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 (1) an electrical energy storage unit US; (2) a unit UR for producing electrical energy from at least one renewable source; (3) an electrical energy consuming chemical production unit UP being electrically connected with the unit US and being electrically connected with the unit UR; means ME for regulating the amount of electrical energy supplied from US to UP and from UR to UP; wherein the process comprises supplying electrical energy to UP from at least one of US and UR; wherein the method of optimizing the process comprises (a) determining for a time interval Δt which starts at a time t the amount of electrical energy ΔER(UP) from at least one renewable source to be consumed in the process in UP within Δt; the amount of electrical energy ΔER(UR) being available from UR within Δt; the value ΔΔER = ΔER(UP) – ΔER(UR); (b) controlling ME so that the process further comprises supplying within Δt electrical energy from UR to UP in an amount δER(UR) and from US to UP in an amount δE(US); wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δt and UR is characterized by the amount of electrical energy ΔER(UR) available within Δt, and wherein ΔER(UR) + ΔE(US) ≥ ΔER(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 the production plant comprises an electrical energy storage unit US, a unit UR forproducing electrical energy from at least one renewable source, an electrical energy consuming chemical production unit UPbeing electrically connected with the unit USand being electrically connected with the unit UR, and means MEfor regulating the amount of electrical energy supplied from USto UPand from URto UP. Further, the present invention relates to the process carried outin 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 priceof the electricity will occur during operation of the plant due to increasing proportions ofrenewable energies in the electricity grid. In particular, but not only in less developed electricity 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, byreducing the combustion of 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 storagecomprehensive 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) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electrically connectedwith the unit US and being electrically connected with the unit UR;(4) means ME for regulating the amount of electrical energy supplied from US to UP and from URto UP; wherein the process comprises supplying electrical energy to UP from at least one of US and UR; 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 ΔER(UP) from at least one renewable source to beconsumed in the process in UP within Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(b) controlling ME so that the process further comprises supplying within Δt electrical energyfrom UR to UP in an amount δER(UR) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);wherein f ≥ 0, g ≤ 1, and f ≤ g; wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δt and URis characterized by the amount of electrical energy ΔER(UR) available within Δt, and wherein ΔER(UR) + ΔE(US) ≥ ΔER(UP).In the formulae in accordance with the present invention, the operator “ ^ “ represents amultiplicator. For example, in formula (1.1), “f ^ ΔER(UP)” relates to f being multiplied withΔER(UP), and “g ^ ΔER(UP)” relates to g being multiplied with ΔER(UP).Preferably, according to the present invention, f < g.Further according to the present invention, providing energy from a unit URfor producingelectrical energy from at least one renewable source to an electrical energy storage unit UScorresponds to an amount ΔER(UR). Furthermore, providing energy from an electrical energy storage unit USto an electrical energy consuming chemical production unit UPcorresponds to anamount ΔE(US). For example, as will be outlined below, Figure 1 shows an embodiment withmeans MEwhich regulate the actual amount δE(US) of electrical energy supplied from USto UPwithin Δt and the actual amount δER(UR) of electrical energy supplied from UR to UP within Δt.According to the present invention, in particular prior to the time interval Δt, the values ofΔER(UP), ΔER(UR) and ΔE(US) are suitably determined and, according to the respective values,and in particular according to the value of ΔΔER = ΔER(UP) – ΔER(UR), the means ME regulate theactual amounts δE(US) and δER(UR). Further according to the present invention, it may be preferred that the unit US is furtherelectrically connected with the unit UR as illustrated, for example, in Figure 2. This principallyallows for supplying electrical energy from the unit UR to the storage unit US, i.e. at least partiallycharging US with electrical energy prepared from at least one renewable source. In this case, it ispreferred that the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US. The process, in this case, further comprises supplying electrical energy to UP from at least one of US and UR, and to US from UR; and according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR).Further according to the present invention, it may be preferred that the electrical energy consuming chemical production unit UPis further electrically connected with a power grid PGasillustrated, for example, in Figure 3. This principally allows for supplying electrical to UP not onlyfrom UR, but also from the power grid PGwhich may become necessary if, for example, URmay not produce sufficient electrical energy to meet the respective electrical energy demand of UPwithin Δt. In this case, it is preferred that the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from PGto UP. The process, in this case,further comprises supplying electrical energy to UP from at least one of US, UR and PG; andaccording to (b), the method of optimizing the process comprises controlling MEso that the process further comprises supplying within Δt electrical energy from URto UPin an amount δER(UR), from USto UPin an amount δE(US), and further from PGto UPin an amount δE(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);wherein PG is characterized by the amount of electrical energy ΔE(PG) releasable within Δt and wherein ΔER(UR) + ΔE(US) + ΔE(PG) ≥ ΔER(UP).Further according to the present invention, it may be preferred that the unit US is furtherelectrically connected with the power grid PG as illustrated, for example, in Figure 4. This principally allows for supplying electrical energy from the power grid PG to the storage unit US, i.e. at least partially charging US with electrical energy provided by the grid. In this case, it is preferred that the means ME according to (4) are means further for regulating the amount of electrical energy supplied from PG to US. The process, in this case, further comprises supplying electricalenergy to UP from at least one of US, UR and PG, and to US from PG; and according to (b), themeans ME are controlled so that the process further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) δ*E(PG) ≥ 0.Further according to the present invention, it may be preferred that the unit US is furtherelectrically connected with the unit URas illustrated, for example, in Figure 5. As indicated above, this principally allows for supplying electrical energy from the unit URto the storage unit US, i.e. atleast partially charging USwith electrical energy prepared from at least one renewable source. In this case, it is preferred that the means MEaccording to (4) are means further for regulating theamount of electrical energy supplied from UR to US. The process, in this case, further comprisessupplying electrical energy to UPfrom at least one of US, URand PG, and to USfrom UR; and according to (b), the means MEare controlled so that the process further comprises supplying within Δt electrical energy from URto USin an amount δ*ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR).Further according to the present invention, it may be preferred that the unit US is furtherelectrically connected with the unit UR and the power grid PG as illustrated, for example, in Figure 6. As indicated above, this principally allows for supplying electrical energy from the unit UR to the storage unit US, i.e. at least partially charging US with electrical energy prepared from at least one renewable source, and additionally or alternatively, allows for supplying electrical energy from the power grid PG to the storage unit US, i.e. at least