, wherein the external fossil heat source H of the device according to (3) EXT-F preferably includes one or more of coal, oil, and natural gas.

[0271] 10. The method according to any one of embodiments 1 to 9, wherein the reforming unit U according to (4) R includes one or more of an autothermal reforming (ATR) unit, a steam reforming (STR) unit, and a partial oxidation (POX) unit, preferably one or more of an autothermal reforming (ATR) unit and a steam reforming (STR) unit.

[0272] 11. The method according to any one of embodiments 1 to 10, wherein in the product gas stream S R obtained from the reforming unit U R the molar ratio of CO:H2 is in the range of 1:2 to 1:3.

[0273] 12. The method according to any one of embodiments 1 to 11, wherein for ΔE>0 and ΔH>0, the process stage (iv) includes (iv) passing S R obtained from U R through M R to obtain a stream S' R which is x volume-% of S R where x = 100.

[0274] 13. The method according to any one of embodiments 1 to 11, wherein for ΔE>0 and ΔH≤0, the process stage (iv') includes (iv') passing S R obtained from U R through M R to obtain a stream S' R which is x volume-% of S R where 0<x<100, and obtaining a stream S'' R which is (100 - x) volume-% of S R .

[0275] 14. The method according to any one of embodiments 1 to 13, wherein for ΔE≤0, the process stage (iv'') includes

[0276] (iv'') passing S R obtained from U R through M R to obtain a stream S' R which is x volume-% of S R where 0≤x<100, and obtaining a stream SR (100-x) volume-% flow S" R .

[0277] 15. The method of embodiment 13 or 14, wherein the stream S" R for another purpose, wherein the other purpose preferably comprises the use of S" R As synthesis gas, more preferably including the use of S" R The synthesis gas can be used to produce one or more of methanol, liquid fuels, hydrocarbons, lubricants, oxo alcohols and ammonia.

[0278] 16. The method of any one of embodiments 1 to 15, wherein the processing unit U according to (5) P Including gas separation unit U PG and water-gas shift reaction unit U PW One or more of .

[0279] 17. The method of embodiment 16, wherein the processing unit U P Including gas separation unit U PG , where for ΔE>0 and ΔH>0, the process stage (v) includes

[0280] (v) The stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0281] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0282] 18. The method of embodiment 16, wherein the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , where for ΔE>0 and ΔH>0, the process stage (v) includes

[0283] (v.1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0284] (v.2) The stream S W Sent to the gas separation unit UPG In, get S H and CO2-rich stream S CO2 ;

[0285] The flow S CO2 Preferably for further use, wherein said further use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilisation (CCU).

[0286] 19. The method of any one of embodiments 16 to 18, wherein the processing unit U P Including gas separation unit U PG , where for ΔE>0 and ΔH≤0, the process stage (v') includes

[0287] (v') the stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0288] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0289] 20. The method of any one of embodiments 16 to 18, wherein the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , where for ΔE>0 and ΔH≤0, the process stage (v') includes

[0290] (v'.1) the stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0291] (v'.2) the stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0292] The flow S CO2 Preferably for further use, wherein said further use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilisation (CCU).

[0293] 21. The method of any one of embodiments 16 to 20, wherein the processing unit U P Including gas separation unit U PG , where for ΔE≤0, the process stage (v") for x≠0 includes

[0294] (v") R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0295] The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

[0296] 22. The method of any one of embodiments 16 to 20, wherein the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , where for ΔE≤0, the process stage (v") for x≠0 includes

[0297] (v".1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0298] (v".2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0299] The flow S CO2 Preferably for further use, wherein said further use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilisation (CCU).

[0300] 23. The process of any one of embodiments 1 to 22, wherein 60 to 100 vol-%, more preferably 70 to 100 vol-%, more preferably 80 to 100 vol-%, more preferably 90 to 100 vol-%, more preferably 95 to 100 vol-%, more preferably 99 to 100 vol-% of the H2-rich stream S H Composed of H2.

