Integrated system for preparing hydrogen and a dehydrogenated product from an alcohol

Abstract

The invention provides an integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising a heat integration system for heat transfer from at least one heat source to the at least one heat sink. The at least one heat sink includes a feed stream comprising an alcohol and / or an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream and / or an infrastructure for handling and / or storing the co- product stream. The at least one heat source includes a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat, and / or the electrolyser system, wherein the electrolyser system is configured to operate the electrochemical cell so as to generate heat.

Description

FIELD OF THE INVENTION The present invention relates to an integrated system for preparing hydrogen and a dehydrogenated product from an alcohol, and to vehicles or platforms incorporating the same. BACKGROUND OF THE INVENTION Increasing awareness about the environment effects of fossil fuels and resulting societal shift away from use of fossil fuels has driven the search for alternative clean fuel sources. A valuable alternative fuel is hydrogen. Hydrogen may be utilised in a fuel cell to generate clean energy by reacting hydrogen and oxygen in which the only by-product is water. However, hydrogen has disadvantages that have limited its widespread use. Hydrogen is a highly flammable gas that, due to its small atomic size, may permeate or leak through storage containers. Consequently, storage of hydrogen can be costly and dangerous. Further, generation of hydrogen can be energy intensive and produces pollution in itself, which reduces the viability of hydrogen as a clean energy source. One solution that has been adopted is the use of liquid organic hydrogen carriers (LOHCs), such as toluene / methylcyclohexane. LOHCs may provide a stable source of hydrogen that is safe for storage and may generate hydrogen on demand by reaction with a catalyst. However, LOHCs are specialised chemicals that must be synthesised, potentially through wasteful processes. Further, when consumed in the generation of hydrogen, LOHCs create a by-product that must be regenerated or disposed of potentially leading to large volumes of by-product that must be transported and stored / disposed of. Another alternative fuel source is direct alcohol fuel cells. A direct alcohol fuel cell utilises an alcohol, e.g. methanol or ethanol, in an electrochemical cell containing an anode and cathode to generate electricity. The alcohol and water react at the anode to produce carbon dioxide and electrons and protons. The protons are transported to the cathode where the protons react with oxygen to produce water. An advantage of the direct alcohol fuel cell is that it uses alcohols that are low-cost and readily available as commodity chemicals, and the only liquid by-product is water. Direct alcohol fuel cells do, however, generate carbon dioxide. Additionally, direct alcohol fuel cells can suffer from a short life span due to the susceptibility of the cathode to e.g., catalyst poisoning by the alcohol permeating from the anode to the cathode. Any discussion of documents, acts, materials, devices, articles or the like which has been included in the present specification is solely for the purpose of providing a context for the present invention. It is not to be taken as an admission that any or all of these matters form part of the prior art base or were common general knowledge in the field relevant to the present invention as it existed before the priority date. BRIEF DESCRIPTION OF THE INVENTION The patent applicant has developed an electrochemical process for partially oxidising an alcohol to produce hydrogen and a dehydrogenated product. In some examples, the alcohol is ethanol. In some examples, the alcohol is a biofuel derived from a biological source, such as bioethanol derived from, e.g., biomass. The alcohol can function as an organic hydrogen carrier which may be oxidised to produce hydrogen at the point of use. In one example application, the hydrogen carrier is transferred to and carried by vehicles to provide a mobile source of fuel for motive power of the vehicles. At a very broad level, this is akin to petrol or diesel being carried by a passenger car as fuel for the internal combustion engine. The electrochemical process may be carried out onboard the vehicle to produce hydrogen gas for use in a hydrogen fuel cell onboard the vehicle. In some other applications, the process may not transfer the hydrogen to a hydrogen fuel cell; the hydrogen may be combusted or captured and stored or transferred for other purposes (e.g., chemical or biological). Advantageously, the dehydrogenated product may be a valuable commodity product, such as acetic acid. Acetic acid may be sold as a chemical or biological feedstock, used as an ingredient in food or feed production, or alternatively re-hydrogenated for further use in the liquid organic hydrogen carrier fuel cycle. Hence, the co-product may need to be handled and stored at the location where it is produced, such as onboard a vehicle, and this presents a unique set of circumstances and desiderata which the present invention seeks to address. The use of an alcohol as the hydrogen carrier also presents a unique set of circumstances and desiderata which the present invention seeks to address. In one aspect, the invention provides an integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising: (a) at least one heat sink including one or more of: (i) a feed stream comprising an alcohol; (ii) an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation (or partial oxidation)_process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream; (iii) an infrastructure for handling and / or storing the co-product stream; (b) at least one heat source including: (iv) a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat; (v) the electrolyser system, wherein the electrolyser system is configured to operate the electrochemical cell so as to generate heat; (c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink. In some examples, the at least one heat source includes the hydrogen fuel cell and the at least one heat sink includes (iii) the infrastructure for handling and / or storing the co-product stream, and at least one of: (i) the feed stream and (ii) the electrolyser system. In some examples, the at least one heat source further includes the electrolyser system and the at least one heat sink includes the feed stream and the infrastructure for handling and / or storing the co-product stream. In some examples, the at least one heat source includes the electrolyser system and the at least one heat sink includes the feed stream and the infrastructure for handling and / or storing the co-product stream. In some examples, the at least one heat sink further includes a battery. In other examples, the at least one heat source further includes a battery. Preferably, the battery is electrically coupled to the electrolyser unit and / or to the hydrogen fuel cell. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: at least one heat source, including an electrolyser configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser is configured to operate so as to generate heat; at least one heat sink, including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: at least one heat source, including an electrolyser configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, a controller configured to operate the electrolyser so as to generate heat; at least one heat sink, including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: at least one heat source, including an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat; at least one heat sink, including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: at least one heat source, including an electrolyser system having an electrolyser configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser system is configured to operate the electrolyser such that the electrolyser generates heat; at least one heat sink, including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol; at least one heat source including a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat; at least one heat sink including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: an electrolyser configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol; at least one heat source including a hydrogen fuel cell for generating electricity from the product stream of the electrolyser, wherein operation of the hydrogen fuel cell generates heat; at least one heat sink including an infrastructure for handling and / or storing the co-product stream; a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure. In another aspect, the invention provides an integrated system for the preparation of a dehydrogenated product from an alcohol, the integrated system comprising: (i) at least one heat source including: (a) an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat; (b) a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat; (ii) at least one heat sink including a battery; and (iii) a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink. Preferably, operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey said heated water stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated water stream provides a working fluid of the thermal network. Preferably, the electrochemical cell generates a heated co-product stream and wherein the heat integration system is configured to convey said heated co-product stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated co-product stream provides a working fluid of the thermal network. In another aspect, the invention provides a vehicle comprising the integrated system. Preferably, the integrated system comprises a hydrogen fuel cell and a battery configured for electrical connection to the hydrogen fuel cell, wherein the vehicle is configured to be motively powered by said battery. Preferably, the vehicle is configured to be motively powered by the hydrogen produced by the electrolyser system. In another aspect, the invention provides a floating or fixed platform, or a power station, comprising integrated system of any preceding statement. In another aspect, the invention provides a method for preparing a dehydrogenated product from an alcohol using the integrated system. In another aspect, the invention provides a method of producing hydrogen from an alcohol using the integrated system. In another aspect, the invention provides a method for producing a dehydrogenated product on a moving platform. In another aspect, the invention provides a method for preparing a dehydrogenated product from an alcohol, the method comprising: performing at least one heat generating process including an electrochemical process, by an electrolyser, to partially dehydrogenate an alcohol to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product, wherein the electrochemical dehydrogenation process is performed such that the electrolyser generates heat; handling and / or storing the co-product stream via an infrastructure; transferring at least a portion of the heat generated by the at least one heat generating process to at least one heat sink including to the co-product stream during handling and / or storing by the infrastructure. Preferably,   the   method   comprises   performing   the   electrochemical dehydrogenation process at a voltage above a thermoneutral voltage. Preferably,   the   method   comprises   performing   the   electrochemical dehydrogenation process above a voltage of about 0.2 volts. In another aspect, the invention provides a method for preparing a dehydrogenated product from an alcohol, the method comprising: performing an electrochemical process, by an electrolyser, to partially dehydrogenate an alcohol to produce a product stream comprising hydrogen and a coproduct stream comprising a dehydrogenated product,; handling and / or storing the co-product stream via an infrastructure; performing at least one heat generating process including operating a hydrogen fuel cell, wherein the operation of the hydrogen fuel cell generates heat; transferring at least a portion of the heat generated by the at least one heat generating process to at least one heat sink including to the co-product stream during handling and / or storing by the infrastructure. Preferably, the method comprises operating the electrochemical cell at a voltage at or below a thermoneutral voltage. Preferably, the method comprises operating the electrochemical cell at or below a voltage of about 0.2 volts. Preferably, the method comprises draining the co-product stream from a handling infrastructure of the infrastructure when the at least one heat generating process is inactive. Preferably, the method comprises transferring the at least a portion of the heat to the co-product stream during handling. Preferably, the method comprises transferring the at least a portion of the heat to the co-product stream during storing. In one aspect, the invention provides an integrated system for preparing hydrogen from an alcohol, the integrated system comprising: (a) at least one heat sink including: (i) a feed stream of a substrate liquid