partially charging US with electrical energy provided by the grid. In this case, it is preferred that the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US and the amount ofelectrical energy supplied from PG to US. The process, in this case, comprises supplying electricalenergy to UP from at least one of US, UR and PG, and to US from at least one of UR and PG; andaccording to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), and further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0.Further according to the present invention, it may be preferred that the unit US is furtherelectrically connected with the unit URand the power grid PGand the unit URis further electricallyconnected to the power grid PG as illustrated, for example, in Figure 7. Generally, it can happenthat electrical energy provided by the power grid PGhas an advantage compared with electrical energy produced in UR. A conceivable advantage, for example, could be that the electrical energy provided by PGis also electrical energy from at least one renewable source and is, however, cheaper than the electrical energy produced in UR. In this case, it may be preferred to supply at least a part of the electrical energy necessary for UPwithin Δt from PGand suitably store at least a part of the electrical energy produced in UR in the storage unit US. If the unit US is sufficiently charged, electrical energy produced in UR can be supplied to the power grid PG. In this case, it is preferred that the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PG to USand the amount of electrical energy supplied from UR to PG. The process, in this case, comprisessupplying electrical energy to UP from at least one of US, UR and PG, and to US from at least oneof UR and PG, and to PG from UR; and according to (b), the means ME are controlled so that theprocess further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG), and further comprises supplying within Δt electrical energy from UR to PG in an amount δ**ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0.According to the present invention, according to (a.1), the amount of electrical energy ΔER(UP) tobe consumed in the process in UP within Δt is determined. This amount ΔER(UP) is to beunderstood 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 UPwithin 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 isrealized in a suitable manner.According to (1.1) and (2.1), the method of the present invention allows for varying both theminimum amount and the maximum amount of δER(UR) via the factors f and g. In particular, thesefactors are defined as f = qE ^ f(min) and g = qE ^ g(max). As far as these definitions areconcerned, 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, more preferably0.98 ≤ f(min) ≤ 1, more preferably 0.99 ≤ f(min) ≤ 1. Preferably, g(max) = 1. This means thataccording to the preferred values above, and if the factor qE = 1, the amount of δER(UR) passedfrom UR to UP within Δt is- in case ΔΔER ≤ 0:preferably in the range of from 80 % to 100 % of ΔER(UP), more preferably in the range of from 90 % to 100 % of ΔER(UP), more preferably in the range of from 95 % to 100 % of ΔER(UP), more preferably in the range of from 97 % to 100 % of ΔER(UP), more preferably in the range of from 98 % to 100 % of ΔER(UP), more preferably in the range of from 99 % to 100 % of ΔER(UP); and- in case ΔΔER > 0:preferably in the range of from 80 % to 100 % of ΔER(UR), more preferably in the range of from 90 % to 100 % of ΔER(UR), more preferably in the range of from 95 % to 100 % of ΔER(UR), more preferably in the range of from 97 % to 100 % of ΔER(UR), more preferably in the range of from 98 % to 100 % of ΔER(UR), more preferably in the range of from 99 % to 100 % of ΔER(UR).According to the present invention, the electrical energy ΔER(UR) which is available within Δt isprepared 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 ΔΔER ≤ 0, therefore, this means that the energy demand ΔER(UP) will be met essentially via ΔER(UR), which means that qE= 1. However, when running the production plant according to the present invention, it is alsoconceivable that, although the use of ΔER(UR) would appear to be advantageous if assessedexclusively from an ecological perspective, the costs of ΔER(UR), compared to the costs of ΔE(US)and preferably ΔE(PG), may render the use of ΔER(UR) less advantageous. Since in most cases,both the ecological and the economical boundary conditions in terms of the supply wilt electrical energy will play a decisive role when running a chemical production plant, the method accordingto the present invention allows for respectively varying the amount of ΔER(UR) depending on thecosts via the factor qE. Therefore, preferably, the present invention also relates to the method as described above, wherein ΔER(UR) is further characterized by a cost factor, ΔE(US) is further characterized by a cost factor, and preferably ΔE(PG) is characterized by a cost 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 ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1), the costs ofΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG)determined according to (4.2) the parameter qE, wherein the higher the costs of ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE. The term “cost factors” of a given amount of energy, such as ΔER(UR), refers to the sum of allindividual cost items incurred in the provision of said amount of electrical energy. The term“costs” of a given amount of energy, such as ΔER(UR), refers to the total costs ΔER(UR).In case the costs of ΔER(UR) are higher than the costs of ΔE(US) and preferably ΔE(PG), it ispreferred that 0 ≤ qE < 1, more preferably 0 ≤ qE ≤ 0.5, more preferably 0 ≤ qE < 0.5, morepreferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE ≤ 0.1. If it advisable for the process of the presentinvention to be carried out in a meaningful manner, it may be preferred that qE = 0, which meansthat according to (b.1), the total amount of electrical energy provided to UP within Δt is suppliedvia δE(US) + δE(PG).Further according to the present invention, it may be preferred that ΔE(US) = ΔER(US) + ΔEN(US) with 0 ≤ ΔER(US) ≤ ΔE(US), wherein ΔER(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 %. Further according to the present invention, it may be preferred that ΔE(PG) = ΔER(PG) + ΔEN(PG)with 0 ≤ ΔE (PG) ≤ ΔE(PG), wherein ΔER(PG) is characterized by a share SPG thereof from at leastone renewable source with SPG= 100 % and ΔEN(PG) is characterized by a share NPGthereof from at least one renewable source with NPG= 0 %.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 5 min to 3 h, more preferably in the range of from 10min to 2 h. By way of example, shorter periods of time may be in the range of from 5 min to 30min, and longer periods of time may be in the range of from 0.5 h to 2 h or from 0.5 to 1 h.Preferably, the sum of all successive time intervals Δt is the runtime of the process of the presentinvention which is controlled 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 the amounts of electrical energy, for example ΔER(UP),ΔER(UR), ΔΔER, and the respective values of parameters such as f and g, including qE, aredetermined and the process is controlled by the method of the present invention accordingly. i.e.the respective amounts of δER(UR), δE(US), δE (PG), and – optionally or preferably – δ*ER(UR),δ**ER(UR) and δ*E(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 desired electrical 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 storageunit which, more preferably, comprises 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). 