[0301] 24. The method according to any one of embodiments 1 to 23, wherein for ΔE>0 and ΔH≤0, the process stage (vi’) comprises

[0302] (vi’) passing the stream S P obtained from U H through M E to obtain a stream S’ that is y volume-% of S H , where 0<y<100, and obtaining a stream S” that is (100 - y) volume-% of S H ; H H H where the stream S”

[0303] or a portion thereof is preferably used for another purpose, where the said another purpose preferably comprises using S” H as a heat source in one or more units other than U C . H H

[0304] 25. The method according to any one of embodiments 1 to 24, wherein for ΔE≤0, the process stage (vii”) for x≠0 comprises using the stream S” H or a portion thereof for another purpose, where the said another purpose preferably comprises using S” H as a heat source in one or more units other than U C . <T

[0305] 26. The method according to any one of embodiments 1 to 25, wherein the method is at least partially computer-implemented.

[0306] 27. The method according to embodiment 26, wherein at least one of E UC , E EXT-S and ΔE is determined by a computer-supported control system, preferably where at least two of E< T UC , E EXT-S and ΔE are determined by a computer-supported control system, more preferably where all three of E UC , E EXT-S and ΔE are determined by a computer-supported control system.

[0307] 28. The method according to embodiment 26 or 27, wherein at least one of M F , U C , M E , U R , U P and M R F C E is determined by a computer-supported control system, preferably where at least one of M F , U C , M E、U R 、U P and M R At least two of the two are determined by a computer-supported control system, more preferably wherein M F 、U C 、M E 、U R 、U P and M R At least three of the items are determined by a computer-supported control system, more preferably wherein M F 、U C 、M E 、U R 、U P and M R At least four of the items are determined by a computer-supported control system, more preferably wherein M F 、U C 、M E 、U R 、U P and M R At least five of the items are determined by a computer-supported control system, more preferably wherein M F 、U C 、M E 、U R 、U P and M R All are determined by the computer-supported control system.

[0308] 29. An integrated production equipment comprising

[0309] (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , wherein the supply device M F with U C Connect to the hydrocarbon feed stream S F At least one of them is sent to U C In, from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ;

[0310] (2) The unit U C The unit comprises a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2;

[0311] (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT , the internal heat source H of the device INT comprising H2, wherein the supply means M E with U C Connect the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ;

[0312] (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R , where U R Arranged in U C Downstream and connected with U C Connect to S O Send to U R middle;

[0313] (5) Controllable processing unit U P , used for processing S R To generate S R Compared with H2-rich stream S H , where U P Arranged in U R Downstream and connected with U R Connect to S R Send to U P middle;

[0314] (6) and optionally a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , where M R Arranged in U R Downstream and U P Upstream, and U R Connect to S R Send to M R and with U P Connect to S' R or S" R Send to U P middle.

[0315] 30. The integrated production plant according to embodiment 29, wherein the unit U for heat-consuming hydrocarbon conversionC Including lysis unit U CC , preferably a thermal cracking unit, more preferably a steam cracking unit.

[0316] 31. The integrated production device of embodiment 30, wherein U C Further comprising a method for treating the cracking gas stream S C Separation unit U S , where U S comprising at least one demethanation unit, wherein the stream S is obtained from said demethanation unit O , and where from U S The one or more product streams are obtained.

[0317] 32. The integrated production facility of any one of embodiments 29 to 31, wherein the reforming unit U R The method comprises one or more of an autothermal reforming (ATR) unit, a steam reforming (STR) unit and a partial oxidation (POX) unit, preferably one or more of an autothermal reforming (ATR) unit and a steam reforming (STR) unit.

[0318] 33. The integrated production facility of any one of embodiments 29 to 32, wherein the unit U P Including for S R or S' R Get the stream S H and CO-rich stream S CO Gas separation unit U PG .