comprising an alcohol; and / or (ii) an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream; (b) at least one heat source including a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat; (c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink. In another aspect, the invention provides a method for preparing hydrogen from an alcohol, the method comprising: (a) providing a feed stream of a substrate liquid comprising an alcohol for use in an electrochemical dehydrogenation process; (b) performing an electrochemical dehydrogenation process, by an electrolyser, to partially dehydrogenate the feed stream to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream; (c) performing at least one heat generating process including generating electricity by a hydrogen fuel cell from the hydrogen produced by the electrochemical dehydrogenation process; (d) transferring at least a portion of the heat generated by the at least one heat generating process to feed stream and / or the electrolyser. In another aspect, the invention provides an integrated system for preparing hydrogen from an alcohol, the integrated system comprising: (a) at least one heat sink including: (i) a feed stream of a substrate liquid comprising an alcohol; and / or (ii) an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream; (b) at least one heat source including means for combusting hydrogen produced by the electrolyser system; (c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink. In another aspect, the invention provides a method for preparing hydrogen from an alcohol, the method comprising: (a) providing a feed stream of a substrate liquid comprising an alcohol for use in an electrochemical dehydrogenation process; (b) performing an electrochemical dehydrogenation process, by an electrolyser, to partially dehydrogenate the feed stream to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream; (c) performing at least one heat generating process including combusting the hydrogen produced by the electrochemical dehydrogenation process; (d) transferring at least a portion of the heat generated by the at least one heat generating process to feed stream and / or the electrolyser. In another aspect, the invention provides an integrated system for preparing hydrogen from an alcohol, the integrated system comprising: (a) at least one heat sink including a feed stream of a substrate fluid comprising an alcohol; (b) at least one heat source including an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat; (c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink. In another aspect, the invention provides a method for preparing hydrogen from an alcohol, the method comprising: (a) providing a feed stream of a substrate liquid comprising an alcohol for use in an electrochemical dehydrogenation process; (b) performing at least one heat generating process including an electrochemical dehydrogenation process, by an electrolyser, to partially dehydrogenate the feed stream to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream, wherein the electrolyser is operated so as to generate heat; (c) transferring at least a portion of the heat generated by the at least one heat generating process to feed stream. In another aspect, the invention provides a method for preparing hydrogen using the integrated system. In another aspect, the invention provides a vehicle comprising the integrated system. In some examples, the feed stream comprises a mixture of alcohol and water. In some examples, the product stream and co-product stream are produced from the mixture of alcohol and water of the feed stream. In some examples, the selective partial dehydrogenation process is referred to as a catalytic process, selective partial oxidation process, partial oxidation process or partial dehydrogenation process. In some examples, the integrated system comprises a hydrogen fuel cell and a battery configured for electrical connection to the hydrogen fuel cell, wherein the vehicle is configured to be motively powered by the battery. In some examples, the vehicle is configured to be motively powered by the hydrogen produced by the electrolyser system. In another aspect, the invention provides a floating or fixed platform, or a power station, comprising integrated system. Also herein described is: A process for preparing hydrogen from an alcohol, the process comprising: (a) providing an electrolyser comprising: i. an anode comprising a partial oxidation catalyst, ii. a cathode comprising a reduction catalyst, and iii. a separator between the anode and the cathode; (b) contacting the anode with a mixture of the alcohol and water; (c) applying a voltage to the electrolyser such that the alcohol is partially oxidized at the anode to produce a dehydrogenated product and a hydrogen precursor, and the hydrogen precursor passes through the separator and is converted to hydrogen at the cathode, wherein the voltage applied to the electrolyser is less than 1.2 V. A system for generating hydrogen from an alcohol, the system comprising: a) an electrolyser, comprising a vessel divided by a separator into a first volume and a second volume, wherein: (i) the first volume houses an anode comprising a partial oxidation catalyst capable of partially oxidizing a mixture of an alcohol and water to produce a dehydrogenated product and a hydrogen precursor, and (ii) the second volume houses a cathode comprising a reduction catalyst capable of converting the hydrogen precursor to hydrogen; b) an energy source for applying a voltage to the electrolyser, wherein the voltage to be applied to the electrolyser is less than about 1.2 V. A process for generating electricity, the process comprising: (a) providing an electrolyser comprising: i. an anode comprising a partial oxidation catalyst, ii. a cathode comprising a reduction catalyst, and iii. a separator between the anode and the cathode; (b) contacting the anode with a mixture of an alcohol and water; (c) applying a voltage to the electrolyser such that the alcohol is partially oxidized at the anode to produce a dehydrogenated product and a hydrogen precursor, and the hydrogen precursor passes through the separator and is converted to hydrogen at the cathode, wherein the voltage applied to the electrolyser is less than 1.2 V; (d) conveying the hydrogen to a fuel cell wherein the fuel cell converts the hydrogen to electricity and water. A system for generating electricity, the system comprising: a) an electrolyser, comprising a vessel divided by a separator into a first volume and a second volume, wherein: (i) the first volume houses an anode comprising a partial oxidation catalyst capable of partially oxidizing a mixture of an alcohol and water to produce a dehydrogenated product and a hydrogen precursor, and (ii) the second volume houses a cathode comprising a reduction catalyst capable of converting the hydrogen precursor to hydrogen; b) an energy source for applying a voltage to the electrolyser, wherein the voltage to be applied to the electrolyser is less than about 1.2 V; wherein in use, the hydrogen from the second volume is conveyed to the fuel cell to produce electricity. The following statements refer to any one of more of the above aspects. The integrated system may also be referred to as an integrated system for generating hydrogen from an alcohol. Where the integrated system comprises a hydrogen fuel cell, the integrated system may be referred to as an integrated system for generating electricity. The partial dehydrogenation process may be referred to as a partial oxidation process, or generally as an electrochemical process. The electrolyser may be or comprise an electrochemical cell (also referred to as an electrolytic cell), which is configured to operate as an electrochemical dehydrogenator for carrying out the partial dehydrogenation process. An electrolyser system may be provided comprising the electrolyser, wherein the electrolyser system is configured to operate the electrolyser, such as via a controller of the electrolyser system. The electrolyser system may be configured to apply and / or control a voltage applied to the electrolyser, such as via a controller of the electrolyser system. The electrolyser system may comprise, or be connectable to, an energy source, such as a battery, for applying a potential to the electrolyser. The wider integrated system may comprise the energy source, such as a battery, for applying the potential. The electrolyser system, or one or more components thereof, may be part of a unit or device. Preferably, an electrolyser unit is provided comprising the electrolyser and a controller for operating the electrolyser (e.g., for applying and / or controlling a potential to the electrolyser). The electrolyser unit is preferably connectable to an energy source, such as a battery. The electrolyser unit is preferably arranged for fluid communication with other parts of the integrated system so as to receive the feed stream and to provide the product and co-product streams. The electrolyser may comprise a vessel divided by a separator into a first volume and a second volume, wherein: (i) the first volume houses an anode comprising a partial oxidation catalyst capable of partially oxidizing a mixture of an alcohol and water to produce a dehydrogenated product and a hydrogen precursor, and (ii) the second volume houses a cathode comprising a reduction catalyst capable of converting the hydrogen precursor to hydrogen. The electrolyser may be operated by applying a potential to the electrolyser such that the alcohol is partially oxidized at the anode to produce a dehydrogenated product and a hydrogen precursor, and the hydrogen precursor passes through the separator and is converted to hydrogen at the cathode. Preferably, where the electrolyser is provided as a heat source, the electrolyser system is configured to operate the electrochemical cell at a potential above a thermoneutral voltage. Preferably, the electrolyser system is configured to operate the electrochemical cell above a voltage of about 0.2 volts (V). Preferably, the electrolyser system is configured to operate the electrochemical cell above a voltage of about 0.2 V and below a voltage of about 1.2 V. Preferably, the electrolyser system is configured to operate the electrochemical cell from above 0.2 V to about 1.2V, more preferably to about 1 V and more preferably still to about 0.5V. Preferably, where the electrolyser is not provided as a heat source, the electrolyser system is configured to operate the electrochemical cell at a voltage at or below a thermoneutral voltage. Preferably, the electrolyser system is configured to operate the electrochemical cell or electrolyser at or below a voltage of about 0.2 volts. Preferably, the infrastructure comprises a handling infrastructure for conveying the co-product stream and wherein the heat integration system is configured for heat transfer to the handling infrastructure or to the co-product stream during handling by the handling infrastructure. Preferably, the infrastructure comprises a storage infrastructure for storing the co-product stream and wherein the heat integration system is configured for heat transfer to the storage infrastructure or to the co-product stream during storing by the storage infrastructure. Thermal loops & heat exchangers Preferably, the heat integration system comprises a thermal network for conveying heat via working fluid. Preferably, the thermal network is arranged to circulate a working fluid between the at least one heat source and the at least one heat sink. Preferably, the thermal network comprises: one or more cooling loops for circulating a first working fluid for heat exchange with one or more respective heat sources of the at least one heat source; one or more heating loops for circulating a second working fluid for heat exchange with one or more respective heat sinks of the at least one heat sink; a central unit for heat exchange between the first working fluid and the second working fluid. With this arrangement, the heating loops can be controlled independently from the cooling loops. Preferably, the central unit comprises a heat exchanger for heat transfer from the first working fluid to the second working fluid. Preferably, the central unit is configured to further cool the first working fluid by removing residual heat. Preferably, the heat integration system comprises one or more heat exchangers for transferring heat between said working fluid and one or more of the at least one source and / or one or more of the at least one heat sink. Heat sources Electrolyser Preferably, the heat integration system is arranged to extract heat from the coproduct stream and / or the product stream of the electrolyser system. Hydrogen fuel cell Preferably, the at least one heat source includes a hydrogen fuel cell arranged to generate electricity from the product stream produced by the electrolyser system, wherein operation of the hydrogen fuel cell generates heat. Preferably, operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey said heated water stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated water stream provides a working fluid of the thermal network. Battery Preferably, the at least one heat source includes a battery, wherein charging and / or discharging