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 US has 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 to100 % 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 USby 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. In particular, according to the present invention, it is possible that two or moredifferent 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 purificationprocesses of any kind, and in general all conceivable processes and combination of process forwhich 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 chemical process and at least one further chemical process.The at least one electrochemical process preferably comprises one or more of production ofhydrogen 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; more preferably one ormore of water electrolysis; chlorine-alkali electrolysis; and production of carbon monoxide byreduction of carbon dioxide via electrolysis.The at least one high-temperature process preferably comprises one or more of electrical heatingof 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-boilerapplication, preferably for production of steam; e-drive application, preferably for operating acompressor, 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 heatpump; application in mechanical vapour compression, application in cooling for example incompressors and / or fans. Preferably according to the present invention, the term “at least one renewable source” refers toat least one energy source which is selected from the group consisting of wind energy; solarenergy; 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 thermalenergy (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 windenergy.- Geothermal energy may comprise one or more or dry steam energy, flash steam energy,and binary cycle energy.- Biomass energy may be derived from liquid and or solid biomass and may include materialsproduced by growth of microorganisms, plants, and animals. As far as biomass species are concerned, those are especially preferred which are comprised in waste material and / or arenot 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 woodtar which in turn is produced during the processing of wood for pulping and papermaking; -- natural sources where aromatic hydrocarbons can be found certain plants, such asguaiacum, and in certain soils, such as those with a high organic matter content; -- lignocellulosic biomass;-- sources comprising furan which in turn is obtained from industrial sugars whichpreferably are not in competition with the food chain.- Hydropower energy may be derived from flowing water, and suitable hydropower facilitiesmay be based on one or more of impoundment, diversion, and pumped storage.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 partially computer-implemented. Morepreferably, the production plant of the present invention further comprises(5) a computer-supported system for controlling at least the means ME according to (4).In particular, this computer-supported system is further used for determining at least one ofΔER(UP) according to (a.1), ΔER(UR) according to (a.2), ΔΔER according to (a.3), preferablydetermining the parameter qE, according to (a.4) as defined in embodiment 8, and morepreferably also the parameters f, g, and qE. Yet further, the present invention relates to and describes a chemical production plant, preferablya chemical production plant referred to hereinabove in the context of the description of thepresent invention, the chemical production plant comprising(1) an electrical energy storage unit US;(2) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electrically connectedwith the unit US and being electrically connected with the unit UR;(4) means ME for regulating the amount of electrical energy supplied from US to UP and from URto UP; wherein the unit US is preferably further electrically connected with the unit UR and the power grid PG and the unit UR is preferably further electrically connected to the power grid PG, and wherein the means ME according to (4) are preferably means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PG to US andpreferably the amount of electrical energy supplied from UR to PG.Concerning the chemical production plant of the present invention and with regard to generallyconceivable units US, UR and 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 chemicalproduction plant as such, in particular embodiments 25 to 35.Still further, the present invention relates to and describes a process, preferably a chemicalproduction plant referred to hereinabove in the context of the description of the present invention,more preferably a process being carried out in a chemical production plant referred tohereinabove, wherein for a time interval Δt of the process, preferably for at least two time intervalΔt of the process, more preferably for all time intervals Δt of the process, the process comprisessupplying electrical energy- from UR to UP in an amount δER(UR);- from US to UP in an amount δE(US);- preferably from UR to US in an amount δ*ER(UR);- preferably from PG to UP in an amount δE(PG);- preferably from PG to US in an amount δ*E(PG);- preferably from UR to PG in an amount δ**ER(UR);and the process further comprises(a) determining for said time interval Δt(a.1) the amount of electrical energy ΔER(UP) from at least one renewable source to beconsumed in the process in UPwithin Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(a.4) preferably determining the parameter qE, comprising(4.1) determining the cost factors of ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1), thecosts of ΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG)determined according to (4.2) the parameter qE, wherein the higher the costs of ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE; wherein, if the costs of ΔER(UR) are higher than the costs of ΔE(US) and preferablyΔE(PG), it is preferred that 0 ≤ qE < 0.5, preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE≤ 0.1, more preferably qE = 0and the process further comprises for said time intervalΔt;(b) controlling ME so that(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(2.4) δ*E(PG) ≥ 0;wherein f= qE ^ f(min);g = qE ^ g(max);with 0.80 ≤ f(min) ≤ 1, 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1;g(max) = 1;0 ≤ qE≤ 1.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 sectionhereinunder, specifically being directed to the chemical production plant as such, in particularembodiments 40 to 45. 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 inembodiment 35, cause the system to perform the method as described herein, such as in any one of embodiments 1 to 24. Still further, the present invention relates to a non-transient computer-readable mediumcontaining instructions which, when executed by one or more processors, cause the one or moreprocessors to perform the computer program as described herein, such as in embodiment 36.Still further, the present invention relates to the use of the production plant as described herein,such as in any one of embodiments 25 to 35, for carrying out the method as described herein,such as in any one of embodiments 1 to 24. Still further, the present invention relates to a method of using the production plant as describedherein, such as in any one of embodiments 25 to 35, for carrying out the method as describedherein, such as in any one of embodiments 1 to 24. 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 orobtained by the process as described herein to obtain a product product Ω. Further to this aspect,the present invention relates to the step of using the chemical production plant as describedherein to obtain a chemical material; and preferably converting the chemical material to obtain aproduct Ω.Preferably, the product Ω is selected from:- building block or monomer; or- polymer, preferably polymer A, polymer composition, preferably polymer composition A, orpolymer product, preferably polymer product A; or- cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide orcomposition or formulation thereof; or- agrochemical composition, agrochemical formulation auxiliary or agrochemically activeingredient; or- active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animalfeed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or- aqueous polymer dispersion, preferably polyurethane or polyurethane – poly(meth)acrylatehybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or- cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredientor composition or formulation thereof; or- polymer B, polymer composition B, coating composition, other functional composition, foil,molded body, coating or 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 2weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / orthat the content of the chemical material in the product Ω is 100 weight-% or less, preferably 95weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less,more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or massbalance and / or book and claim chain of custody models, preferably based on mass balance,preferably the International Sustainability and Carbon Certification (ISCC) standard. The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