[0319] 34. The integrated production facility of any one of embodiments 29 to 33, wherein the unit U P Including for S R or S' R Obtain a stream S containing CO2 and H2 W Water-gas shift reaction unit U PW , and further comprising arranging in U PW Downstream for S W Get the stream S H and CO2-rich stream S CO2 Gas separation unit U PG .

[0320] 35. The integrated production apparatus of any one of embodiments 29 to 34, further comprising a computer-supported control system for controlling the M F 、U C 、M H 、M E 、U R 、U P 、MR 、U CC 、U PG and U PW At least one of .

[0321] 36. A computer program comprising instructions which, when executed by a computer supported control system as defined in embodiment 35, cause the system to perform the method as defined in any one of embodiments 1 to 28.

[0322] 37. A non-transitory computer-readable medium comprising instructions that, when executed by one or more processors, cause the one or more processors to perform the procedure of embodiment 36.

[0323] 38. Use of the integrated production facility of any one of embodiments 29 to 35 for performing the method of any one of embodiments 1 to 28.

[0324] 39. A method of performing the method of any one of embodiments 1 to 28 using the integrated production apparatus of any one of embodiments 29 to 35.

[0325] 40. A process for heat-consuming hydrocarbon conversion in an integrated production facility comprising

[0326] (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ;

[0327] (2) The unit U C The unit comprises a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2;

[0328] (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT ——The internal heat source H of the equipment INT Including H2, for the heat source H EXT-S、H EXT-F and H INT At least one of the above is sent to the heating device M H ;

[0329] (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R ;

[0330] (5) Controllable processing unit U P , used for processing S R or its partial flow S' R To obtain S R or S' R Compared with H2-rich stream S H ;

[0331] (6) and optionally includes a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , and is used to convert S' R Send to U P middle;

[0332] The process includes

[0333] (i) one or more heat sources according to (3) are removed from M E Send to M H , which is sufficient to H Producing satisfaction U C The caloric requirement E UC of calories;

[0334] (ii) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C undergoes hydrocarbon conversion to obtain the one or more product streams S and S O ;

[0335] (iii) S O Send to U R In and make S O in U R After undergoing restructuring, it obtained S R ;

[0336] wherein during the process, the parameter E as defined in any one of Examples 1 to 25 is determined UC 、E EXT-S , ΔE, H2N 、H 2P and ΔH,

[0337] Wherein for ΔE>0 and ΔH>0, the process further comprises

[0338] (iv) Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100;

[0339] (v) The stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0340] (vi) Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where y = 100;

[0341] (vii) will be from M E The obtained stream S' H As H INT Send to M H middle;

[0342] (viii) the external fossil heat source H of the one or more devices EXT-F At least one of them is passed through M E Send to M H In the amount sufficient to H Production (ΔE-E H2P ) calories;

[0343] Wherein for ΔE>0 and ΔH≤0, the process further comprises

[0344] (iv') Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0 <x≤100;

[0345] (v') the stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ;

[0346] (vi') Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where 0 <y≤100;

[0347] (vii') will be from M E The obtained stream S' H As H INT Send to M H middle;

[0348] Wherein for ΔE≤0, the process further comprises

[0349] (iv") Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x≤100;

[0350] (v") R Or if (iv') is performed and x≠0, then the stream S' R Send to U P In, get S H ;

[0351] (vi”) Make the flow S H If from U P If you get it, through M E , and get S H 100 vol-% flow S" H ;

[0352] (vii”) From M E Remove the stream S from H .

[0353] 41. The process of embodiment 40, wherein U C Further comprising a separation unit U S , wherein according to (ii), the process comprises

[0354] (ii.1) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C The cracked gas stream S is obtained by hydrocarbon conversion. C ;

[0355] (ii.2) The cracked gas stream S obtained according to (ii.1) C is sent to a separation unit U comprising at least one demethanation unit S , and the stream S is obtained from the demethanation unit O , wherein one or more product streams S are obtained from U S .