of the battery generates heat. Preferably, the battery is electrically coupled to the electrolyser system and / or the hydrogen fuel cell. The battery may be used to apply potential to the electrochemical cell. The battery may be chargeable by the hydrogen fuel cell. Other heat sinks Preferably, the at least one heat sink includes a battery. Hydrogen combustion Preferably, the at least one heat source includes means for combusting at least a portion of the hydrogen produced by the electrolyser system. Vehicle componentry Preferably, the at least one heat source includes a braking system of a vehicle. Sensing and control Preferably, the integrated system comprises a temperature control system for controlling: (i) heat transfer, via the heat integration system, from the at least one heat source and / or to the at least one heat sink, and / or (ii) heat production, via the at least one heat source. Preferably, the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of a plurality of heat sinks. Preferably, the temperature control system is configured to control the heat integration system and / or the at least one heat source such that: (i) the co-product stream is substantially maintained above a threshold minimum temperature during handling and / or storage, and / or (ii) the battery is substantially maintained above a threshold minimum temperature of preferably 0 degrees Celsius, more preferably 20 degrees Celsius, more preferably 30 degrees Celsius, more preferably 35 degrees Celsius. Preferably, the threshold minimum temperature for the co-product stream is the freezing point of the co-product stream, optionally the freezing point of the dehydrogenated alcohol of the co-product stream. The freezing point is that under the conditions of the system. Preferably, the alcohol is ethanol, the organic acid is acetic acid and, optionally, the threshold temperature is about 17 degrees Celsius; or the alcohol is methanol, the organic acid is formic acid and, optionally, the threshold temperature is about 9 degrees Celsius; or the alcohol is propanol, the organic acid is propanoic acid and, optionally, the threshold temperature is about -20 degrees Celsius; the alcohol is butanol, the organic acid is butyric acid and, optionally, the threshold temperature is about -7 degrees Celsius; the alcohol is pentanol, the organic acid is pentanoic acid and, optionally, the threshold temperature is about -33 degrees Celsius. Preferably, the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a cooling demand and / or priority of each of the heat sources of the plurality of heat sources. Preferably, the temperature control system is configured to control the heat integration system and / or the at least one heat source such that: (i) the electrolyser system is maintained within a predetermined temperature range during operation, such as below about 150°C or preferably below, or at, about 100°C; and / or (ii) the hydrogen fuel cell is maintained within a predetermined temperature range during operation, such as from about 70°C to about 200°C, or from about 600°C to about 1000°C. Preferably, the temperature control system is configured to control a flow rate and / or distribution of working fluid for the at least one heat source and / or for the at least one heat sink. Preferably, the heat integration system comprises one or more pumps for conveying working fluid and wherein the temperature control system is communicatively coupled to the one or more pumps so as to control the flow rate of working fluid. Preferably, the integrated system comprises a plurality of heat sinks, wherein the temperature control system is configured adjust a distribution of heat to the plurality of heat sinks via the heat integration system. Preferably, the temperature control system is configured to dynamically select between, or from among, the plurality of heat sinks for heat transfer via the heat integration system. Preferably, the temperature control system is configured to adjust a distribution of heat from the plurality of heat sources to the heat integration system. Preferably, the temperature control system is configured to dynamically select between, or from among, the plurality of heat sources via the heat integration system. Preferably, the temperature control system is configured to cause the electrolyser system to adjust the operation of the electrochemical cell such that the electrochemical cell generates more or less heat. The temperature control system may be configured to cause the electrolyser system to adjust a potential applied to the electrolyser. Preferably, temperature control system is further configured to: (i) receive information pertaining to one or more of: (a) a temperature of the co-product stream during handling and / or storing by the infrastructure; (b) a temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell and / or a temperature of the battery; (c) a temperature of the ambient environment and / or a forecasted temperature of the ambient environment; (d) a composition of the co-product stream; (e) a mass flow of the co-product stream and / or a mass flow of working fluid; and (ii) control the heat transfer via the heat integration system and / or heat production via the at least one heat source based on said information. Preferably, the integrated system further comprises one or more sensors for monitoring, such as by measuring or detecting: (a) the temperature of the co-product stream during handling and / or storing by the infrastructure; (b) the temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell and / or a temperature of the battery; (c) the temperature of the ambient environment; (d) the composition of the co-product stream and / or purity of the co-product stream with respect to the dehydrogenated alcohol and / or the presence or quantity of one or more predetermined substances in the co-product stream; (e) the mass flow of the co-product stream and / or a mass flow of working fluid; wherein the one or more sensors are communicatively coupled to the temperature control system. Preferably, the threshold minimum temperature is adjusted based on the information pertaining to the composition of the co-product stream. Preferably, the alcohol is a saturated alcohol. In some examples, the alcohol is a C1-8 alcohol. In some examples, the alcohol is a C1-5 alcohol. In some examples, the alcohol is methanol, ethanol, n-propanol, isopropanol, methylene glycol, ethylene glycol, propylene glycol, glycerol or a combination of any two or more thereof. In some examples, the alcohol is ethanol. In some examples, the alcohol is bioethanol. Preferably, the alcohol is ethanol, methanol, propanol, butanol, or pentanol and wherein the dehydrogenated product is acetic acid, formic acid, propanoic acid, butyric acid, or pentanoic acid, respectively. Preferably, the alcohol is at least partially in vapour form. In some examples, the alcohol is substantially in vapour form. Preferably, the dehydrogenated product is an organic acid. Preferably, the dehydrogenated product is a carboxylic acid. In some embodiments, the dehydrogenated product is acetic acid. Thermal loops & heat exchangers Preferably, the heat integration system comprises a thermal network for conveying heat via working fluid. Preferably, operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey the heated water stream for heat transfer to one or more of the at least one heat sink, such that the heated water stream provides a working fluid of the thermal network. Preferably, the heat integration system is configured to convey the co-product stream for heat transfer to one or more of the at least one heat sink, such that the coproduct stream provides a working fluid of the thermal network. Preferably, the thermal network is arranged to circulate a working fluid between the at least one heat source and the at least one heat sink. Preferably, the thermal network comprises: one or more cooling sections for conveying a first working fluid for heat exchange with one or more respective heat sources of the at least one heat source; one or more heating sections for conveying a second working fluid for heat exchange with one or more respective heat sinks of the at least one heat sink; a central unit for heat exchange between the first working fluid and the second working fluid. Preferably, the first working fluid is a heated water stream generated by the hydrogen fuel cell during operation. Preferably, the first working fluid a the co-product stream. Preferably, the central unit comprises a heat exchanger for heat transfer from the first working fluid to the second working fluid. Preferably, the heat integration system comprises one or more heat exchangers for transferring heat between said working fluid and one or more of the at least one source and / or one or more of the at least one heat sink. Sensing and control Preferably, the integrated system further comprises a temperature control system for controlling: (i) heat transfer, via the heat integration system, from the at least one heat source and / or to the at least one heat sink, and / or (ii) heat production, via the at least one heat source. Preferably, the integrated system comprises a plurality of heat sinks including the feed stream and the electrolyser system, wherein the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of the plurality of heat sinks. Preferably, the temperature control system is configured to control the heat integration system and / or the at least one heat source such that: (i) the feed stream is substantially maintained above a threshold temperature for vapourisation, and / or (ii) the electrolyser system is substantially maintained at or above a threshold temperature, preferably at a temperature of about 100 degrees Celsius. Preferably: the alcohol is ethanol and the threshold temperature for vapourisation is about 78 degrees Celsius; or the alcohol is methanol and the threshold temperature is about 65 degrees Celsius; or the alcohol is propanol and the threshold temperature is about 97 degrees Celsius; the alcohol is butanol and the threshold temperature is about 118 degrees Celsius; the alcohol is pentanol and the threshold temperature is about 138 degrees Celsius. Preferably, the temperature control system is configured to control a flow rate and / or distribution of working fluid for the at least one heat source and / or for the at least one heat sink. Preferably, the heat integration system comprises one or more pumps for conveying working fluid and wherein the temperature control system is communicatively coupled to the one or more pumps so as to control the flow rate of working fluid. Preferably, the integrated system comprises a plurality of heat sinks, wherein the temperature control system is configured adjust a distribution of heat to the plurality of heat sinks via the heat integration system. Preferably, the integrated system comprises a plurality of heat sinks, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sinks for heat transfer via the heat integration system. Preferably, the integrated system comprises a plurality of heat sources, wherein the temperature control system is configured to adjust a distribution of heat from the plurality of heat sources to the heat integration system. Preferably, the integrated system comprises a plurality of heat sources, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sources via the heat integration system. Preferably, the temperature control system is configured to cause the electrolyser system to adjust the potential across the electrochemical cell to change a thermodynamic voltage. Preferably, the temperature control system is further configured to: (i) receive information pertaining to one or more of: (a) a temperature of the feed stream; (b) a temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell; (c) a temperature of the ambient environment and / or a forecasted temperature of the ambient environment; (d) a composition of the feed stream; (d) a mass flow of the feed stream and / or a mass flow of working fluid; and (ii) control the heat transfer via the heat integration system and / or heat production via the at least one heat source based on said information. Preferably, the integrated system further comprises one or more sensors for monitoring, such as by measuring or detecting: (a) the temperature of the feed stream during handling and / or storing by the infrastructure; (b) the temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell; (c) the temperature of the ambient environment; (d) the composition of the feed stream and / or purity of the feed stream with respect to the alcohol and / or the presence or quantity of one or more predetermined substances in the feed stream; (d) the mass flow of the feed stream and / or a mass flow of working fluid; wherein the one or more sensors are communicatively coupled to the temperature control system. Preferably, the threshold minimum temperature is adjusted based on the information pertaining to the composition of the feed stream. Preferably, the alcohol is a C1-5 alcohol. Preferably, the alcohol is ethanol, methanol, propanol, butanol, or pentanol and wherein the dehydrogenated product is acetic acid, formic acid, propanoic acid, butyric acid, or pentanoic