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

[1000] to

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

[1000] to

[8005] . The term “building block”, as used in the context of the product 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 higherstructural complexity and / or higher molecular weight than the building block on which thesecondary 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 of phosgene, polyisocyanates and propyleneoxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluenediisocyanate (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 or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1. The term “polymer composition A”, as used in the context of the product 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 polymerproduct 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 cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used in the context of the product 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 usedescaling compound”, as used in the context of the product Ω herein, comprises non-phosphatebased 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 “industrial use 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 usepolymer, industrial use surfactant, descaling compound and / or industrial use biocide are definedin more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrialuse 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 ingredientsand auxiliaries are described in more detail in Reference RF1, paragraph

[4001] . Theagrochemical 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 Ω herein, comprises substances that provide pharmacological activity or otherdirect effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect thestructure 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) methyl ester and 1,2-propandiol and beverage stabilizers,such as polyvinylpyrrolidone-polymer or polyvinylimidazole / 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 Ωherein, comprise a volatile organic substance with a molecular weight between 70-250 g / molcomprising 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 andbut 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 detailin 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 composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curablepolyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsionpolymer”, 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-curablepolyurethane(s) is / are defined in more detail in the section

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

[6016] of Reference RF1. The term “polymeric dispersant”, as used in the context of the product 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) aredefined in more detail in the following sections of Reference RF1:section

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

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

[6006] entitled “Binders for paper coating”section

[6007] entitled “Binders for fiber bonding” section

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

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

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

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

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

[6019] 100% curable coating 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 making pressure-sensitive self-adhesive articles” of Reference RF1. Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

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

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

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

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

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

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

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

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

[6020] of Reference RF1. The term “inorganic binder composition” comprising the polymeric 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 inmore detail in section

[6021] of Reference RF1 entitled “Inorganic binder compositionscomprising the polymeric dispersant and their use”. Specific building material 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 any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term “UV filter”, as used in the context of the product 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 cosmeticsurfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers topersonal care and / or cosmetic compositions or formulations defined in more detail in paragraph

