A method of optimizing a process in a chemical production plant

Abstract

A method of optimizing a process in a chemical production plant, wherein the production plant comprises an electrical energy storage unit US, an electrical energy consuming chemical production unit UP being electrically connected to US and being electrically connected to a power grid PG, and means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP.

Description

A method of optimizing a process in a chemical production plantThe present invention relates to a method of optimizing a process in a chemical production plant, wherein theproduction plant comprises an electrical energy storage unit US, an electrical energy consuming chemical productionunit UP being electrically connected to US and being electrically connected to a power grid PG, and means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP. Further, the present invention relates to the process carried out in the chemical production plant and the production plant as such. The provision of electrical energy is one of the most important criteria for the operation of chemical processes in the corresponding production plants. When planning such plants, it must generally be assumed that fluctuations in the composition of the electricity mix used and the price of the electricity will occur during operation of the plant due toincreasing proportions of renewable energies in the electricity grid. In particular, but not only in less developedelectricity grids, fluctuations in grid stability can be expected due to fluctuations in the proportion of renewable energies. In principle, processes in chemical production plants are ideally operated at constant load. Low loads can lead to the degradation of plants, for example because deposits of various kinds can form in the plant if it is not operated at or near its optimum. Furthermore, from an ecological point of view in particular, the aim is to increasingly electrify processes in chemical production plants in order to reduce dependence on methane as a heating medium, for example, and thus reduce carbon dioxide emissions. Of particular interest here is the use of electrical energy generated from renewable sources. This results in the task of operating processes in electrified chemical production plants in such a way that the production plant is operated constantly and, from an ecological and economic point of view, uses electrical energy from renewable sources wherever possible in order to realize corresponding processes with positive environmental attributes.CN 113993816 A relates to reducing environmental emissions, such as carbon dioxide, by reducing the combustionof hydrocarbons, e.g., natural gas / fossil fuels, used as fuels in ammonia plants. CN 117040019 A relates to a flexible low-cost operation method of a salt hydrogen light storage comprehensive energy system. US 2020 / 098062 A1 relates to systems and methods for allocation of renewable energy capacity.In view thereof, the present invention relates to a method of optimizing a process in a chemical production plant,wherein the production plant comprises(1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected to US and beingelectrically connected to a power grid PG;(3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;wherein the process comprises supplying electrical energy to UP from at least one of US and PG; wherein the method of optimizing the process comprises(a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, wherein ΔES(UP)is characterized by a share SUP thereof from at least one renewable source with SUP = 100 %;(a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and being characterized by ashare SPGthereof from at least one renewable sources with SPG= 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG);(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP in anamount δE(PG) = δES(PG) + δEN(PG) and from USto UPin an amount δE(US), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);wherein f ≥ 0, g ≤ 1, and f ≤ g; wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δt; wherein PG is characterized by the amount of electrical energy ΔES(PG) available within Δt and by the amount ofelectrical energy ΔEN(PG) available within Δt, wherein ΔEN(PG) is characterized by a share NPG thereof from at leastone renewable sources with NPG = 0 %; wherein ΔE(US) + ΔEN(PG) ≥ ΔES(UP). According to the present invention, according to (a.1), the amount of electrical energy ΔES(UP) to be consumed in theprocess in UP within Δt is determined, wherein ΔES(UP) is characterized by a share SUP thereof from at least onerenewable source with SUP= 100 %. This amount ΔES(UP) is to be understood as a theoretical target amount of ecologically advantageous electrical energy prepared from at least one renewable source, which target amount is needed for the process to be carried out in UP within the time interval Δt. According to the steps according to (b), theprocess is then controlled by the method of the present invention so that this target value is realized in a suitablemanner. According to (1.1) and (2.1), the method of the present invention allows for varying both the minimum amount and themaximum amount of δES(PG) via the factors f and g. In particular, these factors are defined as f = qE ^ f(min) and g = qE^ g(max). As far as these definitions are concerned, it is preferred that f < g, more preferably that 0.80 ≤ f(min) ≤ 1,more preferably 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1. It is further preferred that 0.97 ≤ f(min) ≤ 1, morepreferably 0.98 ≤ f(min) ≤ 1, more preferably 0.99 ≤ f(min) ≤ 1. Preferably, g(max) = 1. This means that according tothe preferred values above, and if the factor qE = 1, the amount of δES(PG) passed from PG to UP within Δt is- in case ΔΔES ≤ 0:preferably in the range of from 80 % to 100 % of ΔES(UP), more preferably in the range of from 90 % to 100 % of ΔES(UP), more preferably in the range of from 95 % to 100 % of ΔES(UP), more preferably in the range of from97 % to 100 % of ΔES(UP), more preferably in the range of from 98 % to 100 % of ΔES(UP), more preferably in the range of from 99 % to 100 % of ΔES(UP); and- in case ΔΔES > 0:preferably in the range of from 80 % to 100 % of ΔES(PG), more preferably in the range of from 90 % to 100 % of ΔES(PG), more preferably in the range of from 95 % to 100 % of ΔES(PG), more preferably in the range of from 97 % to 100 % of ΔES(PG), more preferably in the range of from 98 % to 100 % of ΔES(PG), more preferably in the range of from 99 % to 100 % of ΔES(PG).In the formulae in accordance with the present invention, the operator “ ^ “ represents a multiplicator. For example, informula (1.1), “f ^ ΔER(UP)” relates to f being multiplied with ΔER(UP), and “g ^ ΔER(UP)” relates to g being multipliedwith ΔER(UP).Preferably, according to the present invention, f < g.Further according to the present invention, the amount ΔES(UP) is to be understood as a theoretical target amount ofecologically advantageous electrical energy prepared from at least one renewable source, which target amount is needed for the process to be carried out in UP within the time interval Δt. According to the steps according to (b) as indicated above, the process is then controlled by the method of the present invention so that this target value is realized in a suitable manner. Thus, the term “share” is defined as either share SUP thereof from at least one renewable source with SUP= 100 % or as a share SPGthereof from at least one renewable sources with SPG= 100 %. Further according to the present invention,according to one embodiment, it is preferred that with regard to the amountof electrical energy provided as δE(US) + δEN(PG), δEN(PG) is at most δE(US), preferably less than δE(US), and inparticular 0. Therefore, in these cases, it is preferred that 0 ≤ δEN(PG) ≤ δE(US), more preferably 0 ≤ δEN(PG) < δE(US),more preferably δEN(PG) = 0. This means than in cases where a certain amount of necessary electrical energy is to besupplied within Δt by PG and US, it may be preferred that said certain amount of necessary electrical energy is suppliedmainly, preferably solely by US. According to the present invention, the electrical energy ΔES(PG) which is available within Δt is prepared from at least one renewable source. In view of the ecological advantages of such electrical energy, it is conceivable that using this energy is highly advantageous and will be used within Δt although electrical energy ΔE(US) is available. In case of ΔΔES ≤ 0, therefore, this means that the energy demand ΔES(UP) will be met essentially via ΔES(PG), which means thatqE = 1. However, when running the production plant according to the present invention, it is also conceivable that, although the use of ΔES(PG) would appear to be advantageous if assessed exclusively from an ecological perspective,the costs of ΔES(PG), compared to the costs of ΔEN(PG) and ΔE(US), may render the use of ΔES(PG) lessadvantageous. Since in most cases, both the ecological and the economical boundary conditions in terms of the supplywilt electrical energy will play a decisive role when running a chemical production plant, the method according to thepresent invention allows for respectively varying the amount of ΔES(PG) depending on the costs via the factor qE. Therefore, preferably, the present invention also relates to the method as described above, wherein ΔES(PG) is further characterized by cost factors, ΔEN(PG) is further characterized by cost factors, and ΔE(US) is characterized by costs factor, wherein determining for a time interval Δt which starts at a time t