[0356] 42. The process according to embodiment 40 or 41,

[0357] where (iv) comprises

[0358] (iv) passing the S obtained from U R through M R , obtaining a stream S' which is x volume-% of S R , where x = 100; R R

[0359] where (iv') comprises

[0360] [[ID=३३]](iv') passing the S obtained from U R through M R , obtaining a stream S' which is x volume-% of S R , where 0 < x < 100, and obtaining a stream S" which is (100 - x) volume-% of S R R ; R R <00�2269>

[0361] where (iv") comprises <°002271>[[ID=५२]]

[0362] (iv") passing the S obtained from U R through M R , obtaining a stream S' which is x volume-% of S R , where 0 ≤ x < 100, and obtaining a stream S" which is (100 - x) volume-% of S R R R R . [[ID=६८]]

[0363] 43. The process according to any one of embodiments 40 to 42, wherein the processing unit U P comprises a gas separation unit U PG , where (v) comprises

[0364] (v) sending the stream S R or the stream S' R to the gas separation unit U PG , obtaining S H and a stream S rich in CO CO ;

[0365] Where (v') includes

[0366] (v') the stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ;

[0367] Where (v”) includes

[0368] (v") R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO .

[0369] 44. The process of any one of embodiments 40 to 43, wherein the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW ,

[0370] Among them (v) include

[0371] (v.1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0372] (v.2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0373] Where (v') includes

[0374] (v'.1) the stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ;

[0375] (v'.2) the stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ;

[0376] where (v”) includes

[0377] (v”.1) sending the stream S R or the stream S’ R to the water gas shift reaction unit U PW to obtain a stream S containing CO2 and H2 W ;

[0378] (v”.2) sending the stream S W to the gas separation unit U PG to obtain S H and a stream S rich in CO2 CO2 .

[0379] 45. The process according to any one of Examples 40 to 44,

[0380] where (vi’) includes <{

[0381] (vi’) passing the stream S obtained from U P through M H to obtain a stream S’ that is y volume-% of S E H where 0 < y < 100, and obtaining a stream S” that is (100 - y) volume-% of S H H H H . H .

[0382] 46. The method according to any one of examples 40 to 45, which is at least partially computer-implemented. BRIEF DESCRIPTION OF THE DRAWINGS

[0383] Figure 1 is a schematic illustration of an interconnection unit and device of an integrated production plant of the present invention and for performing the method of the present invention, and the streams sent to and obtained from the unit and device. In this figure, the supply device M F is shown for supplying one or more hydrocarbon feed streams S C to the unit U for heat-consuming hydrocarbon conversion F . In this unit U C hydrocarbon conversion occurs, and one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 are obtained from U C O . Further, the unit U C H includes a heating device M H which in turn includes means for receiving heat from one or more heat sources H S (sustainable heat source H outside the device EXT-S , fossil heat source H outside the device EXT-S and internal heat source H of the device INT) a device for generating heat, wherein the one or more heat sources H S Including hydrogen (H2). Then the light hydrocarbon containing CH4 is converted into waste gas stream S O Sent to reforming unit U R , from which a stream S containing H2 and CO is obtained R Then this stream S R Sent to processing unit U P In the process unit, a H2-rich stream S is obtained. H (and optionally one or more other streams, indicated by dashed arrows).

[0384] According to the control method of the present invention, if the determined value ΔE=E UC –E EXT-S (i.e. U C The heat demand can be connected to an external sustainable heat source H via one or more devices EXT-S Supply to U C The difference in heat, which is indicated by the dashed arrow marked “ext”) is greater than zero, that is, U cannot be satisfied only by a sustainable heat source outside the device. C The following parameters are determined based on the heat demand:

[0385] -In device M H The amount of H2 required to produce ΔE in the solution. This amount is referred to herein as H 2N .

[0386] -Can be used in U R and the maximum amount of H2 produced in UP, which is then contained in stream S H This amount is referred to herein as H 2P , and based on H 2P , a certain amount of heat can be generated, which is referred to as E in this article H2P .

[0387] - parameter ΔH, which is defined as the difference H 2N -H 2P .