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

[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 thecontext 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 is mentioned, 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) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electricallyconnected with the unit US and being electrically connected with the unit UR; (4) means ME for regulating the amount of electrical energy supplied from US to UP andfrom UR to UP; wherein the process comprises supplying electrical energy to UP from at least one of US and UR; 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 ΔER(UP) from at least one renewable source tobe consumed in the process in UP within Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(b) controlling ME so that the process further comprises supplying within Δt electricalenergy from URto UPin an amount δER(UR) and from USto UPin an amount δE(US), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);wherein f ≥ 0, g ≤ 1, and f ≤ g;wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δtand UR is characterized by the amount of electrical energy ΔER(UR) available within Δt, andwherein ΔER(UR) + ΔE(US) ≥ ΔER(UP).The method of embodiment 1, wherein the unit US is further electrically connected with theunit UR, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from URto US; wherein the process comprises supplying electrical energy to UP from at least one of US and UR, and to US from UR; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR).The method of embodiment 1, wherein according to (3), the electrical energy consumingchemical production unit UP is further electrically connected with a power grid PG and the means ME according to (4) are means further for regulating the amount of electrical energy supplied from PG to UP; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG; wherein according to (b), the method of optimizing the process comprises controlling ME so that the process further comprises supplying within Δt electrical energy from URto UPin an amount δER(UR), from USto UPin an amount δE(US), and further from PGto UPin an amount δE(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);wherein PGis characterized by the amount of electrical energy ΔE(PG) releasable within Δt and wherein ΔER(UR) + ΔE(US) + ΔE(PG) ≥ ΔER(UP).The method of embodiment 3, wherein the unit US is further electrically connected with thepower grid PG, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from PGto US; wherein the process comprises supplying electrical energy to UPfrom at least one of US, URand PG, and to USfrom PG; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) δ*E(PG) ≥ 0.The method of embodiment 3, wherein the unit US is further electrically connected with theunit UR, and the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG, and to US from UR; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR).The method of embodiment 3, wherein the unit US is further electrically connected with theunit URand the power grid PG, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from URto USand the amount of electrical energy supplied from PGto US; wherein the process comprises supplying electrical energy to UPfrom at least one of US, URand PG, and to USfrom at least one of URand PG; wherein according to (b), the means MEare controlled so that the process further comprises supplying within Δt electrical energy from URto USin an amount δ*ER(UR), and further comprises supplying within Δt electrical energy from PGto USin an amount δ*E(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0.The method of embodiment 3, wherein the unit US is further electrically connected with theunit UR and the power grid PG and the unit UR is further electrically connected to the power grid PG, and the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PG to US and the amount of electrical energy supplied from UR to PG; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG, and to US from at least one of UR and PG, and to PG from UR; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), further comprises supplying within Δt electrical energy from PGto USin an amount δ*E(PG), and further comprises supplying within Δt electrical energy from URto PGin an amount δ**ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0.8. The method of any one of embodiments 1 to 7, whereinf = qE ^ f(min);g = qE ^ g(max);with 0.80 ≤ f(min) ≤ 1, 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1; g(max) = 1;0 ≤ qE ≤ 1.9. The method of embodiment 8, wherein qE = 1.10. The method of embodiment 8, wherein ΔER(UR) is further characterized by a cost factor,ΔE(US) is further characterized by a cost factor, and preferably ΔE(PG) is characterized by a cost 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 ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1), thecosts of ΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG)determined according to (4.2) the parameter qE, wherein the higher the costs of ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE; wherein, if the costs of ΔER(UR) are higher than the costs of ΔE(US) and preferablyΔE(PG), it is preferred that 0 ≤ qE < 1, preferably 0 ≤ qE ≤ 0.5, more preferably0 ≤ qE < 0.5, more preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE ≤ 0.1, morepreferably qE = 0.11. The method of any one of embodiments 1 to 10, wherein ΔE(US) = ΔER(US) + ΔEN(US) with0 ≤ ΔER(US) ≤ ΔE(US), wherein ΔER(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 %.The method of any one of embodiments 1 to 11, wherein ΔE(PG) = ΔER(PG) + ΔEN(PG) with0 ≤ ΔER(PG) ≤ ΔE(PG), wherein ΔER(PG) is characterized by a share SPGthereof from at least one renewable source with SPG= 100 % and ΔEN(PG) is characterized by a share NPGthereof from at least one renewable source with NPG= 0 %.The method of any one of embodiments 1 to 12, wherein Δt is in the range of from 5 min to24 h, 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 5 min to 3 h, more preferably in the range of from 10 min to 2 h.The method of any one of embodiments 1 to 13, wherein the electrical storage unit USaccording to (1) is a stationary energy 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.The method of any one of embodiments 1 to 14, wherein the electrical storage unit USaccording to (1) has a capacity 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; wherein the electrical storage unit US has 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 according to (3).The method of any one of embodiments 1 to 15, wherein the electrical storage unit USaccording to (1) is a modular system, the method comprising increasing and / or decreasing the capacity of US bay adding or removing one or more electrical storage modules depending on the varying consumption of electrical energy in the chemical production unit UP according to (3).The method of any one of embodiments 1 to 16, wherein the process carried out in thechemical production unit UPaccording to (3) comprises one or more of at least one electrochemical process, at least one a high-temperature chemical process and at least one further chemical process.The method of embodiment 17, wherein the at least one electrochemical processcomprises one or more of production of hydrogen and co-production of oxygen viaelectrolysis of water (water electrolysis); production of chlorine and co-production ofhydrogen 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 temperaturedistillation (air separation); production of aluminium via electrochemical reduction ofalumina (Hall-Héroult process); production of carbon monoxide via reduction of carbondioxide via electrolysis (eCOSTM process); electrochemical production of hydrocarbons fromcarbon dioxide and water; and electrochemical activation of nitrogen; preferably one ormore of water electrolysis; chlorine-alkali electrolysis; and production of carbon monoxideby reduction of carbon dioxide via electrolysis.The method of embodiment 17 or 18, wherein the at least one high-temperature processcomprises 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 liquefiedpetroleum gas (LPG) in the presence of water steam; steam-methane reforming;dehydrogenation reaction, preferably of propane and / or butane; reverse water-gas shiftreaction; melting of metals and / or metal compounds including the production of virginmaterials and of recycled materials; and calcination processes, preferably in one or more ofcatalyst field, battery field, and electronics field; methane pyrolysis; and plasma processesincluding use of plasma for waste treatment such as gasification, for carbon dioxideactivation, for nitrogen activation, and for methane pyrolysis; preferably one or more ofelectrical heating of a cracker furnace and methane pyrolysis.The method of any one of embodiments 17 to 19, wherein the at least one further chemicalprocess 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 inmechanical vapour compression, application in cooling for example in compressors and / orfans.The method of any one of embodiments 1 to 20, wherein the at least one renewable sourcefor the unit URaccording to (2) comprise at least one of solar energy, wind energy, hydro energy, tidal energy, geothermal energy, biomass energy, ammonia obtained fromrenewable sources, biomethane, bio-LNG, and H2 obtained from renewable sources.The method of any one of embodiments 1 to 21, being at least partially computer-implemented.23. The method of embodiment 22, wherein the production plant further comprises(5) a computer-supported system for controlling at least the means ME according to (4).24. The method of embodiment 23, wherein the computer-supported system is further used fordetermining at least one of ΔER(UP) according to (a.1), ΔER(UR) according to (a.2), ΔΔERaccording to (a.3), and preferably qE according to (a.4).25. A chemical production plant, preferably as referred to in any one of embodiments 1 to 24,comprising (1) an electrical energy storage unit US;(2) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electricallyconnected with the unit US and being electrically connected with the unit UR; (4) means ME for regulating the amount of electrical energy supplied from US to UP andfrom UR to UP; wherein the unit US is preferably further electrically connected with the unit UR and the power grid PG and the unit UR is preferably further electrically connected to the power grid PG, and wherein the means ME according to (4) are preferably means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PG to US and preferably the amount of electrical energy supplied from UR to PG.26. The production plant of embodiment 25, wherein the electrical storage unit US according to(1) is a stationary energy 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.27. The production plant of embodiment 25 or 26, wherein the electrical storage unit USaccording to (1) has a capacity 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.28. The production plant of any one of embodiments 25 to 27, wherein the electrical storageunit US according to (1) has a power, in kW, sufficient for 20 to 100 %, preferably for 30 to100 %, more preferably from 40 to 100 %, more preferably from 50 to 100 % of thechemical production unit UPaccording to (3).The production plant of any one of embodiments 25 to 28, wherein the electrical storageunit USaccording to (1) is a modular system, 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 UPaccording to (3).The production plant of any one of embodiments 25 to 29, wherein the chemical productionunit UPaccording to (3) is a unit for carrying 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.The production plant of embodiment 30, wherein the at least one electrochemical processcomprises 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); 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 ormore of water electrolysis; chlorine-alkali electrolysis; and production of