according to (a) further comprises(a.4) determining the parameter qE, comprising(4.1) determining the cost factors of ΔES(PG), the cost factors of ΔEN(PG) and the cost factors of ΔE(US);(4.2) determining, based on the cost factors determined according to (4.1), the costs of ΔES(PG), ΔEN(PG)and ΔE(US); (4.3) determining, based on the costs of ΔES(PG), ΔEN(PG) and ΔE(US) determined according to (4.2) theparameter qE, wherein the higher the costs of ΔES(PG) relative to the costs of ΔEN(PG) and ΔE(US), the smaller qE. The term “cost factors” of a given amount of energy, such as ΔES(PG), refers to the sum of all individual cost itemsincurred in the provision of said amount of electrical energy. The term “costs” of a given amount of energy, such asΔES(PG), refers to the total costs ΔES(PG).In case the the costs of ΔES(PG) are higher than the costs of ΔEN(PG) and ΔE(US), it is preferred that 0 ≤ qE < 1,preferably 0 ≤ qE ≤ 0.5, more preferably 0 ≤ qE < 0.5, more preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE ≤ 0. If itadvisable for the process of the present invention to be carried out in a meaningful manner, it may be preferred that qE= 0, which means that according to (b.1), the total amount of electrical energy provided to UP within Δt is supplied viaδE(US) + δEN(PG). According to a specific scenario of the present invention, it is preferred that with regard to the amount of electrical energy provided as δE(US) + δEN(PG), δEN(PG) is at most δE(US), preferably less than δE(US), and in particular 0. Therefore, in these cases, it is preferred that 0 ≤ δEN(PG) ≤ δE(US), more preferably 0 ≤ δEN(PG) < δE(US), morepreferably δEN(PG) = 0. This means than in cases where a certain amount of necessary electrical energy is to besupplied within Δt by PG and US, it may be preferred that said certain amount of necessary electrical energy is suppliedmainly, preferably solely by US. According to another specific scenario of the present invention, it is preferred that in case ΔΔES > 0, which means that there is not enough electrical energy available via ΔES(PG) to meet the energy demand ΔES(UP), either as such and / or in view of the costs as discussed above, only US is used as electrical energy source for UP within Δt. Therefore, in these cases, it is preferred that if ΔΔES > 0, δES(PG) = δEN(PG) = 0.Further according to the present invention, it may be preferred that ΔE(US) = ΔES(US) + ΔEN(US) with 0 ≤ ΔES(US) ≤ ΔE(US), wherein ΔES(US) is characterized by a share SUS thereof from at least one renewable source with SUS = 100 % and ΔEN(US) is characterized by a share NUS thereof from at least one renewable source with NUS = 0 %. Preferably according to the present invention, the term “at least one renewable source” refers to at least one energysource which is selected from the group consisting of wind energy; solar energy; biomass energy; geothermal energy;hydropower energy including tidal energy; one or more sources prepared from renewable sources including one or more of ammonia, hydrogen (H2), biomethane, and bio-LNG; and a combination of two or more thereof.- Solar energy may comprise one or more of photovoltaic (PV) solar energy, solar thermal energy (STE),concentrated solar power (CSP), passive solar energy, and building-integrated photovoltaics (BIPV).- Wind energy may comprise one or more of utility scale wind energy and offshore wind energy.- Geothermal energy may comprise one or more or dry steam energy, flash steam energy, and binary cycleenergy.- Biomass energy may be derived from liquid and or solid biomass and may include materials produced bygrowth of microorganisms, plants, and animals. As far as biomass species are concerned, those are especiallypreferred which are comprised in waste material and / or are not in competition with the food-chain. Examples therefor include, but are not limited to, -- wood tar where aromatic hydrocarbons can be obtained from the distillation of wood tar which in turn isproduced during the processing of wood for pulping and papermaking; -- natural sources where aromatic hydrocarbons can be found certain plants, such as guaiacum, and incertain soils, such as those with a high organic matter content; -- lignocellulosic biomass;-- sources comprising furan which in turn is obtained from industrial sugars which preferably are not incompetition with the food chain.- Hydropower energy may be derived from flowing water, and suitable hydropower facilities may be based on oneor more of impoundment, diversion, and pumped storage.Preferably according to the present invention, the electrical energy storage unit USaccording to (1) is further electrically connected to the power grid PGaccording to (2). This configuration allows for supplying energy from the power grid PGto the storage unit US within a time interval Δt. It is noted that the method of the present allows for supplying energy from the power grid PG to the storage unit US within a certain number of preferably consecutive time intervals Δt, thereby at least partially charging US, and then subsequently stopping this specific supply for a certain number of preferably consecutive time intervals Δt. Therefore, the present invention also relates to the method as described above, wherein the electrical energy storage unit US according to (1) is further electrically connected to the power grid PG according to (2); wherein the means ME are means further for regulating the amount of electrical energy supplied from PG to US;wherein the process comprises supplying electrical energy to UP from at least one of US and PG and optionally further from PG to US; wherein according to (b), the method of optimizing the process further comprises controlling ME so that the process further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG) = δ*ES(PG) + δ*EN(PG), wherein(b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax≤ 1;(b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g. According to the method of the present invention, if electrical energy is to be supplied from PG to US, the respective amount can be varied for a given Δt via the factors x and y as indicated above. If, for example, US is sufficiently charged, no energy δ*ES(PG) will be supplied, and x is chosen to be zero. On the other hand, if the state of charge of US allows it, δ*ES(PG) will be the entire amount of available energy, i.e. xmax = 1, and ymax = 1, respectively. It is noted that the values of xmax and ymax will depend on the respective state of charge of US, and these values will be determined according to the present invention, preferably by the means ME. With regard to the time interval Δt, it is preferred that Δt is in the range of from 5 min to 24 h, more preferably in the range of from 5 min to 12 h, more preferably in the range of from 5 min to 6 h, more preferably in the range of from 5min to 3 h, more preferably in the range of from 10 min to 2 h. By way of example, shorter periods of time may be inthe range of from 5 min to 30 min, and longer periods of time may be in the range of from 0.5 h to 2 h or from 0.5 to 1h. Preferably, the sum of all successive time intervals Δt is the runtime of the process of the present invention which iscontrolled by the method of the present invention. According to the present invention, successive time intervals may can have the same length or different lengths.According to the present invention, it may be preferred that for every time interval Δt, the respective values of theamounts of electrical energy, for example ΔES(UP), ΔES(PG), ΔΔES, and the respective values of parameters such as fand g, including qE, and x and y, are determined and the process is controlled by the method of the present inventionaccordingly. i.e. the respective amounts of δES(PG), δE(US), δEN(PG), and – optionally or preferably – δ*ES(PG) andδ*EN(PG) are supplied. By determining said values of the amounts of electrical energy and said values of parameters for every time interval Δt, the present invention allows for taking into account, for example, varying supply of desiredelectrical energy over time and for realizing an optimized process by reacting flexibly to changing ecological and economical boundary conditions.With regard to the electrical storage unit US, it is preferred that it is a stationary energy storage unit which, morepreferably, comprises one or more of at least one battery on sodium-sulfur basis (NaS battery) and at least one batterybased on lithium iron phosphate cathode material (LFP battery). More preferably, the unit US comprises at least one NaS battery. Preferably, the electrical storage unit US has a capacity in the range of from 5.000 to 750.000 kWh, more preferably in the range of from 10.000 to 600.000 kWh, more preferably in the range of from 100.000 to 600.000 kWh, more preferably in the range of from 200.000 to 550.000 kWh. The electrical storage unit UShas a power, in kW, sufficient preferably for 20 to 100 %, more preferably for 30 to 100 %, more preferably from 40 to 100 %, more preferably from 50 to 100 % of the chemical production unit UP, such as from 60 to 100 % or from 70 to 100 % or from 80 to 100 % or from 90 to 100 %. The electrical storage unit USis preferably a modular system. In this case, the method of the present invention preferably comprises increasing and / or decreasing the capacity of US by adding or removing one or more electrical storage modules depending on the varying consumption of electrical energy in the chemical production unit UP.Generally, there are no specific restrictions regarding the process carried out in the chemical production unit UP. Inparticular, according to the