[0388] If ΔH is greater than zero, this means that the heat demand ΔE cannot be met by the maximum amount H alone. 2P Cover, then control the processing unit U P , supply device M E Make the maximum amount H 2P Via H2-rich stream S H and S' H Send to M H In order to H E H2P In this case, the remaining amount of heat is converted to an external fossil heat source HEXT-F At least one of them is passed through M E to generate the remaining amount of heat (ΔE – E H2P ) is sent to M H middle.

[0389] If ΔH is less than or equal to zero, it means that the heat demand ΔE can be R and U P The amount of available H2 covers the control process unit U P , supply device M E So that it will be enough to H The amount of H2 produced in the amount ΔE is via the H2-rich stream S H and S' H Send to M H In this case, you can control U P , in such a way that S H The amount of H2 in M H In this case, the flow S H will be with the stream S' H Same, that is, supply device M E The control method is such that the entire flow S H As a stream S' H Sent to M H However, if the H The amount of H2 available is too high, i.e. based on S H =S' H In M H Excessive heat generation (e.g. due to control U P It is not allowed to produce lower amounts of S H ), then the supply device M E The method may be controlled so that only S is sufficient to produce ΔE. H The appropriate part (ie S' H ) sent to M H In, and S H Part of (S) H ) is used for one or more additional suitable purposes.

[0390] According to the control method of the present invention, if the determined value ΔE=E UC –E EXT-S (i.e. U C The heat demand can be connected to an external sustainable heat source H via one or more devices EXT-S Supply to U C The difference in heat) is less than or equal to zero, that is, the device can be heated only by a sustainable heat source H outside the device. EXT-S Meet U CThe heat demand of the processing unit U P , supply device M E is controlled in such a way that H2 is not passed through the H2-rich stream S H Send to M H In this case, the supply device M E The method of being controlled is such that S H Part of it is sent to M H and with S H Same S" H is used for one or more additional suitable purposes.

[0391] Figure 2 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 1 In contrast, the device includes a U R Downstream and U P Additional upstream controllable supply device M R By adding M R Integration into the equipment additionally allows control of the entire process. In particular, M R Allow the stream S obtained from the reorganization R The corresponding partial flow S' R Send to U P , then you can do the same as above for Figure 1 The partial flow is processed as described. The partial flow S" obtained accordingly R It can be used for other purposes, wherein it is preferably used as synthesis gas, in particular for the production of one or more of methanol, liquid fuels, hydrocarbons, lubricants, oxo alcohols and ammonia. C The energy demand of the entire flow S R By M R , in this scenario, S' R With S R same.

[0392] Figure 3 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 1 In contrast, the unit U C The preferred configuration, where U C Including lysis unit U CC , preferably a thermal cracking unit, more preferably a steam cracking unit. Further, unit U C Including separation unit U S, the separation unit is used to separate the CC The obtained cracking gas flow S C Downstream processing. This separation unit U S It comprises a demethanization stage (not shown) from which a light hydrocarbon conversion waste gas stream S is obtained. O .

[0393] Figure 4 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 3 In contrast, the device shown here additionally includes Figure 2 The device M is described in detail in the context of R .

[0394] Figure 5 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 3 In contrast, the unit U P The specific configuration of the gas separation unit U PG The gas separation unit is used to separate the reformed gas from the reformed gas stream S R Separate the H2-rich gas stream S H , except S H In addition, a CO-rich stream S is obtained CO .

[0395] Figure 6 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention and for carrying out the method according to the invention, as well as the flows fed to and taken from said units and devices. Figure 5 In contrast, the device shown here additionally includes Figure 2 The device M is described in detail in the context of R .

[0396] Figure 7 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 5 In contrast, the unit U P Another specific configuration, namely as a downstream gas separation unit U PG Water-gas shift reaction unit U PW Configuration. In unit U GW In the middle, make the flow S R undergoes a water-gas shift reaction and obtains a stream S containing CO2 and H2W , and the stream is then sent to U PG In this case, the gas separation unit U GS For streaming from S W Separate the H2-rich gas stream S H , except S H In addition, a CO2-rich stream S is obtained CO2 .