carbon monoxideby reduction of carbon dioxide via electrolysis.The production plant of embodiment 30 or 31, wherein the at least one high-temperatureprocess comprises one or more of electrical heating of a cracker furnace, preferably forproducing 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.33. The production plant of any one of embodiments 30 to 32, wherein the at least one furtherchemical process comprises one or more of e-boiler application, preferably for production ofsteam; 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 / orfans.34. The production plant of any one of embodiments 25 to 33, wherein the unit UR according to(2) is a unit for producing electrical energy from one or more at least one renewable sourceselected 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.35. The production plant of any one of embodiments 25 to 34, further comprising(5) a computer-supported system for controlling at least the means ME according to (4).36. A computer program comprising instructions which, when the program is executed by thecomputer-supported system as defined in embodiment 35, cause the system to perform themethod of any one of embodiments 1 to 24.37. A non-transient computer-readable medium containing instructions which, when executedby one or more processors, cause the one or more processors to perform the program according to embodiment 36.38. Use of the production plant according to any one of embodiments 25 to 35 for carrying outthe method according to any one of embodiments 1 to 24.39. A method of using the production plant according to any one of embodiments 25 to 35 forcarrying out the method according to any one of embodiments 1 to 24.40. A process as referred to in any one of embodiments 1 to 24 being carried out in a chemicalproduction plant according to any one of embodiments 25 to 35, wherein for a time interval Δt of the process, the process comprises supplying electrical energy- from UR to UP in an amount δER(UR);- from US to UP in an amount δE(US);- preferably from UR to US in an amount δ*ER(UR);- preferably from PG to UP in an amount δE(PG);- preferably from PG to US in an amount δ*E(PG);- preferably from UR to PG in an amount δ**ER(UR);the process further comprises(a) determining for said time interval Δt(a.1) the amount of electrical energy ΔER(UP) from at least one renewable source tobe consumed in the process in UPwithin Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(a.4) preferably determining the parameter qE, comprising(4.1) determining the cost factors of ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1),the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferablyΔE(PG) determined according to (4.2) the parameter qE, wherein thehigher the costs of ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE; wherein, if the costs of ΔER(UR) are higher than the costs of ΔE(US) andpreferably ΔE(PG), it is preferred that 0 ≤ qE < 0.5, preferably 0 ≤ qE ≤ 0.2, morepreferably 0 ≤ qE ≤ 0.1, more preferably qE = 0and the process furthercomprises for said time interval Δt;(b) controlling ME so that(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(2.4) δ*E(PG) ≥ 0;wherein f= qE ^ f(min);g = qE ^ g(max);with0.80 ≤ f(min) ≤ 1, 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1;g(max) = 1;0 ≤ qE≤ 1.41. The process of embodiment 40, wherein the process carried out in the chemical productionunit UPis one or more of at least one electrochemical process, at least one a high- temperature chemical process and at least one further chemical process.42. The process of embodiment 41, wherein the at least one electrochemical processcomprises 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); isolation of nitrogen and oxygen from air via low temperature distillation (air separation); production of aluminium via electrochemical reduction ofalumina (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 carbon monoxideby reduction of carbon dioxide via electrolysis.43. The process of embodiment 41 or 42, wherein the at least one high-temperature processcomprises 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; preferably one or more of electrical heating of a cracker furnace and methane pyrolysis.44. The process of any one of embodiments 41 to 43, wherein the at least one further chemicalprocess 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 inmechanical vapour compression, application in cooling for example in compressors and / orfans.45. The process of any one of embodiments 40 to 44, being at least partially computer-implemented.46. A process, preferably according to any one of embodiments 40 to 45, comprising the stepof converting a chemical material obtainable by or obtained by the process according to any one of embodiments 40 to 45 to obtain a product product Ω.47. A process comprising the step of using the chemical production plant according to any oneof embodiments 25 to 35 to obtain a chemical material; and preferably converting thechemical material to obtain a product Ω.48. The process of embodiment 46 or 47, wherein the product Ω is selected from:- building block or monomer; or- polymer, preferably polymer A, polymer composition, preferably polymer compositionA, or polymer product, preferably polymer product A; or -cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide orcomposition or formulation thereof; or -agrochemical composition, agrochemical formulation auxiliary or agrochemicallyactive ingredient; or -active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient,animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or -aqueous polymer dispersion, preferably polyurethane or polyurethane –poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or -cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmeticingredient or composition or formulation thereof; or -polymer B, polymer composition B, coating composition, other functional composition,foil, molded body, coating or coated substrate.49. The process of any one of embodiments 46 to 48,wherein the content of the chemical material in the product Ω is 1 weight-% or more,preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the chemical material in the product Ω is 100 weight-% or less,preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservationand / 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 aproduction plant according to the present invention. Particular reference is made, among others, to embodiment 1 of the general description. Figure 1 shows an electrical storage unit US which is characterized by an amount of electricalenergy ΔE(US) which can be released within a time interval Δt. Further, Figure 1 shows a unit URfor producing electrical energy from at least one renewable source which is characterized by anamount of electrical energy ΔER(UR) which is available, i.e. which can be produced within saidtime interval Δt. Both US and UR are electrically connected (dashed lines) with a chemicalproduction unit UP which is, among others, characterized by an amount of electrical energyΔER(UP) from at least one renewable source, which energy is necessary to carry out the processin UP within Δt. Yet further, Figure 1 shows means ME which regulate the actual amount δE(US) ofelectrical energy supplied from US to UP within Δt and the actual amount δER(UR) of electricalenergy supplied from UR to UP within Δt. According to the present invention, in particular prior tothe time interval Δt, the values of ΔER(UP), ΔER(UR) and ΔE(US) are suitably determined and,according to the respective values, and in particular according to the value of ΔΔER= ΔER(UP) –ΔER(UR), the means ME regulate the actual amounts δE(US) and δER(UR).Figure 2 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particular reference is made, among others, to embodiment 2 of the general description.Compared with Figure 1, Figure 2 additionally shows that the unit USis electrically connected also to the unit UR(dotted line), and that, during the time interval Δt, a certain amount of electricalenergy δ*ER(UR) may be passed from the unit UR to the unit US, and the actual amount ofδ*ER(UR) is regulated by the means ME.Figure 3 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particularreference is made, among others, to embodiment 3 of the general description.Compared with Figure 1, Figure 3 additionally shows that the unit UP is electrically connected also to a power grid PG (dashed line), and that, during the time interval Δt, a certain amount ofelectrical energy δE(PG) may be passed from the power grid PG to the unit UP, and the actualamount of δE(PG) is regulated by the means ME. For example, during a specific time interval Δt,electrical energy may be passed both from the power grid PG and from the storage unit US to the unit UP, whereas it is also conceivable that, during another time interval Δt, electrical energy is passed to UP only from US or only from UP.Figure 4 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particular reference is made, among others, to embodiment 4 of the general description. Compared with Figure 3, Figure 4 additionally shows that the power grid PG is electrically connected also to the unit US (dotted line), and that, during the time interval Δt, a certain amountof electrical energy δ*E(PG) may be passed from the power grid PG to the unit US, and the actualamount of δ*E(PG) is regulated by the means ME.Figure 5 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particularreference is made, among others, to embodiment 5 of the general description. Compared with Figure 3, Figure 4 additionally shows that the unit URis electrically connected also to the unit US(dotted line), and that, during the time interval Δt, a certain amount of electricalenergy δ*ER(UR) may be passed from the unit UR to the unit US, and the actual amount ofδ*ER(UR) is regulated by the means ME.Figure 6 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particular reference is made, among others, to embodiment 6 of the general description. Compared with Figure 5, Figure 6 additionally shows that the power grid PGis electrically connected also to the unit US(dotted line), and that, during the time interval Δt, a certain amountof electrical energy δ*E(PG) may be passed from the power grid PG to the unit US, and the actualamount of δ*E(PG) is regulated by the means ME.Figure 7 illustrates a preferred method and a preferred process according to the presentinvention as well as a preferred production plant according to the present invention. Particular reference is made, among others, to embodiment 1 of the general description. Compared with Figure 6, Figure 7 additionally shows that the unit UR is electrically connected also to the power grid PG (dotted line), and that, during the time interval Δt, a certain amount ofelectrical energy δ**ER(UR) may be passed from the unit UR to the power grid PG, and the actualamount of δ**ER(UR) 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) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electricallyconnected with the unit USand being electrically connected with the unit UR; (4) means ME for regulating the amount of electrical energy supplied from US to UP andfrom URto UP; wherein the process comprises supplying electrical energy to UP from at least one of US and UR; 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 ΔER(UP) from at least one renewable source tobe consumed in the process in UP within Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(b) controlling ME so that the process further comprises supplying within Δt electricalenergy from UR to UP in an amount δER(UR) and from US to UP in an amount δE(US), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);wherein f ≥ 0, g ≤ 1, and f ≤ g; wherein US is characterized by the amount of electrical energy ΔE(US) releasable within Δt and UR is characterized by the amount of electrical energy ΔER(UR) available within Δt, and wherein ΔER(UR) + ΔE(US) ≥ ΔER(UP).