present invention, it is possible that two or more different process are carried out in the unit UP, either in parallel and / or serially, of which at least one process is controlled by the method of the present invention. It is noted that a process which is controlled by the method of the present invention is not restricted to a process directed to producing a specific chemical compound or mixture of compounds, but also includes purification processes of any kind, and in general all conceivable processes and combination of process for which electrical energy is needed. More preferably, the process of the present invention which is controlled by the method of the present invention comprises one or more of at least one electrochemical process, at least one a high-temperature chemicalprocess and at least one further chemical process.The at least one electrochemical process preferably comprises one or more of production of hydrogen and co-production of oxygen via electrolysis of water (water electrolysis); production of chlorine and co-production of hydrogen and sodium hydroxide via electrolysis of sodium chloride in the presence of water (chlorine-alkali electrolysis); isolationof nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium viaelectrochemical reduction of alumina (Hall-Héroult process); production of carbon monoxide via reduction of carbon dioxide via electrolysis (eCOSTMprocess); electrochemical production of hydrocarbons from carbon dioxide and water; and electrochemical activation of nitrogen; more preferably one or more of water electrolysis; chlorine-alkalielectrolysis; and production of carbon monoxide by reduction of carbon dioxide via electrolysis.The at least one high-temperature process preferably comprises one or more of electrical heating of a cracker furnace,preferably for producing olefins and / or aromatic compounds via thermal cleavage of naphtha and / or liquefied petroleum gas (LPG) in the presence of water steam; steam-methane reforming; dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shift reaction; melting of metals and / or metal compounds including the production of virgin materials and of recycled materials; and calcination processes, preferably in one or more of catalyst field, battery field, and electronics field; methane pyrolysis; and plasma processes including use of plasma for waste treatment such as gasification, for carbon dioxide activation, for nitrogen activation, and for methane pyrolysis; more preferably one or more of electrical heating of a cracker furnace and methane pyrolysis.The at least one further chemical process preferably comprises one or more of e-boiler application, preferably forproduction of steam; e-drive application, preferably for operating a compressor, more preferably operating acompressor for gas compression; application in heat pump with high coefficient of performance including closed-loopheat pump and open-loop heat pump; application in mechanical vapour compression, application in cooling forexample in compressors and / or fans. Regarding the determination of the amounts of electrical energy and the values of the parameters, as indicated above, can be carried out either manually, or by using the support of a computer system, or by a combination thereof. Preferably, the method of the present invention, and also the process of the present invention, is at least partiallycomputer-implemented. More preferably, the production plant of the present invention further comprises(4) a computer-supported system for controlling at least the means ME according to (3).In particular, this computer-supported system is further used for determining at least one of ΔES(UP) according to (a.1), ΔES(PG) according to (a.2), ΔΔES according to (a.3), preferably determining the parameter qE, according to (a.4) as defined in embodiment 4, and more preferably also the parameters f, g, x and y. Yet further, the present invention relates to and describes a chemical production plant, preferably a chemicalproduction plant referred to hereinabove in the context of the description of the present invention, the chemicalproduction plant comprising(1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected with the unit US andbeing electrically connected with a power grid PG;(3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;wherein the unit US is preferably further electrically connected with the power grid PG; wherein the means ME are preferably means further for regulating the amount of electrical energy supplied from PG to US.Concerning the chemical production plant of the present invention and with regard to generally conceivable units USand UP, as well as generally conceivable and preferred processes carried out in UP, full reference is made to what is disclosed hereinabove in the context of the description of the method of the present invention and in the context of the respective embodiments of the embodiment section hereinunder, specifically being directed to the chemical production plant as such, in particular embodiments 23 to 32.Still further, the present invention relates to and describes a process, preferably a chemical production plant referred tohereinabove in the context of the description of the present invention, more preferably a process being carried out in a chemical production plant referred to hereinabove, wherein for a time interval Δt of the process, preferably for at least two time interval Δt of the process, more preferably for all time intervals Δt of the process, the process comprises supplying electrical energy- from PG to UP in an amount δE(PG);- from US to UP in an amount δE(US);- preferably from PG to US in an amount δ*E(PG);and the process further comprises(a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, wherein ΔES(UP)is characterized by a share SUPthereof from at least one renewable source with SUP= 100 %; (a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and being characterized by ashare SPG thereof from at least one renewable sources with SPG = 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG); and the process further comprises for said time interval Δt;(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP in anamount δE(PG) = δES(PG) + δEN(PG) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax≤ 1; (b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax ≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g. With regard to generally conceivable and preferred processes carried out in UP, full reference is made to what is disclosed hereinabove in the context of the description of the method of the present invention and in the context of the respective embodiments of the embodiment section hereinunder, specifically being directed to the chemical production plant as such, in particular embodiments 37 to 42.Still further, the present invention relates to a computer program comprising instructions which, when the program is executed by the computer-supported system as defined herein such as in embodiment 32, cause the system to perform the method as described herein, such as in any one of embodiments 1 to 22. Still further, the present invention relates to a non-transient computer-readable medium containing instructions which, when executed by one or more processors, cause the one or more processors to perform the computer program as described herein such as in embodiment 33. Still further, the present invention relates to the use of the production plant as described herein, such as in any one ofembodiments 23 to 32, for carrying out the method as described herein, such as in any one of embodiments 1 to 22.Still further, the present invention relates to a method of using the production plant as described herein, such as in anyone of embodiments 23 to 32, for carrying out the method as described herein, such as in any one of embodiments 1to 22. According to another aspect, the present invention relates to a process, preferably to the process as described above, which comprises the step of converting a chemical material obtainable by or obtained by the process as describedherein to obtain a product product Ω. Further to this aspect, the present invention relates to the step of using thechemical production plant as described herein to obtain a chemical material; and preferably converting the chemical material to obtain a product Ω.Preferably, the product Ω is selected from:- building block or monomer; or- polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product,preferably polymer product A; or- cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulationthereof; or- agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or- active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, humanfood additive, dietary supplements, aroma chemical or aroma composition; or- aqueous polymer dispersion, preferably polyurethane or polyurethane – poly(meth)acrylate hybrid polymerdispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or- cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition orformulation thereof; or- polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coatingor coated substrate.Regarding this process from which the product Ω, is obtained, it is preferred:that the content of the chemical material in the product Ω is 1 weight-% or more, preferably 2 weight-% or more, morepreferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / orthat the content of the chemical material in the product Ω is 100 weight-% or less, preferably 95 weight-% or less, morepreferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard. The publication Prior Art Disclosure; Issue 684; paragraphs