acid, respectively. Preferably, the substrate liquid comprises a mixture of one or more alcohols and water. Preferably, the at least one heat sink further includes a battery. Preferably, the at least one heat source further includes a battery. Other aspects of the invention may become apparent from the following description which is given by way of example only and with reference to the accompanying drawings. As used herein the term "and / or" means "and" or "or", or both. As used herein "(s)" following a noun means the plural and / or singular forms of the noun. The term "comprising" as used in this specification and claims means "consisting at least in part of". When interpreting statements in this specification and claims which include that term, the features, prefaced by that term in each statement, all need to be present but other features can also be present. Related terms such as "comprise" and "comprised" are to be interpreted in the same manner. In this specification, where reference has been made to external sources of information, including patent specifications and other documents, this is generally for the purpose of providing a context for discussing the features of the present invention. Unless stated otherwise, reference to such sources of information is not to be construed, in any jurisdiction, as an admission that such sources of information are prior art or form part of the common general knowledge in the art. For the purpose of this specification, where method steps are described in sequence, the sequence does not necessarily mean that the steps are to be chronologically ordered in that sequence, unless there is no other logical manner of interpreting the sequence. BRIEF DESCRIPTION OF THE DRAWINGS The invention will now be described by way of example only and with reference to the drawings in which: Figure 1 shows a general example of an integrated system 100 according to the invention. Figure 2 shows a first example of an integrated system 100 according to the invention. Figure 3 shows a second example of an integrated system 100 according to the invention. Figure 4 shows a third example of an integrated system 100 according to the invention. Figure 5 shows a fourth example of an integrated system 100 according to the invention. Figure 6 shows an optional section 422 comprising a central heat exchanger device 424 that may be employed in heat integration systems 100 according to the invention. Figure 7 shows a fifth example of an integrated system 100 according to the invention. Figure 8 shows a sixth example of an integrated system 100 according to the invention. Figure 9 shows a seventh example of an integrated system 100 according to the invention. Figure 10 shows an eighth example of an integrated system 100 according to the invention. Figure 11 shows a ninth example of an integrated system 100 according to the invention. Figure 12 shows a second general example of an integrated system 100 according to the invention. Figure 13 shows a tenth example of an integrated system 100 according to the invention. Figure 14 shows an eleventh example of an integrated system 100 according to the invention. Figure 15 shows a twelfth example of an integrated system 100 according to the invention. Figure 16 shows a thirteenth example of an integrated system 100 according to the invention. Figure 17 shows a fourteenth example of an integrated system 100 according to the invention. Figure 18 shows a fifteenth example of an integrated system 100 according to the invention. Figure 19 shows a third general example of the integrated system according to the invention. Figure 20 shows a sixteenth example of the integrated system 100 according to the invention. Figures 21a-eshow example implementations of the integrated system 100. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS According to various aspects of the various embodiments of the present invention as illustrated in Figures 1-20, there is provided an integrated system for the preparation of a hydrogen and a dehydrogenated product, such as an organic acid, from an alcohol, which will now be described. In a broad sense, as illustrated generally in Figures 1, 12, and 19 the integrated system 100 comprises a heat sink 200, a heat source 300 / 400, and a heat integration system 400 configured to transfer heat from the heat source to the heat sink. Heat integration for co-product handling In Figures 1-12, the heat sink includes an infrastructure 200 for handling and / or storing the dehydrogenated product, such that at least a portion of the heat generated by the heat source is transferred to the dehydrogenated product during handling and / or storing, thereby helping to keep the dehydrogenated product from freezing. The integrated system 100 comprises an electrolyser 300. The electrolyser comprises an electrochemical cell operable as an electrolytic cell and more specifically as an electrochemical dehydrogenator for producing hydrogen and a dehydrogenated product from an alcohol via an electrochemical dehydrogenation process. The electrochemical process and the electrolyser are described in greater detail elsewhere in this specification. In general, the electrolyser comprises an electrochemical cell having an anode and a cathode (i.e., the electrodes), and a separator, such as a membrane, between the anode and the cathode. The electrolyser may be part of an electrolyser system, which is configured to control the operation of the electrolyser, such as by applying and / or controlling a potential applied to the electrolyser. Preferably, the electrolyser system comprises a controller for such purposes. The electrolyser system may provide for various connections or couplings for integration with the other parts of the integrated system. For example, the electrolyser system may be arranged to couple the electrolyser to an energy source, such as a battery, for applying a potential to the electrolyser (i.e., a cell voltage across the electrodes). The electrolyser system may also provide for fluid connections with other parts of the integrated system. In particular, the electrolyser 300 is arranged to receive a feed stream 102 comprising an alcohol and to produce a product stream 104 comprising hydrogen and co-product stream 106 comprising a dehydrogenated alcohol (i.e., the dehydrogenated product). The electrolyser and one or more other components of the electrolyser system may be part of a unit or device. Preferably, an electrolyser unit is provided comprising the electrolyser 300 and a controller for operating the electrolyser (e.g., for applying and / or controlling a potential to the electrolyser). The electrolyser unit is preferably connectable to an energy source, such as a battery. The electrolyser unit is preferably arranged for fluid communication with other parts of the integrated system so as to receive the feed stream and to provide the product and co-product streams. The hydrogen may be provided to a hydrogen fuel cell 500 for the generation of electricity, as discussed elsewhere in this specification, or provided for other purposes (e.g., combusted, or otherwise used or sold as feedstock chemical for chemical or biological purposes). It may also be desirable, or indeed necessary, for the dehydrogenated product to be handled and stored for a time at the location where the reaction process takes place before subsequent use or distribution. For example, the dehydrogenated product may be recycled within an LOHC cycle (i.e., re-hydrogenated) or, as is preferred, at least some of the dehydrogenated product may be provided as a saleable chemical for other purposes (e.g., chemical or biological). Hence, the integrated system 100 comprises infrastructure 200 for handling and / or storing the co-product stream 106. The co-product stream 106 is conveyed by a handling infrastructure 202, which may include for example one or more pumps, fluid lines (e.g., tubes, pipes and the like), metering devices, flow measurement and control devices, and other such equipment as will be appreciated, from the electrolyser system to a storage infrastructure 204 (e.g., one or more storage units, vessels, containers, tanks or the like) where the dehydrogenated product may be stored as desired for later use or distribution. The storage infrastructure may be for example an adaptable storage device. The handling and storage infrastructure 202, 204 may be together referred to simply as the infrastructure 200. Preferably, the dehydrogenated product is an organic acid, such as formic acid, acetic acid, propionic acid, or butyric acid, produced by selective partial dehydrogenation (oxidation) of methanol, ethanol, propanol, or butanol, respectively. The freezing point of substances such as these may be sufficiently high as to potentially present a handling and / or storage challenge in the conditions where they are produced, particularly when produced as a pure stream or handled as such (e.g., after purification). Indeed, in some environments the ambient temperature may be, or drop to (at least temporarily or intermittently), below the freezing point of the dehydrogenated product, causing the formation of crystals in the co-product stream during handling and / or storage, and ultimately leading to a phase transition of the dehydrogenated product from liquid to solid, i.e., freezing. This can be problematic during handling as the infrastructure may be designed to manage fluid flow (e.g., liquid, vapour, or a mixture thereof) by means of pumps, fluid lines and the like, which may be unable to operate if the dehydrogenated product freezes or begins to do so. Even the formation of crystals among a largely liquid body of co-product can be problematic as this may still cause blockages or otherwise interfere with the operation of system componentry, such as pumps. Equally, it may be desirable to maintain the dehydrogenated 5 product in a liquid state during storage so that the product may be emptied, such as by draining or pumping, for subsequent use or distribution (as described elsewhere). If the stored product were to freeze, then significant energy and time may be consumed thawing the contents to bring it into a desired state for further handling (e.g., emptying), such as by using an external heat source. Due to enthalpy of fusion, more energy may be required to 10 melt a frozen quantity of dehydrogenated product than would be required to simply maintain that quantity above freezing. The integrated system advantageously comprises a heat integration system 400 arranged to transfer heat from one or more heat sources 300, 500 in the system to the product stream 106 during handling and / or storage to at least assist in maintaining the co-15 product stream 106 in a fluid state (e.g., as a liquid) or at least in a flowable condition (e.g., as a slurry). In some examples, heat may be transferred to the co-product stream 106 indirectly by heating the infrastructure 200 (e.g., parts of the handling infrastructure 202, or the storage infrastructure 204). In some examples, heat may be transferred to the coproduct stream 106 during handling and / or storage more directly, such as by heat exchange 20 between a working fluid and the co-product via a heat exchanger device. In some examples, the heat integration system 400 may be able to provide sufficient heat to maintain the coproduct stream 106 above freezing during handling and / or storage, though in some cases additional (e.g., external) sources of heat may be provided in combination. Either way, the arrangement can at least aid in the prevention of freezing, or the formation of crystals, in 25 the co-product stream 106 during handling and / or storage. Suitable means for transferring heat in this way will be apparent to the skilled person. In the specific examples that follow, the heat integration systems 400 comprise of a thermal network for circulating working fluid, wherein the thermal network is arranged for thermal communication between the heat source(s) and heat sink(s) via one or more heat 30 exchangers and comprises of one or more cooling sections (loops, in some examples) for cooling at the heat source and one or more heating sections (loops, in some examples) for heating at the heat sinks, but this should not be understood as representing the extent of suitable arrangements. In some examples, the one or more heat exchangers may be replaced with one or more heat pumps. This may advantageously raise the quality of the heat from the heat source (for example, where the heat source produces less heat than desired). Electrolyser as heat source In some examples, the heat source is provided by the electrolyser 300. Depending upon the conditions of operation (discussed in more detail below) the electrolyser system -and in particular the electrolyser 300 thereof - produces heat and hence is considered a heat source in the context of the present invention. As mentioned, the electrolyser 300 comprises an electrochemical cell configured as an electrochemical dehydrogenator. The electrolyser system may be arranged to control the operation of the electrochemical cell and in particular the potential or cell voltage applied across the electrodes, which may control the thermodynamic state. As one skilled in the art will appreciate, the thermodynamic state may be