2. The method of claim 1, wherein the unit US is further electrically connected with the unit UR,and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from URto US; wherein the process comprises supplying electrical energy to UPfrom at least one of USand UR, and to USfrom UR;wherein according to (b), the means MEare controlled so that the process further comprises supplying within Δt electrical energy from URto USin an amount δ*ER(UR), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR).

3. The method of claim 1, wherein the unit UP is further electrically connected with a powergrid PG and the means ME according to (4) are means further for regulating the amount of electrical energy supplied from PG to UP; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG; wherein according to (b), the method of optimizing the process comprises controlling ME so that the process further comprises supplying within Δt electrical energy from UR to UP in an amount δER(UR), from US to UP in an amount δE(US), and further from PG to UP in anamount δE(PG), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);wherein PG is characterized by the amount of electrical energy ΔE(PG) releasable within Δt and wherein ΔER(UR) + ΔE(US) + ΔE(PG) ≥ ΔER(UP).

4. The method of claim 3, wherein the unit US is further electrically connected with the powergrid PG, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from PGto US; wherein the process comprises supplying electrical energy to UPfrom at least one of US, URand PG, and to USfrom PG; wherein according to (b), the means MEare controlled so that the process further comprises supplying within Δt electrical energy from PGto USin an amount δ*E(PG), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) δ*E(PG) ≥ 0;or wherein the unit USis further electrically connected with the unit UR, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from UR to US; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG, and to US from UR; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);or wherein the unit US is further electrically connected with the unit UR and the power grid PG, and the means ME according to (4) are means further for regulating the amount of electrical energy supplied from UR to US and 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, UR and PG, and to US from at least one of UR and PG;wherein according to (b), the means ME are controlled so that the process further comprisessupplying within Δt electrical energy from URto USin an amount δ*ER(UR), and further comprises supplying within Δt electrical energy from PGto USin an amount δ*E(PG), wherein(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0;or wherein the unit USis further electrically connected with the unit URand the power grid PGand the unit URis further electrically connected to the power grid PG, and the means MEaccording to (4) are means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PG to US and the amount of electrical energy supplied from UR to PG; wherein the process comprises supplying electrical energy to UP from at least one of US, UR and PG, and to US from at least one of UR and PG, and to PG from UR; wherein according to (b), the means ME are controlled so that the process further comprises supplying within Δt electrical energy from UR to US in an amount δ*ER(UR), further comprises supplying within Δt electrical energy from PG to US in an amount δ*E(PG), and further comprises supplying within Δt electrical energy from UR to PG in an amount δ**ER(UR), wherein (b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR);(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR);(2.4) δ*E(PG) ≥ 0.