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

[1000] to

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

[1000] to

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

[1000] to

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

[2001] to

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

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

[2009] and

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

[2011] of Reference RF1. The term “industrial use polymer”, as used in the context of the product Ω herein, comprises rheology, polycarboxylate,alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaningpolymers defined in more detail in paragraphs

[3035] to

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

[3008] to

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

[3001] to

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

[3006] to

[3007] of Reference RF1. The term “industrialuse solvent”, as used in the context of the product Ω herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

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

[3056] to

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

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

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

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

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

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

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

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

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

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

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

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

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

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

[6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017)] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1.Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail inthe following sections of Reference RF1:section

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

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

[6006] entitled “Binders for paper coating”section

[6007] entitled “Binders for fiber bonding” section

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

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

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

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

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

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

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

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

[6011] entitled “Organicsolvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1. Theconverting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

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

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

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

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

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

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

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

[6021] of ReferenceRF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific buildingmaterial formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building materialformulation comprising a polymeric dispersant are disclosed in more detail in section

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

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

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

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

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

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

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

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

[8000] to

[8005] of Reference RF1. The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The method of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The method of any one ofembodiments 1, 2, 3 and 4". Further in particular, it is noted that in each instance where a range of embodiments ismentioned, for example in the context of a term such as "The production plant of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The production plant of any one of embodiments 1, 2, 3 and 4". Yet further in particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1, 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.1. A method of optimizing a process in a chemical production plant,wherein the production plant comprises (1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected to US and beingelectrically connected to a power grid PG; (3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;wherein the process comprises supplying electrical energy to UP from at least one of US and PG;wherein the method of optimizing the process comprises (a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, whereinΔES(UP) is characterized by a share SUP thereof from at least one renewable source with SUP = 100 %; (a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and beingcharacterized by a share SPG thereof from at least one renewable sources with SPG = 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG);(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP inan amount δE(PG) = δES(PG) + δEN(PG) and from US to UP in an amount δE(US), wherein(b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);wherein f ≥ 0, g ≤ 1, and f ≤ g; wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δt;wherein PG is characterized by the amount of electrical energy ΔES(PG) available within Δt and by the amountof electrical energy ΔEN(PG) available within Δt, wherein ΔEN(PG) is characterized by a share NPG thereof fromat least one renewable sources with NPG = 0 %;wherein ΔE(US) + ΔEN(PG) ≥ ΔES(UP).2. The method of embodiment 1, whereinf = qE ^ f(min);g = qE ^ g(max);with 0.80 ≤ f(min) ≤ 1, preferably 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1; g(max) = 1;0 ≤ qE ≤ 1.3. The method of embodiment 2, wherein 0.97 ≤ f(min) ≤ 1, preferably 0.98 ≤ f(min) ≤ 1, more preferably 0.99 ≤f(min) ≤ 1.4. The method of embodiment 2 or 3, wherein qE = 1.5. The method of embodiment 2 or 3, wherein ΔES(PG) is further characterized by cost factors, ΔEN(PG) is furthercharacterized by cost factors, and ΔE(US) is characterized by cost factors, wherein determining for a time interval Δt which starts at a time t according to (a) further comprises (a.4) determining the parameter qE, comprising(4.1) determining the cost factors of ΔES(PG), the cost factors of ΔEN(PG) and the cost factors ofΔE(US); (4.2) determining, based on the cost factors determined according to (4.1), the costs of ΔES(PG),ΔEN(PG) and ΔE(US);(4.3) determining, based on the costs of ΔES(PG), ΔEN(PG) and ΔE(US) determined according to(4.2) the parameter qE, wherein the higher the costs of ΔES(PG) relative to the costs ofΔEN(PG) and ΔE(US), the smaller qE.6. The method of embodiment 5, wherein the costs of ΔES(PG) is higher than the costs of ΔEN(PG) and ΔE(US), 0 ≤qE < 1, preferably 0 ≤ qE ≤ 0.5, more preferably 0 ≤ qE < 0.5, more preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤qE ≤ 0, more preferably qE = 0.7. The method of any one of embodiments 1 to 6, wherein 0 ≤ δEN(PG) ≤ δE(US), preferably0 ≤ δEN(PG) < δE(US), more preferably δEN(PG) = 0.8. The method of any one of embodiments 1 to 7, wherein the at least one renewable source is selected from thegroup consisting of wind energy; solar energy; biomass energy; geothermal energy; hydropower energyincluding tidal energy; one or more sources prepared from renewable sources including one or more of ammonia, hydrogen (H2), biomethane, and bio-LNG; and a combination of two or more thereof.9. The method of any one of embodiments 1 to 8, wherein ΔE(US) = ΔES(US) + ΔEN(US) with0 ≤ ΔES(US) ≤ ΔE(US), wherein ΔES(US) is characterized by a share SUSthereof from at least one renewable source with SUS= 100 % and ΔEN(US) is characterized by a share NUSthereof from at least one renewable source with NUS= 0 %.10. The method of any one of embodiments 1 to 9,wherein the electrical energy storage unit US according to (1) is further electrically connected to the power grid PG according to (2); wherein the means ME are means further for regulating the amount of electrical energy supplied from PG to US; wherein the process comprises supplying electrical energy to UP from at least one of US and PG and optionally further from PG to US; wherein according to (b), the method of optimizing the process further comprises controlling ME so that the process