characterised broadly by reference to a 'minimum voltage', which is related to the Gibbs free energy change of the reaction and which sets the threshold potential for the reaction to take place, and a 'thermoneutral voltage', which is related to the enthalpy difference of the reaction and which determines whether the reaction requires heat to overcome the reaction barriers (i.e., what may be considered an endothermic state) or whether the system overall generates heat (i.e., what may be considered an exothermic state). In short, if the electrolyser is operating the reaction below the minimum voltage, then the reaction does not take place; if operating at or above the minimum voltage but below the thermoneutral voltage, then the reaction takes place if adequate heat is provided to meet the entropic term; if operating at the thermoneutral voltage, then the reaction takes place isothermally and without requiring (or generating) heat; and finally, if operating above the thermoneutral voltage, then the reaction takes place and any 'extra' energy provided as an overpotential, above the thermoneutral voltage, is converted to heat in direct proportion to the potential above the thermoneutral voltage. This heat may be produced through losses in the electrodes (i.e., the anode and the cathode) and / or through Ohmic resistance of the separator. In some examples, the minimum voltage is about 60 millivolts. In some examples, the thermoneutral voltage is about 0.2 volts. The applicant recognises that there can be advantages in operating above the thermoneutral voltage to drive the reaction at a reasonable rate to generate sufficient hydrogen for the desired purpose (e.g., for use by a fuel cell) and without requiring an excessively large reactor. However, the resulting exotherm is generally considered waste heat and it is desirable for the heat to be removed so that the electrolyser operates within a preferred temperature range (discussed elsewhere). Otherwise, operation of the electrolyser above the thermoneutral voltage may not be sustainable. Additionally, the dehydrogenated product may be produced at a temperature above boiling and in some circumstances it may be desirable to cool the product stream such that the stream can be handled in a predominantly liquid state. With the integrated system of the present invention, the heat integration system can advantageously cool the electrolyser, thereby allowing the electrolyser to operate above thermoneutral voltage and within a preferred temperature range (preferably isothermally), while also providing a source of heat for use in preventing freezing of the co-product during handling and / or storage. This can result in a higher rate of reaction and hence a higher rate of hydrogen (and co-product) production, whilst also addressing the aforementioned issues with handling and storage of the co-product. Thus, in the context of the present invention, the electrolyser system 300 is configured to operate the electrolyser (i.e., by controlling a potential applied across the electrodes) above the thermoneutral volage of the system when it is desirable or acceptable for the electrochemical cell to generate heat. It is noted that the electrolyser may still be operated at a relatively low potential to favour partial oxidation of the alcohol, as discussed in more detail below. This may also improve integration with a hydrogen fuel cell, where present. Preferred ranges for the potential applied to the electrolyser are described elsewhere in this specification. Examples Figure 2 shows a first example of an integrated system 100 in which a heat integration system 400 is provided for conveying heat from the electrolyser 300 to the handling and / or storage infrastructure 202, 204. In Figure 2, the heat integration system 400 comprises a thermal network in the form of a thermal loop 402 for circulating a working fluid. The thermal loop 402 may comprise pumps, such as pumps 404, for affecting movement of the working fluid therewithin (the number of pumps and location within the thermal network may differ from that shown in the figures). The thermal loop 402 is arranged for thermal communication between the heat source (in this case, the electrolyser system 300) and heat sink(s) 202, 204 and comprises of one or more cooling sections 406 and one or more heating sections 408. The cooling section 406 is arranged for heat transfer between the electrolyser system 300 (e.g., a part of the electrolyser system, and / or its contents) and the working fluid and in particular to provide cooled working fluid 406a to be heated by heat exchange with the electrolyser system 300, thereby cooling the electrolyser 300. Hence, the cooling section 406 may comprise a heat exchanger device 410 associated with (i.e., integrated with, disposed within, or otherwise thermally coupled for suitable heat exchange) the electrolyser 300. The heat exchanger device 410 may be arranged for heat exchange between a working fluid and the heated co-product. The heat integration system 400 may also be arranged to extract heat from the heated product (i.e., hydrogen) stream 104. The one or more heating sections 408 are arranged for heat transfer between the working fluid and the co-product stream 106 (i.e., the dehydrogenated product during handling and / or storage) and in particular to provide heated working fluid 406b to be cooled by heat exchange with the infrastructure 200, or with the dehydrogenated product within the infrastructure, thereby heating the dehydrogenated product during handling and / or storage. Where there is a plurality of heat sinks, these are preferably serviced by a corresponding plurality of parallel heating loops as shown in Figure 2, each loop siphoning off a portion of the working fluid for delivery to a respective heat sink, as shown. A serial arrangement is also possible, but the parallel arrangement may advantageously provide greater control over the heat distribution between heat sinks and may help to ensure that each of the heat sinks is provided with working fluid at sufficient temperature for desired heat exchange. A first heating loop 408a may be arranged for heat transfer to one or more parts of the handling infrastructure, or portions thereof, as shown in Figure 2. The first heating loop 408a may comprise a heat exchanger device 412 associated with the handling infrastructure 202. A second heating loop 408b may be arranged for heat transfer to the storage infrastructure 204, or a part thereof (e.g., a container), such as via a heat exchanger device 414 associated with the storage infrastructure 204, as also shown. Third and subsequent heating loops may be provided as desired to other heat sinks (not shown), such as to other parts of the handling infrastructure or storage infrastructure, or for use outside of the system. Figure 3 for instance shows a second example of an integrated system in which a heating loop (being a third loop in the illustrated example) is provided for heat transfer to a battery, as described in more detail below. One or more of these heating loops, and any combination thereof, may be provided as desired. Figure 3 shows a second example of the integrated system 100. The second example is substantially the same as the first example except that the system further comprises a battery 206 associated with a respective heating loop 408c of the heat integration system 400. The battery 206 may be arranged to provide electrical power for the electrolyser system, for example, as shown by the dashed line 206a. In other words, the battery 206 may be electrically coupled to the electrolyser system. It may be desirable for the temperature of the battery 206 to be maintained at or above a threshold, particularly during periods of charging and discharging, for desired operation and performance. The threshold temperature may be 0°C, preferably 10°C, more preferably 20°C, preferably still 30°C, or more preferably still 35°C. As described above in the context of the co-product stream, in some environments the ambient temperature may be, or drop to (at least temporarily or intermittently), this threshold temperature and hence the heat integration system may be employed to the benefit of the battery, too. Hence, in Figure 3 a further (third) heating loop 408c is arranged for heat transfer to the battery 206. This heating loop 408c may comprise a heat exchanger device 416 associated with the battery 206. Any number of the heating loops shown in Figure 3 may be provided in addition to that for the battery. While not shown, an integrated system comprising a single heating loop for heating the battery, without the addition of heating loops for the infrastructure, is nonetheless envisaged. In some circumstances, the battery 206 may also be a heat source, for example during periods of heavy charging or discharging, and / or depending on the ambient conditions, and it may in such circumstances be desirable to cool the battery rather than to heat the battery. In one example (not shown), the heat integration system 400 may be arranged to transfer heat from the battery 206, as a heat source among the other heat source(s) of the system, to one or more of the heat sinks. Hence, the heat integration system 400 may comprise a thermal loop with a cooling section for heat exchange with the battery. In some examples, such as that illustrated in Figure 4, the heat source is provided by a hydrogen fuel cell 500. As one skilled in the art will appreciate, the operation of the hydrogen fuel cell 500 produces heat and hence the fuel cell is considered a heat source in the context of the present invention. The hydrogen fuel cell 500 may be a significant source of heat during operation given typical efficiencies (e.g., 50-65%), particularly for a high-energy or high-temperature hydrogen fuel cell, or for a fuel cell operated near its maximum rated capacity. When present and operational, the hydrogen fuel cell may be responsible for producing most of the excess heat in the system. This heat is generally considered waste heat and so its removal may be desirable to maintain the temperature of the fuel cell within preferred operational conditions (preferable isothermal). With the heat integration system 400 of the present example, the integrated system can advantageously cool the hydrogen fuel cell 500 thereby allowing the fuel cell to operate within a desired temperature range, while also providing a source of heat for use in preventing freezing of the co-product during handling and / or storage. Figure 4 shows a third example of the integrated system 100. The cooling section 406 of the thermal loop 402 in this example operates in substantially the same way as that already described for Figure 2, except that in this case the cooling section 406 is arranged for heat transfer between the hydrogen fuel cell 500 (e.g., a part of the fuel cell, and / or its contents) and the working fluid and in particular to provide cooled working fluid 406a to be heated by heat exchange with the fuel cell 500, thereby cooling the fuel cell. Hence, the cooling section 406 may comprise a heat exchanger device 418 associated with (i.e., integrated with, disposed within, or otherwise thermally coupled for suitable heat exchange) the fuel cell. The heat exchanger device 418 may be configured for heat exchange between the working fluid and a heated water stream produced by the fuel cell 500, for example. The heating section 408 may be substantially as described above for Figure 2. Figure 5 shows a fourth example of the integrated system 100. The fourth example is substantially the same as the third example except that the system further comprises a battery 206 associated with a respective heating loop 408c of the heat integration system 400, in a manner analogous to Figures 2 and 3. As already discussed with respect of Figure 3, the battery 206 may be arranged to provide electrical power for the electrolyser system 300, for example, as shown by the dashed line. In this example, the battery 206 may also, or alternatively, be arranged to store electrical charge from the hydrogen fuel cell 500. In other words, the battery 206 may be electrically coupled to the hydrogen fuel cell 500 and / or to the electrolyser system 300. The heat integration system 400 in Figure 5 is configured to provide heat to the battery 206 in much the same way as already described for Figure 3. In other examples, the hydrogen produced by the electrolyser is combusted rather than being conveyed to a fuel cell (e.g., in an internal combustion engine of a vehicle). Hence, the at least one heat source may include combustion means for combusting the hydrogen. A portion of the hydrogen generated by the electrolyser may be combusted, which may be solely for the purposed of generating heat. Combusting hydrogen can generate more heat than other processes. In one example, the heat source includes a battery. In another example, the heat source includes a braking system of a vehicle. Central heat exchanger unit One might expect the cooling load and the heating load of the integrated system to differ, such that the demand on the heat integration system is different for the heat source(s) compared to the heat sink(s). For example, the preferred temperature for the operation of the heat sources, and