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, 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1;g(max) = 1;0 ≤ qE≤ 1;wherein ΔER(UR) is further characterized by a cost factor, ΔE(US) is further characterized by a cost factor, and preferably ΔE(PG) is characterized by a cost 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 ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1), thecosts of ΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG)determined according to (4.2) the parameter qE, wherein the higher the costsof ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE; wherein, if the costs of ΔER(UR) are higher than the costs of ΔE(US) and preferablyΔE(PG), it is preferred that 0 ≤ qE < 1, preferably 0 ≤ qE ≤ 0.5, more preferably0 ≤ qE < 0.5, more preferably 0 ≤ qE ≤ 0.2, more preferably 0 ≤ qE ≤ 0.1, morepreferably qE = 0.

6. The method of any one of claims 1 to 5,wherein ΔE(US) = ΔER(US) + ΔEN(US) with 0 ≤ ΔER(US) ≤ ΔE(US), wherein ΔER(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 %; and / or wherein ΔE(PG) = ΔER(PG) + ΔEN(PG) with 0 ≤ ΔER(PG) ≤ ΔE(PG), wherein ΔER(PG) is characterized by a share SPG thereof from at least one renewable source with SPG = 100 % and ΔEN(PG) is characterized by a share NPG thereof from at least one renewable source with NPG = 0 %.

7. The method of any one of claims 1 to 6, wherein Δt is in the range of from 5 min to 24 h,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 5 min to 3 h, more preferably in the range of from 10 min to 2 h.

8. The method of any one of claims 1 to 7, wherein the electrical storage unit US according to(1) is a stationary energy 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 phosphatecathode material (LFP battery), preferably at least one NaS battery; wherein the electrical storage unit UShas a capacity preferably in the range of from 5.000 to750.000 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 preferablyfrom 50 to 100 % of the chemical production unit UPaccording to (3).

9. The method of any one of claims 1 to 8, wherein the process carried out in the chemicalproduction unit UPaccording to (3) comprises 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 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; more preferably one or more of water electrolysis; chlorine-alkali electrolysis; and production of carbon monoxide by reduction of carbondioxide via electrolysis; wherein the at least one high-temperature process preferably comprises one or more ofelectrical 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; 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 heatpump and open-loop heat pump; application in mechanical vapour compression, applicationin cooling for example in compressors and / or fans.

10. The method of any one of claims 1 to 9, wherein the at least one renewable source isselected 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.

11. The method of any one of claims 1 to 10, being at least partially computer-implemented;wherein the production plant preferably further comprises (5) a computer-supported system for controlling at least the means ME according to (4);wherein the computer-supported system is preferably further used for determining at least one of ΔER(UP) according to (a.1), ΔER(UR) according to (a.2), ΔΔER according to (a.3), andpreferably qE according to (a.4).

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) a unit UR for producing electrical energy from at least one renewable source;(3) an electrical energy consuming chemical production unit UP being electricallyconnected with the unit US and being electrically connected with the unit UR; (4) means ME for regulating the amount of electrical energy supplied from US to UP andfrom UR to UP; (5) preferably a computer-supported system for controlling at least the means MEaccording to (4); wherein the unit US is preferably further electrically connected with the unit UR and the power grid PG and the unit UR is preferably further electrically connected to the power grid PG, and wherein the means ME according to (4) are preferably means further for regulating the amount of electrical energy supplied from UR to US, the amount of electrical energy supplied from PGto USand preferably the amount of electrical energy supplied from URto PG.

13. A process, preferably as referred to in any one of claims 1 to 11, being carried out in achemical production plant according to claim 12, wherein for a time interval Δt of the process, the process comprises supplying electrical energy- from UR to UP in an amount δER(UR);- from US to UP in an amount δE(US);- preferably from UR to US in an amount δ*ER(UR);- preferably from PG to UP in an amount δE(PG);- preferably from PG to US in an amount δ*E(PG);- preferably from UR to PG in an amount δ**ER(UR);the process further comprises(a) determining for said time interval Δt(a.1) the amount of electrical energy ΔER(UP) from one or more renewable sources tobe consumed in the process in UPwithin Δt; (a.2) the amount of electrical energy ΔER(UR) being available from UR within Δt;(a.3) the value ΔΔER = ΔER(UP) – ΔER(UR);(a.4) preferably determining the parameter qE, comprising(4.1) determining the cost factors of ΔER(UR), ΔE(US) and preferably ΔE(PG);(4.2) determining, based on the cost factors determined according to (4.1),the costs of ΔER(UR), ΔE(US) and preferably ΔE(PG); (4.3) determining, based on the costs of ΔER(UR), ΔE(US) and preferablyΔE(PG) determined according to (4.2) the parameter qE, wherein the higher the costs of ΔER(UR) relative to the costs of ΔEN(PG) and preferably ΔE(PG), the smaller qE; wherein, if the costs of ΔER(UR) are higher than the costs of ΔE(US) andpreferably ΔE(PG), it is preferred that 0 ≤ qE < 0.5, preferably 0 ≤ qE ≤ 0.2, morepreferably 0 ≤ qE ≤ 0.1, more preferably qE = 0and the process furthercomprises for said time interval Δt;(b) controlling ME so that(b.1) if ΔΔER ≤ 0,(1.1) f ^ ΔER(UP) ≤ δER(UR) ≤ g ^ ΔER(UP);(1.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(1.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(1.4) δ*E(PG) ≥ 0;(b.2) if ΔΔER > 0,(2.1) f ^ ΔER(UR) ≤ δER(UR) ≤ g ^ ΔER(UR);(2.2) δE(US) + δE(PG) = ΔER(UP) – δER(UR); and preferably(2.3) 0 ≤ δ*ER(UR) + δ**ER(UR) ≤ ΔER(UR) – δER(UR); and preferably(2.4) δ*E(PG) ≥ 0;wherein f= qE ^ f(min);g = qE ^ g(max);with 0.80 ≤ f(min) ≤ 1, 0.90 ≤ f(min) ≤ 1, more preferably 0.95 ≤ f(min) ≤ 1;g(max) = 1;0 ≤ qE≤ 1.

14. A computer program comprising instructions which, when the program is executed by thecomputer-supported system as defined in claims 11 and 12, cause the system to perform the method according to any one of claims 1 to 11.

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

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