further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG) = δ*ES(PG) + δ*EN(PG), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax ≤ 1; (b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax ≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g.11. The process of any one of embodiments 1 to 10,wherein if ΔΔES > 0, δES(PG) = δEN(PG) = 0.12. The method of any one of embodiments 1 to 11, wherein Δt is in the range of from 5 min to 24 h, preferably inthe range of from 5 min to 12 h, more preferably in the range of from 5 min to 6 h, more preferably in the range of from 5 min to 3 h, more preferably in the range of from 10 min to 2 h.13. The method of any one of embodiments 1 to 12, wherein the electrical storage unit US is a stationary energystorage unit comprising one or more of at least one battery on sodium-sulfur basis (NaS battery) and at least one battery based on lithium iron phosphate cathode material (LFP battery), preferably at least one NaS battery.14. The method of any one of embodiments 1 to 13, wherein the electrical storage unit US has a capacity in therange of from 5.000 to 750.000 kWh, preferably in the range of from 10.000 to 600.000 kWh, more preferably in the range of from 100.000 to 600.000 kWh, more preferably in the range of from 200.000 to 550.000 kWh; wherein the electrical storage unit UShas a power, in kW, sufficient preferably for 20 to 100 %, more preferably for 30 to 100 %, more preferably from 40 to 100 %, more preferably from 50 to 100 % of the chemical production unit UP.15. The method of any one of embodiments 1 to 14, wherein the electrical storage unit US is a modular system, themethod comprising increasing and / or decreasing the capacity of US by adding or removing one or more electrical storage modules depending on the varying consumption of electrical energy in the chemical production unit UP.16. The method of any one of embodiments 1 to 15, wherein the process carried out in the chemical production unitUPcomprises one or more of at least one electrochemical process, at least one a high-temperature chemical process and at least one further chemical process.17. The method of embodiment 16, wherein the at least one electrochemical process comprises one or more ofproduction of hydrogen and co-production of oxygen via electrolysis of water (water electrolysis); production of chlorine and co-production of hydrogen and sodium hydroxide via electrolysis of sodium chloride in the presence of water (chlorine-alkali electrolysis); isolation of nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium via electrochemical reduction of alumina (Hall-Héroult process); production of carbon monoxide via reduction of carbon dioxide via electrolysis (eCOSTMprocess); electrochemical production of hydrocarbons from carbon dioxide and water; and electrochemical activation of nitrogen; preferably one or more of water electrolysis; chlorine-alkali electrolysis; and production of carbonmonoxide by reduction of carbon dioxide via electrolysis.18. The method of embodiment 16 or 17, wherein the at least one high-temperature process comprises one ormore of electrical heating of a cracker furnace, preferably for producing olefins and / or aromatic compounds via thermal cleavage of naphtha and / or liquefied petroleum gas (LPG) in the presence of water steam; steam- methane reforming; dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shift reaction; melting of metals and / or metal compounds including the production of virgin materials and of recycled materials; and calcination processes, preferably in one or more of catalyst field, battery field, and electronics field; methane pyrolysis; and plasma processes including use of plasma for waste treatment such as gasification, for carbon dioxide activation, for nitrogen activation, and for methane pyrolysis; preferably one or more of electrical heating of a cracker furnace and methane pyrolysis.19. The method of any one of embodiments 16 to 18, wherein the at least one further chemical process comprisesone or more of e-boiler application, preferably for production of steam; e-drive application, preferably for operating a compressor, more preferably operating a compressor for gas compression; application in heat pump with high coefficient of performance including closed-loop heat pump and open-loop heat pump; application in mechanical vapour compression, application in cooling for example in compressors and / or fans.20. The method of any one of embodiments 1 to 19, being at least partially computer-implemented.21. The method of embodiment 20, wherein the production plant further comprises(4) a computer-supported system for controlling at least the means ME according to (3).22. The method of embodiment 21, wherein the computer-supported system is further used for determining at leastone of ΔES(UP) according to (a.1), ΔES(PG) according to (a.2), ΔΔES according to (a.3), and preferably determining the parameter qE, according to (a.4) as defined in embodiment 4.23. A chemical production plant, preferably as referred to in any one of embodiments 1 to 22, comprising(1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected with the unit USand being electrically connected with a power grid PG; (3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;wherein the unit US is preferably further electrically connected with the power grid PG; wherein the means ME are preferably means further for regulating the amount of electrical energy supplied from PG to US.24. The production plant of embodiment 23, wherein the electrical storage unit US according to (1) is a stationaryenergy storage unit comprising one or more of at least one battery on sodium-sulfur basis (NaS battery) and at least one battery based on lithium iron phosphate cathode material (LFP battery), preferably at least one NaS battery.25. The production plant of embodiment 23 or 24, wherein the electrical storage unit US according to (1) has acapacity in the range of from 5.000 to 750.000 kWh, preferably in the range of from 10.000 to 600.000 kWh, more preferably in the range of from 100.000 to 600.000 kWh, more preferably in the range of from 200.000 to 550.000 kWh.26. The production plant of any one of embodiments 23 to 25, wherein the electrical storage unit US according to (1)has a power, in kW, sufficient for 20 to 100 %, preferably for 30 to 100 %, more preferably from 40 to 100 %,more preferably from 50 to 100 % of the chemical production unit UP according to (3).27. The production plant of any one of embodiments 23 to 26, wherein the electrical storage unit US is a modularsystem, the method comprising increasing and / or decreasing the capacity of USby adding or removing one or more electrical storage modules depending on the varying consumption of electrical energy in the chemical production unit UP.28. The production plant of any one of embodiments 23 to 27, wherein the chemical production unit UP is a unit forcarrying out one or more of at least one electrochemical process, at least one a high-temperature chemical process and at least one further chemical process.29. The production plant of embodiment 28, wherein the at least one electrochemical process comprises one ormore of production of hydrogen and co-production of oxygen via electrolysis of water (water electrolysis); production of chlorine and co-production of hydrogen and sodium hydroxide via electrolysis of sodium chloride in the presence of water (chlorine-alkali electrolysis); isolation of nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium via electrochemical reduction of alumina (Hall-Héroult process); production of carbon monoxide via reduction of carbon dioxide via electrolysis (eCOSTMprocess); electrochemical production of hydrocarbons from carbon dioxide and water; and electrochemical activation of nitrogen; preferably one or more of water electrolysis; chlorine-alkali electrolysis; and production ofcarbon monoxide by reduction of carbon dioxide via electrolysis.30. The production plant of embodiment 28 or 29, wherein the at least one high-temperature process comprisesone or more of electrical heating of a cracker furnace, preferably for producing olefins and / or aromatic compounds via thermal cleavage of naphtha and / or liquefied petroleum gas (LPG) in the presence of water steam; steam-methane reforming; dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shift reaction; melting of metals and / or metal compounds including the production of virgin materials and of recycled materials; and calcination processes, preferably in one or more of catalyst field, battery field, and electronics field; methane pyrolysis; and plasma processes including use of plasma for waste treatment such as gasification, for carbon dioxide activation, for nitrogen activation, and for methane pyrolysis; preferablyone or more of electrical heating