the amount of heat generated, may be significantly higher than the desired, or necessary, temperature for the heat sinks. As discussed below, the electrolyser 300 may operate at, or in excess of, about 100 degrees Celsius, whereas the dehydrogenated product, or any battery 206, may only need to be maintained at around room temperature, or lower. Hence, there may be advantages in separating the cooling and heating loops of the heat integration system so that each can be controlled or operated independently. Figure 6 shows an optional section 422 of a heat integration system 400, which may be employed in any of the heat integration systems 400 described above or below to provide greater control over the heat integration system 400 for meeting the heating and cooling demands of the heat exchange at the either side of the system. The illustrated example reflects the thermal loops of Figure 1, but appropriate arrangements for other examples will be clear from the presence of the optional section 422 in those figures. The optional section 422 comprises a central unit 424 having a heat exchanger device 426 that separates the cooling and heating sections 406,408 of the thermal loop 402 into one or more cooling loops for circulating a first working fluid (i.e., delivering cooled working fluid 406a to the one or more heat sources) and one or more heating loops for circulating a second working fluid (i.e., delivering heated working fluid 408 to the one or more heat sinks), such that the heating loop(s) and cooling loop(s) are physically isolated (i.e., there is no transfer of working fluid from one to the other) while the heat exchanger device maintains thermal communication therebetween for transferring heat from the heated first working fluid to the second working fluid. With this arrangement, the cooling loop(s) and the heating loop(s), and in particular the circulation of working fluid therewithin, can be controlled independently. The cooling loop 406 and the one or more heating loops 408 may comprise pumps 404 respectively, to affect movement of the working fluids, and that movement may be different. For example, the rate of flow of working fluid in the cooling loop 406 may be greater than the rate of flow of working fluid in the heating loop 408. The central unit 424 may be arranged to provide further conditioning of the first working fluid to further remove heat (i.e., remove residual heat) before being circulated again at the desired temperature in the cooling loop. Additionally, the present example can enable the use of different (e.g., specialised) working fluids suitable for the cooling section 406 and the heating section 408, though in some instances the first working fluid and the second working fluid may be the same substance (e.g., water). As in the preceding examples, the one or more cooling loop 406 are arranged for heat transfer between the heat source(s) and the first working fluid and in particular to provide cooled working fluid 406a to be heated by heat exchange with the heat source(s), thereby cooling the heat source(s). In this case, the heated first working fluid is then recirculated back to the central unit 424. Likewise, the one or more heating loops 408 are arranged for heat transfer between the second working fluid and the heat sink(s) and in particular to provide heated working fluid 406b to be cooled by heat exchange with heat sink(s). The one or more heating loops 408a-c are further arranged to recirculate the cooled working fluid back to the central unit, where it is brought into thermal communication with the cooling loop to affect heat transfer therebetween. In particular, the central heat exchanger is arranged to provide for heat transfer from the heated first working fluid to the cooled second working fluid, so as to provide cooled first working fluid and heated second working fluid for the functions already described. The central unit 424 may be arranged to provide further conditioning of the first working fluid to further remove residual heat before being circulated again in the cooling loop. Plurality of heat sources The central unit 424 may be particularly advantageous in cases where the integrated system comprises a plurality of heat sources. Figure 7 shows a fifth example of an integrated system 100, in which both the electrolyser 300 and the hydrogen fuel cell 500 are employed as heat sources within the context of the present invention. Here, the cooling section 406 of the thermal loop comprises of a pair of cooling loops, each serving a respective heat source. Namely, a first cooling loop is arranged to provide cooled working fluid to the electrolyser 300 for heat transfer from the electrolyser to the working fluid (e.g., via a heat exchanger device associated with the electrolyser system), and a second cooling loop is arranged to provide cooled working fluid to the hydrogen fuel cell for heat transfer from the fuel cell to the working fluid (e.g., via a heat exchanger device associated with the fuel cell). The heated working fluid from the cooling loops is then provided to the heat sink(s) for heat transfer heat to the heat sink(s). As above, one or more of the heating loops 408a-b shown, and any combination thereof, may be provided as desired. Additionally, while this example is shown comprising the central heat exchanger unit, this should be understood as a preferable option and one skilled in the art will recognise the appropriate configuration for circulating a working fluid directing between heat sources and heat sinks. Figure 8 shows a sixth example of an integrated system 100, substantially the same as the fifth example but further comprising a battery 206 associated with a respective heating loop 408c of the heat integration system 100. One or more of the heating loops shown, and any combination thereof, may be provided as desired. Additionally, the battery 206 may in some examples be employed as a heat source, as already described. It will be appreciated that the ultimate purpose of the heat integration systems 400 described is to transfer heat to the dehydrogenated product during handling and / or storage and that this can be carried out 'directly', such as via substantially direct heat exchange with the working fluid, or indirectly, such as by heat exchange between the working fluid and the physical infrastructure surrounding the co-product stream, i.e., parts of the handling infrastructure 202 or storage infrastructure 204, which in turn transfer heat to the co-product contents. Additionally, one skilled in the art will appreciate that heat exchangers may take many forms and configurations, and what is shown schematically in the figures is merely for the purposes of explanation. Working fluid In the examples discussed so far, the working fluid has been dedicated working fluid isolated within the thermal loop 402 of the heat integration system 400. The working fluid may be any working fluid suitable for the demands of the system. In some examples, the working fluid is water. As mentioned, the hydrogen fuel cell 500 may produce water as a byproduct and this water may be heated by waste heat generated by the operation of the fuel cell 500. Figure 9 shows a seventh example of the integrated system 100 in which this heated water stream 108 produced by the hydrogen fuel cell 500 is employed as the working fluid in the heat integration system 400 and conveyed, such as via one or more pumps 404, from the fuel cell 500 to one or more heat sinks of the system for heat exchange. Unlike previous embodiments, since the heated water stream 108 may be produced substantially continuously during the operation of the hydrogen fuel cell 500, the want for recirculating the working fluid in a closed loop may be obviated and hence the water may be subsequently conveyed to a water storage infrastructure 204 (e.g., one or more containers), or discharged (e.g., drained or otherwise disposed of). In other examples, the water may be put to further use within the system. As will be appreciated, the example shown in Figure 9 may otherwise have any of the features already described for other examples. For instance, the cooling section 406 of the present example may be combined with other cooling loops. Such examples may involve the optional section 422 shown in Figure 6 (which may be present in any event such that the water-based cooling section of Figure 9 is separated from the heating loops, which may then employ different working fluids). Similarly, the products of the electrolyser 300, such as the hydrogen 104 and the co-product stream 106, may be heated by the operation of the electrolyser 300. Figure 10 shows an eighth example of the integrated system 100 in which the heated co-product stream 106 produced by the electrolyser 300 is employed as the working fluid in the heat integration system and conveyed, by the handling infrastructure 202, from the electrolyser 300 to the storage infrastructure 204 via one or more heat sinks (e.g., a battery 204 of the system, and / or any other heat sinks) of the system for heat exchange. In this case the handling infrastructure serves the function of the heat integration system 400 and comprises the heating and / or cooling sections of the thermal network. Since the heated co-product stream 106 may be produced substantially continuously during the operation of the electrolyser 300, and in general the intention is to convey the co-product for storage, the want for recirculating the working fluid in a closed loop may be obviated and hence the coproduct stream 106 is simply conveyed to the storage infrastructure 204. In some examples, the handling infrastructure 202 is arranged to provide a parallel heating loop, in which heat from the heated co-product stream is siphoned to a heat sink for heat exchange via, for example, a heat exchanger 416 associated with the heat sink (this option being illustrated by the dashed co-product line). In other examples, the heated co-product stream is run serially through one or more heat sinks. In some examples, the handling infrastructure 202 is arranged to provide a plurality of parallel heating loops for a plurality of heat sinks (with heat exchange via, for example, respective heat exchanger devices). In other examples, the stream employed for heat integration may be a mixture of feed and co-product substances that is recycled back as feed for further dehydrogenation by the electrolyser system (for example, where not all of the alcohol in the feed is consumed during the dehydrogenated process, such that the result is a co-product mixture comprising dehydrogenated alcohol and un-dehydrogenated alcohol), while the infrastructure 202 is arranged to convey the purified co-product stream 106 to the storage infrastructure 204. In yet other examples, heat from the hydrogen product is extracted, additionally or alternatively, and conveyed to the heat sinks. In general, Figures 9 and 10 show examples where one or more heated products of the system are used as the working fluid. In other words, the heat integration system is configured to convey one or more products of a heat source of the system, heated by waste heat from the operation of that heat source, from the heat source to one or more heat sinks. The heat integration system is further arranged for heat exchange between the heated working fluid and the desired heat sink, such as via one or more heat exchanger devices as already described. However, since the working fluid in this case is prepared in a heated state, the system may avoid the need for a heat exchanger associated with the heat source. This can reduce the complexity of the system and may increase efficiency of heat transfer from source to sink. In the illustrated examples of Figures 9 and 10, the heat integration system 400 is shown to convey the working fluid from the source to the heat sink(s). However, in other examples, the heat integration system 400 may comprise the optional section 422 described above, such that the heated product from the heat source(s) is arranged as a cooling section for heat exchange (e.g., via a heat exchanger device such as in the central unit) with a second working fluid within one or more separate heating loops. This may provide some or all of the advantages associated with such an arrangement already discussed. Additionally, the heat integration system may comprise one or more such cooling loops, or sections, arranged in parallel. For example, the heat integration system may comprise a first cooling section arranged to use the heated water stream from the hydrogen fuel cell as the working fluid, and a second cooling section (e.g., a cooling loop) arranged to use the heated co-product mixture from the electrolyser as the working fluid. Each cooling section may be arranged for heat exchange with one or more heating loops via a central unit, as described above. Alternatively, or additionally, the cooling sections as presently described may be used in combination with any of the cooling sections previously described. Draining of handling infrastructure As will be appreciated from the foregoing discussion with respect to the heat sources, the generation of sufficient heat for the intended purpose(s) (notably that of antifreezing for the co-product) is generally dependent upon the operation