[0397] Figure 8 is a schematic representation of the interconnected units and devices of an integrated production plant according to the invention for carrying out the method according to the invention, and of the streams fed into and taken from said units and devices. Figure 7 In contrast, the device shown here additionally includes Figure 2 The device M is described in detail in the context of R .

Claims

1. A method for controlling a process carried out in an integrated production facility, wherein the integrated production facility comprises (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ; (2) The unit U C The unit includes a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2; (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT ——The internal heat source H of the equipment INT Including H2, for the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ; (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R ; (5) Controllable processing unit U P , used for processing S R or its partial flow S' R To obtain S R or S' R Compared with H2-rich stream S H ; (6) and optionally includes a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , and is used to convert S' R Send to U P middle; in The process includes (i) one or more heat sources according to (3) are removed from M E Send to M H , which is sufficient to H Producing satisfaction U C The heat requirement E for the hydrocarbon conversion UC of calories; (ii) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C undergoes hydrocarbon conversion to obtain the one or more product streams S and S O ; (iii) S O Send to U R and make S O in U R After undergoing restructuring, it obtained S R ; Wherein the method for controlling the process comprises (a) Determine U C The hydrocarbon conversion in M H Provided caloric demand E UC ; (b) determining a sustainable heat source H external to the one or more devices EXT-S Available for U C The amount of calories E EXT-S ; (c) Determine ΔE = E UC –E EXT-S ,and (c.1) If ΔE>0, then (c.1.1) Determine H 2N , that is, in M H The amount of H2 required to produce ΔE in (c.1.2) Determine H 2P , which is used to H Production volume E H2P The calories in U R and U P can be generated to be included in S H The maximum amount of H2 in (c.1.3) Determine ΔH = H 2N –H 2P ;and (c.1.3.1) If ΔH > 0, then Control the processing unit U P , the supply device M E And optionally the supply device M R , so that H 2P Via S H Send to M H middle; The process further comprises (iv) Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100; (v) The stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ; (vi) Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where y = 100; (vii) will be from M E The obtained stream S' H As H INT Send to M H middle; (viii) the external fossil heat source H of the one or more devices EXT-F At least one of them is passed through M E Send to M H In the amount sufficient to H Production (ΔE-E H2P ) calories; (c.1.3.2) If ΔH ≤ 0, then Control the processing unit U P , the supply device M E And optionally the supply device M R , so that it will be sufficient to H The amount of H2 produced in ΔE is S H Send to M H middle; The process further comprises (iv') Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0 <x≤100; (v') the stream S R Or if (iv) is performed, then the stream S' R Send to U P In, get S H ; (vi') Make U P The obtained stream S H By M E , and get S H y volume-% flow S' H , where 0 <y≤100; (vii') will be from M E The obtained stream S' H As H INT Send to M H middle; (c.2) If ΔE≤0, then Control the processing unit U P , the supply device M E And optionally the supply device M R , so that H2 is not transferred through S H Send to M H middle; The process further comprises (iv") Optionally, R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x≤100; (v") the flow S R Or if (iv') is performed and x≠0, then the stream S' R Send to U P In, get S H ; (vi”) Make the flow S H If from U P If you get it, through M E , and get S H 100 vol-% flow S" H ; (vii”) From M E Remove the stream S" H .

2. The method according to claim 1, wherein 40 to 100 vol-%, preferably 60 to 100 vol-%, more preferably 80 to 100 vol-%, more preferably 90 to 100 vol-%, more preferably 95 to 100 vol-% of S O Composed of CH4.

3. The method according to claim 1 or 2, wherein The unit U for heat-consuming hydrocarbon conversion C Including lysis unit U CC , preferably a thermal cracking unit, more preferably a steam cracking unit.