of a cracker furnace and methane pyrolysis.31. The production plant of any one of embodiments 28 to 30, wherein the at least one further chemical processcomprises one or more of e-boiler application, preferably for production of steam; e-drive application, preferably for operating a compressor, more preferably operating a compressor for gas compression; application in heat pump with high coefficient of performance including closed-loop heat pump and open-loop heat pump;application in mechanical vapour compression, application in cooling for example in compressors and / or fans.32. The production plant of any one of embodiments 23 to 31, further comprising(4) a computer-supported system for controlling at least the means ME.33. A computer program comprising instructions which, when the program is executed by the computer-supportedsystem as defined in embodiment 32, cause the system to perform the method of any one of embodiments 1 to 22.34. A non-transient computer-readable medium containing instructions which, when executed by one or moreprocessors, cause the one or more processors to perform the program according to embodiment 33.35. Use of the production plant according to any one of embodiments 23 to 32 for carrying out the methodaccording to any one of embodiments 1 to 22.36. A method of using the production plant according to any one of embodiments 23 to 32 for carrying out themethod according to any one of embodiments 1 to 22.37. A process as referred to in any one of embodiments 1 to 22 being carried out in a chemical production plantaccording to any one of embodiments 23 to 32, wherein for a time interval Δt of the process, the process comprises supplying electrical energy- from PG to UP in an amount δE(PG);- from US to UP in an amount δE(US);- preferably from PG to US in an amount δ*E(PG);the process further comprises (a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, whereinΔES(UP) is characterized by a share SUP thereof from at least one renewable source with SUP = 100 %; (a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and beingcharacterized by a share SPG thereof from at least one renewable sources with SPG = 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG); and the process further comprises for said time interval Δt(b) controlling ME so that(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP inan amount δE(PG) = δES(PG) + δEN(PG) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax ≤ 1; (b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g.38. The process of embodiment 37, wherein the process carried out in the chemical production unit UP is one ormore of at least one electrochemical process, at least one a high-temperature chemical process and at least one further chemical process.39. The process of embodiment 38, wherein the at least one electrochemical process comprises one or more ofproduction of hydrogen and co-production of oxygen via electrolysis of water (water electrolysis); production of chlorine and co-production of hydrogen and sodium hydroxide via electrolysis of sodium chloride in the presence of water (chlorine-alkali electrolysis); isolation of nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium via electrochemical reduction of alumina (Hall-Héroult process); production of carbon monoxide via reduction of carbon dioxide via electrolysis (eCOSTMprocess); electrochemical production of hydrocarbons from carbon dioxide and water; and electrochemical activation of nitrogen; preferably one or more of water electrolysis; chlorine-alkali electrolysis; and production of carbonmonoxide by reduction of carbon dioxide via electrolysis.40. The process of embodiment 38 or 39, wherein the at least one high-temperature process comprises one ormore of electrical heating of a cracker furnace, preferably for producing olefins and / or aromatic compounds via thermal cleavage of naphtha and / or liquefied petroleum gas (LPG) in the presence of water steam; steam- methane reforming; dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shift reaction; melting of metals and / or metal compounds including the production of virgin materials and of recycled materials; and calcination processes, preferably in one or more of catalyst field, battery field, and electronics field; methane pyrolysis; and plasma processes including use of plasma for waste treatment such as gasification, for carbon dioxide activation, for nitrogen activation, and for methane pyrolysis; preferably one or more of electrical heating of a cracker furnace and methane pyrolysis.The process of any one of embodiments 38 to 40, wherein the at least one further chemical process comprisesone or more of e-boiler application, preferably for production of steam; e-drive application, preferably for operating a compressor, more preferably operating a compressor for gas compression; application in heat pump with high coefficient of performance including closed-loop heat pump and open-loop heat pump;application in mechanical vapour compression, application in cooling for example in compressors and / or fans.The process of any one of embodiments 37 to 41, being at least partially computer-implemented.A process, preferably according to any one of embodiments 37 to 42, comprising the step of converting achemical material obtainable by or obtained by the process according to any one of embodiments 37 to 42 toobtain a product Ω.A process comprising the step of using the chemical production plant according to any one of embodiments 23to 32 to obtain a chemical material; and preferably converting the chemical material to obtain a product Ω.The process of embodiment 43 or 44, wherein the product Ω is selected from:- building block or monomer; or- polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymerproduct, preferably polymer product A; or- cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition orformulation thereof; or- agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or- active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive,human food additive, dietary supplements, aroma chemical or aroma composition; or- aqueous polymer dispersion, preferably polyurethane or polyurethane – poly(meth)acrylate hybridpolymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or- cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient orcomposition or formulation thereof; or- polymer B, polymer composition B, coating composition, other functional composition, foil, molded body,coating or coated substrate.The process of any one of embodiments 43 to 45,wherein the content of the chemical material in the product Ω is 1 weight-% or more, preferably 2 weight-% ormore, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-%or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more;and / or wherein the content of the chemical material in the product Ω is 100 weight-% or less, preferably 95 weight-% orless, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard. Short description of the figuresFigure 1 illustrates a method and a process according to the present invention as well as a production plant accordingto the present invention. Figure 1 shows an electrical storage unit USwhich is characterized by an amount of electrical energy ΔE(US) which can be released within a time interval Δt. Further, Figure 1 shows a power grid PGwhich is characterized by an amount of electrical energy ΔE(PG) which is available, i.e. which can be provided within said time interval Δt. Both USand PGare electrically connected (dashed lines) with a chemical production unit UPwhich is,among others, characterized by an amount of electrical energy ΔES(UP) characterized by a set S of electrical energyprovenance parameters as defined herein, which energy is necessary to carry out the process in UPwithin Δt. Yet further, Figure 1 shows means ME which regulate the actual amount δE(US) of electrical energy supplied from US to UPwithin Δt and the actual amount δE(PG) of electrical energy supplied from PG to UP within Δt. According to the presentinvention, in particular prior to the time interval Δt, the values of ΔES(UP), ΔE(US) and ΔE(PG) are suitably determinedand, according to the respective values, and in particular according to the value of ΔΔES = ΔES(UP) – ΔES(PG), themeans ME regulate the actual amounts δE(US) and δE(PG).Figure 2 illustrates a preferred method and a preferred process according to the present invention as well as apreferred production plant according to the present invention. Compared with Figure 1, Figure 2 additionally shows that the unit USis electrically connected also to the power grid PG(dotted line), and that, during the time interval Δt, a certain amount of electrical energy δ*E(PG) may be passed from the power grid PGto the unit US, and the actual amount of δ*E(PG) is regulated by the means ME.