of the heat sources within the system and there may be circumstances in which there is no active heat generating process to be used by the heat integration system, or insufficient heat (e.g., when the electrolyser and / or hydrogen fuel cell are inactive, or operated in such a way that no, or insufficient, heat is generated). Preferably, the integrated system 100 is configured to drain the handling infrastructure 202 of co-product during (in response to, simultaneously with, or in anticipation of) one or more of the heat sources being inactive, or in state of generating no or insufficient heat, to avoid freezing or the formation of crystals in the handling infrastructure during this time (which may only be temporary). Co-product remaining in the handling infrastructure 202 may be conveyed (e.g., pumped or allowed to drain under gravity) to the storage infrastructure 204, where a greater volume of co-product may cool more slowly and thus remain above freezing for a greater amount of time. Additionally, it may be easier to address any freezing of co-product in a centralised space, like a container of the storage infrastructure, than in the handling infrastructure, which may be a network of fluid lines and componentry. The formation of crystals in the storage infrastructure is potentially also less operationally problematic than in the handling infrastructure. Additionally, or alternatively, the integrated system 100 may be configured to generate or transfer excessive (or increased) heat prior to such a period of heat source inactivity, preferably to elevate the temperature of the co-product to a higher temperature above the freezing point, thereby providing more time before the co-product stream in the handling and / or storage infrastructure cools to a point of freezing. Temperature sensing and control Preferably, the heat integration system 400 is configured to control the distribution of heat from one or more heat sources to one or more of the heat sinks, such as via a temperature control system 600 comprising one or more controller devices (in this example, a central controller 602). For example, the heat integration system 400 may be configured to control an amount, or rate, of heat transferred, or to select among or switch between heat sources and / or heat sinks, to meet the demands or priorities of the system. In the illustrated examples, where the heat integration system 400 comprises of heat exchanger devices and circulating working fluid, the temperature control system 600 may be configured to control the flow of working fluid around heating and / or cooling loops, by communicating with (e.g., transmitting control signals to) flow control devices of the heat integration system, such as pumps 404. The temperature control system 600 may also be configured to control the operation of the electrolyser system 300 and / or hydrogen fuel cell 400, such as via communicative coupling between the controller 602 and the electrolyser system 300 and / or hydrogen fuel cell 500 or an associated controller. For example, the temperature control system 600 may be configured adjust the potential applied to the electrolyser by the electrolyser system 300 to switch between or select among particular operational states, such as above the thermoneutral voltage, at the thermoneutral voltage, between the thermoneutral voltage and the minimum voltage, at the minimum voltage, or even below the minimum voltage to cease the reaction. The temperature control system 600 may be configured to adjust the operation of the electrolyser system 300 between such states to control the rate of the reaction. As will be appreciated from the foregoing discussion, this may also control the amount of heat generated by the electrolyser system 300. The same may be true of the hydrogen fuel cell 500. Preferably, such control is based on information about environmental conditions (e.g., ambient temperature) and / or internal conditions (e.g., temperatures of infrastructure 200, or the co-product stream 102, or rate of flow or composition of the co-product stream). The integrated system 100 may comprise one or more sensors for monitoring (e.g., measuring) the temperature of the co-product stream (either directly or via the infrastructure) and / or one or more sensors for monitoring the composition of the coproduct stream (or at least the presence, or prevalence, of one or more predetermined substances). The integrated system may comprise a device for monitoring the mass flow of the product stream. The integrated system may comprise a sensor for monitoring the ambient temperature. The temperature control system 600 may be communicatively coupled to the one or more sensors (e.g., by wired or wireless communication technology) and configured to receive information (e.g., measurement data) from the sensors and to control the distribution of heat accordingly. The temperature control system 600 may be configured to process the received information, such as by comparing received values to one or more thresholds, or ranges, and to transmit control signals based on said processing. Hence, with this arrangement, the thermal network 400 of the heat integration system may be considered a temperature control loop. Figure 11 shows a ninth example of an integrated system 100 comprising a sensing and temperature control system 600. The arrangement of the sixth example is used merely to illustrate the concept, but it will be understood that the features described can be implemented in any of the integrated system examples. Various sensing and control is shown in Figure 11 and any combination or selection therefrom is within the scope of the disclosure. For example, the integrated system 100 may comprise a temperature sensor 604 arranged to monitor the temperature of the electrolyser 300 and to transmit data, such as temperature readings, to a central controller 602 of the temperature control system 600, such as via communication link 604a. The controller 602 may be configured to receive and process the data, and to transmit control signals (not shown) to a flow control device of the cooling loop (e.g., the pump 404) to adjust the rate of flow of the cooled first working fluid to the electrolyser system based on said processing. For example, if the controller 602 determines that the temperature of the electrolyser 300 is above a threshold maximum value, or is rising faster than a threshold rate, then a control signal may be sent to a flow control device associated with the cooling loop (such as the pump 404) to increase the rate of flow of the working fluid thereby increasing the rate of heat exchange and thus the cooling of the electrolyser system 300. Equally, if the controller 602 determines that the temperature of the electrolyser 300 has fallen to below a threshold minimum value, or is falling faster than a threshold rate, then a control signal may be sent to the flow control device (e.g., pump 404) to reduce, or even stop, the flow of the first working fluid until the temperature of the electrolyser 300 has returned to within a desired range. Additionally, or alternatively, in such circumstances the controller 602 may signal to the electrolyser system to increase the rate of the reaction (e.g., by operating further in excess of the thermoneutral voltage) so as to generate more heat. Preferably, the temperature control system 600 is configured to maintain the temperature of the electrolyser 300 at or below about 200 degrees Celsius, at or below about 150 degrees Celsius, and preferably at or below about 100 degrees Celsius. In some circumstances it may be desirable to operate the electrolyser 300 at a temperature as low as about 80°C, or as high as about 190°C or even 200°C. Preferably the temperature control system is configured to operate the electrolyser 300 isothermally. Similarly, where the integrated system 100 comprises other, or alternative, heat sources, such as the hydrogen fuel cell 500 (e.g., as shown in Figures 3-6) and / or the battery 206 (e.g., as shown in Figures 5-6), the integrated system 100 may comprise one or more temperature sensors 606, 608 for monitoring the temperature of those heat sources, and may be configured to control the associated thermal loop(s) in a manner analogous to that discussed above, mutatis mutandis. Preferably, the temperature control system 600 is configured to control the heat integration system 400 such that the temperature of the battery 206 does not fall to below the preferred threshold temperature(s) mentioned above. Preferably, the controller is configured to control the heat integration system such that the temperature of the fuel cell is maintained within the preferred operational temperatures discussed elsewhere in this specification. In cases where the integrated system 100 comprises multiple heat sources, the controller advantageously selects among or between the heat sources depending on which of the heat sources is generating heat at a particular time, or how much heat is being generated by each of the heat sources (as determined by the sensors, for example). For example, referring to Figure 5, the temperature control system 600 may be configured to control cooling loops such that the cooling demands of the heat sources, or heat extraction demands, are met. Such decisions may also, or alternatively, be based on cooling priorities (e.g., a hierarchy of heat sources). The integrated system 100 may comprise one or more temperature sensors 610 for monitoring the temperature of the co-product stream 102 during handling by the handling infrastructure 202 (or parts thereof), or the temperature of the infrastructure itself (or parts thereof), and to transmit data, such as temperature readings, to the controller 602. 5 The controller 602 may be configured to receive and process the data, and to transmit control signals to a flow control device of the associated heating loop to adjust the rate of flow of the heated working fluid to the handling infrastructure 202. For example, if the controller 602 determines that the temperature of the product stream 106 is nearing, at or below a threshold minimum value, or falling faster than a threshold rate, then a control 10 signal may be sent to a flow control device associated with the cooling loop (such as the pump 404) to increase the rate of flow of the working fluid thereby increasing the rate of heat exchange and thus the heating of the co-product stream 106. As will be appreciated, in such circumstances the temperature control system 600 may also adjust the cooling loop (e.g., via pump 5) and / or the operation of the heat source(s) such that sufficient heat is 15 captured for conveying to the co-product stream 106. Similarly, the integrated system 100 may comprise one or more temperature sensors 612 for monitoring the temperature of the co-product stream during storing by the storage infrastructure 204 (or parts thereof), or the temperature of the infrastructure itself (or parts thereof), and to control the associated thermal loop(s). One skilled in the art will 20 recognise that the discussion above regarding the handling of the co-product applies, mutatis mutandis, to the present example of co-product storage. The same is true for any temperature sensors in other heat sinks. Preferably, the temperature control system 600 is configured to control the heat integration system 400 and / or the at least one heat source such that the co-product stream 25   106 is substantially maintained above a threshold minimum temperature during handling and / or storage. The threshold minimum temperature may be the freezing point of the coproduct stream under the conditions of handling and / or storage. In some examples, the threshold temperature is the freezing point of substantially pure dehydrogenated product (e.g., organic acid). Where the alcohol is ethanol and the organic acid is acetic acid, the 30 threshold temperature may be about 17 degrees Celsius. Where the alcohol is methanol and the organic acid is formic acid, the threshold temperature may be about 9 degrees Celsius. Wherein the alcohol is propanol and the organic acid is propanoic acid, the threshold temperature may be about -20 degrees Celsius. Where the alcohol is butanol and the organic acid is butyric acid, the threshold temperature may be about -7 degrees Celsius. Where the alcohol is pentanol and the organic acid is pentanoic acid, the threshold temperature may be about -33 degrees Celsius. By maintaining the temperature of the coproduct stream above the freezing point, the heat integration system may substantially prevent freezing of the dehydrogenated product, thus maintaining the co-product stream in a fluid (e.g., liquid) state. Preferably, the temperature control system 600 is configured to control the heat integration system 400 and / or the at least one heat source such that the battery 206, where present, is substantially maintained above a threshold minimum temperature, such as the threshold temperatures already mentioned. The integrated system 100 may comprise one or more temperature sensors 608 for monitoring the temperature of the battery. The heat integration system 100 may further comprise one or more alternative or additional heat sinks 207 and associated temperature sensors 615. In cases where the