4. The method according to claim 3, wherein: U C Further comprising a separation unit U S , wherein according to (ii), the process comprises (ii.1) at least one hydrocarbon feed stream S F Send to U C and making the at least one feed stream S F in U C The cracked gas stream S is obtained by hydrocarbon conversion. C ; (ii.2) The cracked gas stream S obtained according to (ii.1) C Sent to a separation unit U comprising at least one demethanation unit S , the stream S is obtained from the demethanation unit O , from U S obtaining the one or more product streams S; wherein the demethanation step according to (ii.2) preferably comprises a distillation step from which an overhead stream S comprising CH4 and H2 is obtained O1 , and more preferably further comprising a separation step, wherein S O1 Separated into a H2-rich stream and a CH4-rich stream S O2 , where according to (iii) S O1 or a partial flow thereof, preferably S O2 or a portion thereof as the flow S O Enter U R .

5. The method according to any one of claims 1 to 4, preferably any one of embodiments 3 to 5, wherein 96 to 100 vol-%, preferably 98 to 100 vol-%, more preferably 99 to 100 vol-%, more preferably 99.9 to 100 vol-% of S O Composed of CH4, and wherein preferably 0 to 4 volume-%, more preferably 0 to 2 volume-%, more preferably 0 to 1 volume-%, more preferably 0 to 0.1 volume-% of S O Composed of H2.

6. The method according to any one of claims 1 to 5, wherein The one or more devices according to (3) are external sustainable heat sources H EXT-S Including one or more of solar energy, wind energy, hydro energy, tidal energy, geothermal energy and biomass energy, ammonia obtained from renewable sources, biomethane, bio-LNG and H2 obtained from renewable sources.

7. The method according to any one of claims 1 to 6, wherein The reforming unit U according to (4) R The method comprises one or more of an autothermal reforming (ATR) unit, a steam reforming (STR) unit and a partial oxidation (POX) unit, preferably one or more of an autothermal reforming (ATR) unit and a steam reforming (STR) unit.

8. The method according to any one of claims 1 to 7, in, (iv) including (iv) Make R Obtained S R By M R , and get S R Volume-% flow S' of x R , where x = 100; Among them, (iv') includes (iv’) Make the S obtained from U R obtained S R through M R to obtain a stream S’ of x volume-% as S R where 0 < x < 100, and to obtain a stream S” of (100 - x) volume-% as S R ; R R ; Among them, (iv") includes (iv) R Obtained S R By M R , and get S R Volume-% flow S' of x R , where 0≤x<100, and obtained as S R (100-x) volume-% flow S" R ; Wherein the flow S" R At least a portion of the R As synthesis gas, more preferably including the use of S" R The synthesis gas can be used to produce one or more of methanol, liquid fuels, hydrocarbons, lubricants, oxo alcohols and ammonia.

9. The method according to any one of claims 1 to 8, wherein According to (5) the processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW One or more of .

10. The method of claim 9, wherein: The processing unit U P Including gas separation unit U PG , Among them (v) include (v) The stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ; in (v') includes (v') the stream S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ; in (v) includes (v") the flow S R Or the stream S' R Sent to the gas separation unit U PG In, get S H and CO-rich stream S CO ; The flow S CO Preferably for further use, wherein said further use preferably comprises the use of S CO Methanol is synthesized with hydrogen, preferably from a renewable source.

11. The method of claim 9, wherein: The processing unit U P Including gas separation unit U PG and water-gas shift reaction unit U PW , Among them (v) include (v.1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ; (v.2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ; in (v') includes (v'.1) the stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ; (v'.2) the stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ; in (v) includes (v".1) The stream S R Or the stream S' R Sent to the water gas shift reaction unit U PW In the process, a stream S containing CO2 and H2 is obtained. W ; (v".2) The stream S W Sent to the gas separation unit U PG In, get S H and CO2-rich stream S CO2 ; The flow S CO2 Preferably for further use, wherein said further use preferably comprises one or more of carbon capture and storage (CCS) and carbon capture utilisation (CCU).