Claims

Claims1. A method of optimizing a process in a chemical production plant,wherein the production plant comprises (1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected to US and beingelectrically connected to a power grid PG; (3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;wherein the process comprises supplying electrical energy to UP from at least one of US and PG; wherein the method of optimizing the process comprises (a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, whereinΔES(UP) is characterized by a share SUPthereof from at least one renewable source with SUP= 100 %; (a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and beingcharacterized by a share SPGthereof from at least one renewable sources with SPG= 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG);(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP inan amount δE(PG) = δES(PG) + δEN(PG) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);wherein f ≥ 0, g ≤ 1, and f ≤ g; wherein USis characterized by the amount of electrical energy ΔE(US) releasable within Δt; wherein PGis characterized by the amount of electrical energy ΔES(PG) available within Δt and by the amount of electrical energy ΔEN(PG) available within Δt, wherein ΔEN(PG) is characterized by a share NPGthereof from at least one renewable sources with NPG= 0 %; wherein ΔE(US) + ΔEN(PG) ≥ ΔES(UP).

2. The method of claim 1, wherein the at least one renewable source is selected from the group consisting of windenergy; solar energy; biomass energy; geothermal energy; hydropower energy including tidal energy; one or more fuels from renewable sources including one or more of ammonia, hydrogen (H2), biomethane, and bio- LNG; and a combination of two or more thereof.

3. The method of claim 1 or 2, wherein Δt is in the range of from 5 min to 24 h, preferably in the range of from 5min to 12 h, more preferably in the range of from 5 min to 6 h, more preferably in the range of from 5 min to 3 h, more preferably in the range of from 10 min to 2 h.

4. The method of any one of claims 1 to 3, wherein the electrical storage unit US is a stationary energy storage unitcomprising one or more of at least one battery on sodium-sulfur basis (NaS battery) and at least one battery based on lithium iron phosphate cathode material (LFP battery), preferably at least one NaS battery; wherein the electrical storage unit US has a capacity preferably in the range of from 5.000 to 750.000 kWh, more preferably in the range of from 10.000 to 600.000 kWh, more preferably in the range of from 100.000 to 600.000 kWh, more preferably in the range of from 200.000 to 550.000 kWh; wherein the electrical storage unit UShas a power, in kW, sufficient preferably for 20 to 100 %, more preferably for 30 to 100 %, more preferably from 40 to 100 %, more preferably from 50 to 100 % of the chemical production unit UP.

5. The method of any one of claims 1 to 4, whereinf = qE ^ f(min);g = qE ^ g(max);with f< g, more preferably 0.80 ≤ f(min) ≤ 1, preferably 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1;g(max) = 1;0 ≤ qE ≤ 1.

6. The method of claim 5, wherein qE = 1.

7. The method of claim 5, wherein ΔES(PG) is further characterized by cost factors, ΔEN(PG) is furthercharacterized by cost factors, and ΔE(US) is characterized by cost factors, wherein determining for a time interval Δt which starts at a time t according to (a) further comprises (a.4) determining the parameter qE, comprising(4.1) determining the cost factors of ΔES(PG), the cost factors of ΔEN(PG) and the cost factors ofΔE(US); (4.2) determining, based on the cost factors determined according to (4.1), the costs of ΔES(PG),ΔEN(PG) and ΔE(US); (4.3) determining, based on the costs of ΔES(PG), ΔEN(PG) and ΔE(US) determined according to(4.2) the parameter qE, wherein the higher the costs of ΔES(PG) relative to the costs of ΔEN(PG) and ΔE(US), the smaller qE; wherein, if the costs of ΔES(PG) are higher than the costs of ΔEN(PG) and ΔE(US), it is preferred that 0 ≤ qE < 1,preferably 0 ≤ qE ≤ 0.5, more preferably 0 ≤ qE < 0.5, more preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE ≤0.1, more preferably qE = 0.