12. The method according to any one of claims 1 to 11, wherein 60 to 100 vol-%, more preferably 70 to 100 vol-%, more preferably 80 to 100 vol-%, more preferably 90 to 100 vol-%, more preferably 95 to 100 vol-%, more preferably 99 to 100 vol-% of the H2-rich stream S H Composed of H2.

13. The method according to any one of claims 1 to 12, wherein (vi') including (vi’) cause the stream S obtained from U P to pass through M H and obtain a stream S' of y volume-% as S E where 0 < y < 100, and obtain a stream S" of (100 - y) volume-% as S H H H H ​​​​ Wherein the flow S" H or a portion thereof is preferably used for another purpose, wherein said another purpose preferably comprises the use of S" H As a U C A heat source in one or more units other than the 14. The method according to any one of claims 1 to 13, wherein (vii”) For x≠0, include the flow S” H or a portion thereof for another use, wherein the other use preferably comprises the use of S" H As a U C A heat source in one or more units other than the 15. An integrated production device, preferably an integrated production device for carrying out the method according to any one of claims 1 to 14, comprising (1) Supply device M F , for the conversion of heat-consuming hydrocarbons to unit U C Providing one or more hydrocarbon feed streams S F , wherein the supply device M F with U C Connect the hydrocarbon feed stream S F At least one of them is sent to U C In, from U C Obtain one or more product streams S and a light hydrocarbon conversion waste gas stream S containing CH4 O ; (2) The unit U C The unit includes a heating device M for providing heat to the hydrocarbon conversion H wherein the heating device M H including a heat source H S means for generating heat, and wherein said one or more heat sources H S Including H2; (3) Controllable supply device M E , used to provide one or more devices with an external sustainable heat source H EXT-S , one or more external fossil heat sources H EXT-F , and one or more internal heat sources H INT , the internal heat source H of the device INT comprising H2, wherein the supply means M E with U C Connect the heat source H EXT-S 、H EXT-F and H INT At least one of the above is sent to the heating device M H ; (4) Reforming unit U R , used to convert the light hydrocarbon into waste gas stream S O is subjected to reforming to obtain a product gas stream S comprising CO and H2 R , where U R Arranged in U C Downstream and connected with U C Connect to S O Send to U R middle; (5) Controllable processing unit U P , used for processing S R To generate S R Compared with H2-rich stream S H , where U P Arranged in U R Downstream and connected with U R Connect to S R Send to U P middle; (6) and optionally includes a controllable supply device M R , for optionally converting the stream S R The flow is divided into the partial flow S' R and flow S" R , where M R Arranged in U R Downstream and U P Upstream, and U R Connect to S R Send to M R and with U P Connect to S' R or S" R Send to U P middle; The unit U for heat-consuming hydrocarbon conversion C Preferably comprising a lysis unit U CC , more preferably a thermal cracking unit, more preferably a steam cracking unit, wherein U C Preferably, the method further comprises a method for treating the cracked gas stream S C Separation unit U S , where U S comprising at least one demethanation unit, wherein the stream S is obtained from said demethanation unit O , and where from U S obtaining the one or more product streams; The reforming unit U R Preferably comprising one or more of an autothermal reforming (ATR) unit, a steam reforming (STR) unit and a partial oxidation (POX) unit, more preferably one or more of an autothermal reforming (ATR) unit and a steam reforming (STR) unit; Preferably, the unit U P Including for S R or S' R Get the stream S H and CO-rich stream S CO Gas separation unit U PG , or include for S R or S' R Obtain a stream S containing CO2 and H2 W Water-gas shift reaction unit U PW , and further comprising arranging in U PW Downstream for S W Get the stream S H and CO2-rich stream S CO2 Gas separation unit U PG .

16. The integrated production facility of claim 15, further comprising a computer-supported control system for controlling M F 、U C 、M H 、M E 、U R 、U P 、M R 、U CC 、U PG and U PW At least one of .

17. A computer program comprising instructions which, when executed by a computer supported control system as defined in claim 16, cause the system to perform the method as claimed in any one of claims 1 to 14.

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