8. The method of any one of claims 1 to 7, wherein 0 ≤ δEN(PG) ≤ δE(US), preferably0 ≤ δEN(PG) < δE(US), more preferably δEN(PG) = 0.

9. The method of any one of claims 1 to 8,wherein the electrical energy storage unit US according to (1) is further electrically connected to the power grid PG according to (2); wherein the means ME are means further for regulating the amount of electrical energy supplied from PG to US; wherein the process comprises supplying electrical energy to UP from at least one of US and PG and optionally further from PG to US; wherein according to (b), the method of optimizing the process further comprises controlling MEso that the process further comprises supplying within Δt electrical energy from PGto USin an amount δ*E(PG) = δ*ES(PG) + δ*EN(PG), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax≤ 1; (b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG);(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax ≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g.

10. The method of any one of claims 1 to 9, wherein the process carried out in the chemical production unit UPcomprises one or more of at least one electrochemical process, at least one a high-temperature chemical process and at least one further chemical process; wherein the at least one electrochemical process preferably comprises one or more of production of hydrogenand co-production of oxygen via electrolysis of water (water electrolysis); production of chlorine and co- production of hydrogen and sodium hydroxide via electrolysis of sodium chloride in the presence of water (chlorine-alkali electrolysis); isolation of nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium via electrochemical reduction of alumina (Hall-Héroult process); production of carbon monoxide via reduction of carbon dioxide via electrolysis (eCOSTMprocess); electrochemical production of hydrocarbons from carbon dioxide and water; and electrochemical activation of nitrogen; more preferably one or more of water electrolysis; chlorine-alkali electrolysis; and production of carbon monoxide byreduction of carbon dioxide via electrolysis; wherein the at least one high-temperature process preferably comprises one or more of electrical heating of acracker furnace, preferably for producing olefins and / or aromatic compounds via thermal cleavage of naphthaand / or liquefied petroleum gas (LPG) in the presence of water steam; steam-methane reforming; dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shift reaction; melting of metals and / or metal compounds including the production of virgin materials and of recycled materials; and calcination processes, preferably in one or more of catalyst field, battery field, and electronics field; methanepyrolysis; and plasma processes including use of plasma for waste treatment such as gasification, for carbon dioxide activation, for nitrogen activation, and for methane pyrolysis; more preferably one or more of electrical heating of a cracker furnace and methane pyrolysis; wherein the at least one further chemical process preferably comprises one or more of e-boiler application,preferably for production of steam; e-drive application, preferably for operating a compressor, more preferably operating a compressor for gas compression; application in heat pump with high coefficient of performance including closed-loop heat pump and open-loop heat pump; application in mechanical vapour compression,application in cooling for example in compressors and / or fans.

11. The method of any one of claims 1 to 10, being at least partially computer-implemented;wherein the production plant preferably further comprises (4) a computer-supported system for controlling at least the means ME according to (3);wherein the computer-supported system is preferably further used for determining at least one of ΔES(UP) according to (a.1), ΔES(PG) according to (a.2), ΔΔES according to (a.3), and preferably determining the parameter qE, according to (a.4) as defined in claim 7.

12. A chemical production plant, preferably as referred to in any one of claims 1 to 11, comprising(1) an electrical energy storage unit US;(2) an electrical energy consuming chemical production unit UP being electrically connected with the unit USand being electrically connected with a power grid PG; (3) means ME for regulating the amount of electrical energy supplied from US to UP and from PG to UP;(4) preferably a computer-supported system for controlling at least the means ME.according to (3);wherein the unit USis preferably further electrically connected with the power grid PG; wherein the means MEare preferably means further for regulating the amount of electrical energy supplied from PGto US.

13. A process as referred to in any one of claims 1 to 11 being carried out in a chemical production plant accordingto claim 12, wherein for a time interval Δt of the process, the process comprises supplying electrical energy- from PG to UP in an amount δE(PG);- from US to UP in an amount δE(US);- preferably from PG to US in an amount δ*E(PG);the process further comprises (a) determining for a time interval Δt which starts at a time t(a.1) the amount of electrical energy ΔES(UP) to be consumed in the process in UP within Δt, whereinΔES(UP) is characterized by a share SUP thereof from at least one renewable source with SUP = 100 %; (a.2) the amount of electrical energy ΔES(PG) being available from PG within Δt and beingcharacterized by a share SPG thereof from at least one renewable sources with SPG = 100 %; (a.3) the value ΔΔES = ΔES(UP) - ΔES(PG); and the process further comprises for said time interval Δt;(b) controlling ME so that the process further comprises supplying within Δt electrical energy from PG to UP inan amount δE(PG) = δES(PG) + δEN(PG) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔES ≤ 0,(1.1) f ^ ΔES(UP) ≤ δES(PG) ≤ g ^ ΔES(UP);(1.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(1.3) δ*ES(PG) = x ^ [ΔES(PG) - δES(PG)];with 0 ≤ x ≤ xmax, xmax≤ 1; (b.2) if ΔΔES > 0,(2.1) f ^ ΔES(PG) ≤ δES(PG) ≤ g ^ ΔES(PG);(2.2) δE(US) + δEN(PG) = ΔES(UP) - δES(PG); and preferably(2.3 δ*ES(PG) = y ^ [ΔES(PG) - δES(PG)];with 0 ≤ y ≤ ymax, ymax≤ 1; wherein f ≥ 0, g ≤ 1, and f ≤ g.

14. A computer program comprising instructions which, when the program is executed by the computer-supportedsystem as defined in claims 11 and 12, cause the system to perform the method according to any one of claims1 to 11.

15. A process, preferably according to claim 13, comprising the step of converting a chemical material obtainableby or obtained by the process according to claim 13 to obtain a product product Ω; and / or a process comprisingthe step of using the chemical production plant according to claim 12 to obtain a chemical material; and preferably converting the chemical material to obtain a product Ω.

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