integrated system 100 comprises multiple heat sinks, the temperature control system 600 advantageously controls heat transfer via the heat integration system 400 and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of the plurality of heat sinks. The temperature control system 600 may control a distribution of heat (i.e., controlling a proportion of heat to each heat sink) or select among or between the heat sinks depending on which of the heat sinks requires heat at a particular time (as determined by the sensors, for example). For example, referring to Figure 5, the temperature control system 600 may be configured to control heating loops such that the heating demands of the heat sinks are met. Such decisions may also, or alternatively, be based on heating priorities (e.g., a hierarchy of heat sinks). Preferably, preventing the co-product from freezing during handling and / or storage is prioritised over, say, maintaining the battery within a preferred temperature range. It will be appreciated that the aforementioned freezing point of the co-product stream may depend on the composition of the co-product stream (e.g., the purity of the dehydrogenated alcohol). As the skilled person will appreciate, the presence of other substances (e.g., diluents, such as water, or alcohol, such as un-dehydrogenated feed) may alter (e.g., increase) the temperature at which the co-product stream freezes and may therefore change the heating demands of the co-product stream. Hence, the integrated system preferably comprises one or more sensors for monitoring (e.g., measuring) the composition, or purity, of the co-product stream, or for detecting the presence or prevalence (e.g., quantity or proportion) of one or more substances in the co-product stream. The controller may be configured to adjust (preferably dynamically) the threshold minimum temperatures based on information pertaining to the composition of the coproduct stream, such as by data from such sensors. In some examples, the integrated system 100 comprises one or more sensors for monitoring (e.g., measuring) mass flow of the co-product in the handling infrastructure 202 and information pertaining to such may be communicated to the controller 602 for managing the distribution of heat by the heat integration system 400. For example, an increase in mass flow of the co-product may be associated with an increased heating load and so the controller may respond by increasing the amount of heat transferred to the handling infrastructure (e.g., by increasing the rate of flow of working fluid). It is also possible, alternatively or additionally, for one or more of the heating or cooling sections of the thermal network to comprise sensors 614, such as temperature sensors or mass flow measurement devices, for monitoring of the working fluid (temperature or flow rate) and for such information to be provided to and processed by the controller 602, as shown by example in the Figure 11. Such information may control, for example, the function of any central unit 424 to remove residual heat from the working fluid before delivering that working fluid to the heat sources. The integrated system 100 may comprise one or more sensors 616 for monitoring the ambient temperature and transmit data, such as temperature readings, to the controller 602. The controller 602 may be configured to receive and process the data, and to transmit control signals to a flow control device of the associated heating loop to adjust the rate of flow of the heated working fluid to the handling infrastructure 202. The controller 602 may also, or alternatively, be communicatively coupled to an external source of information 618, such as through a connection to the internet, or an online server, and be configured to receive information about current and forecasted weather. Such information may likewise be provided to and processed by the controller 602. The controller 602 may act pre-emptively to anticipate, for example, a forecasted temperature drop by increasing the temperature of, or transfer of heat to, one or more of the heat sinks in advance, and / or by increasing the heat generation of one or more heat sources. Similar control may be provided for anticipating, or responding to, a period of inactivity (or lack of sufficient heat generation) from heat source(s), as already discussed, such as by causing the handling infrastructure to substantially drain of co-product, or by elevating the temperature of the co-product stream (through increased heat generation or exchange) to a higher value above the threshold temperature. The specific example in Figure 11 shows various sensors and control devices of this kind that may advantageously be employed in the integrated system. Any combination of these elements may be provided. Heat integration for electrochemical process A further aspect of the invention is shown generally in Figure 12. In a general sense, the integrated system comprises a heat source, a heat sink, and a heat integration system configured to transfer heat from the heat source to the heat sink for use by the electrolyser system, either for vapourising the feed stream 102, or for meeting the thermodynamic requirements of the electrochemical process. The integrated system 100 comprises an electrolyser 300 comprising an electrochemical cell operable as an electrolytic cell and more specifically as an electrochemical dehydrogenator for producing hydrogen and a dehydrogenated product from an alcohol via an electrochemical dehydrogenation process, as per the previous discussion. The electrochemical process and the electrolyser are described in greater detail at the end of this specification. The applicant has recognised that there can be efficiency advantages in operating below the thermoneutral voltage. For example, there are no losses through waste heat. Thus, in the context of the present discussion, the electrolyser system is configured to operate the electrochemical cell (i.e., by controlling a potential or cell voltage applied across the electrodes) below the thermoneutral volage of the system such that the system is endothermic. Further advantages to a low potential are discussed further below. In such circumstances, a source of heat is required to account for the entropic term; otherwise, operation of the electrochemical cell below the thermoneutral voltage may not be possible. Additionally, the electrolyser 300, and in particular the electrochemical cell, may be designed to accept the substrate (e.g., substrate mixture comprising alcohol and water) as a vapour and therefore it may be necessary or at least desirable for the feed stream 102 to be provided at sufficient temperature for vapourisation, as described in greater detail below. With this in mind, the heat integration system 400 of the integrated system 100 may be arranged to transfer heat from one or more heat sources 500 in the system to the feed stream 102 and / or to the electrolyser 300 to at least assist in vapourising the feed stream for the electrochemical cell and / or accounting for the entropic term of the reaction when operating below the thermoneutral voltage. Preferably, one of the at least one heat sources is a hydrogen fuel cell 500 arranged to generate electricity 502 from the hydrogen produced by the electrolyser 300. The hydrogen fuel cell 500 may, for example, be used to charge a battery (not shown). As mentioned, the operation of the hydrogen fuel cell 500 may produce heat and hence the hydrogen fuel cell 500 is considered a heat source in the context of the present invention. The hydrogen fuel cell 500 may be a significant source of heat during operation given typical efficiencies (e.g., 50-65%), particularly for a high-energy or high-temperature hydrogen fuel cell, or for a fuel cell operated near its maximum rated capacity. When present and operational, a fuel cell may be responsible for producing most of the excess heat in a system. This heat is generally considered waste heat and so its removal may be desirable to maintain the temperature of the fuel cell within preferred operational conditions (preferable isothermal). The hydrogen fuel cell 500 may produce water as a by-product of the process and at least some of the heat produced by the operation of the hydrogen fuel cell may be carried by this water. In other words, the hydrogen fuel cell 500 is arranged to produce a heated by-product stream 108, i.e., a heated water stream. With the heat integration system 400, the integrated system 100 can advantageously cool the hydrogen fuel cell 500, thereby allowing the fuel cell 500 to operate within a desired temperature range (discussed elsewhere in this specification), while also providing a source of useful heat for vapoursing the feed stream 102 and / or meeting the thermodynamic requirements of the dehydrogenation process. By providing a source of heat for the reaction, the present invention can enable the electrolyser 300 to operate below thermoneutral voltage, thereby achieving greater efficiency. As one skilled in the art will appreciate, heat transferred to the feed stream 102 may facilitate both vapourisation and accounting for the entropic term of the reaction by adding heat to the process via the feed stream 102. Alternatively, or additionally, heat may be provided to the electrolyser system 300 for accounting for entropic term, such as via a heat exchanger device, independently of any heat added to the feed stream 102. In some examples, heat may be transferred to the feed stream 102 indirectly by heating the infrastructure (e.g., parts of the handling infrastructure of the feed stream 102). In some examples, heat may be transferred to the feed stream 102 at the point of delivery to, or by, the electrolyser system 300 for vapourisation. In some examples, heat may be transferred to the feed stream 102 more directly, such as by heat exchange between a working fluid and the feed stream via a heat exchanger device. This is described in more detail below. In some examples, the heat integration system 400 may be able to provide sufficient heat to vapourise the feed stream 102 (e.g., the alcohol thereof) for delivery to the electrolyser system 300. In some examples, the heat integration system 400 may be able to provide sufficient heat to account for the entropic term of the reaction. In some examples, though, additional (e.g., external) sources of heat may be provided in combination. Either way, the arrangement can at least aid in the vapourisation of the feed stream 102 and / or accounting for entropic term by providing heat. Suitable means for transferring heat in this way will be apparent to the skilled person. In the specific examples that follow, the heat integration systems 400 comprise of a thermal network for conveying working fluid, preferably in the form of a heated water stream 108 produced by the hydrogen fuel cell 500, wherein the thermal network is arranged for thermal communication between the heat source(s) and heat sink(s) via one or more heat exchangers, but this should not be understood as representing the extent of suitable arrangements. In other examples, the one or more heat exchangers may be replaced with one or more heat pumps. This may advantageously raise the quality of the heat from the heat source (for example, where a low-temperature hydrogen fuel cell is employed). Figure 13 shows a tenth example of an integrated system 100 according to the invention, in which the heated water stream 108 produced by a hydrogen fuel cell 500 is conveyed to the feed stream 102 of the electrolyser system 300 for heat transfer thereto via a heat integration system 400. In Figure 13, the heat integration system 400 comprises a by-product handling infrastructure 402 for conveying a heated water stream 108 produced by the hydrogen fuel cell 500 for heat exchange with the feed stream 102. The infrastructure 402 may comprise one or more pumps 404, fluid lines (e.g., tubes, pipes and the like), metering devices, flow measurement and control devices, and other such equipment as will be appreciated. The by-product handling infrastructure 402 is arranged for thermal communication between the heat source (in this case, the hydrogen fuel cell 500) and heat sink (in this case, the feed stream 102) and may therefore be regarded as a thermal network, with the heated water stream 102 acting as the working fluid thereof. The thermal network 402 may comprise pumps, such as pump 404, for affecting movement of the working fluid (i.e., heated water stream 108) therewithin. The thermal network is arranged for heat transfer between the working fluid (i.e., heated water stream 108) and the feed stream 102 and hence the thermal network may comprise a heat exchanger device 420 associated with the feed stream 102, as shown. As already mentioned, the heat transfer may be indirect, such as via heat exchange with the handling equipment of the feed stream, or more directly with the dehydrogenated product within the infrastructure. Since the heated water stream 108 may be produced substantially continuously during the operation of the hydrogen fuel cell 500, there may be no reason to recirculate the working fluid in a closed loop and hence the cooled water stream 110 (after heat exchange) may be subsequently conveyed to a water storage infrastructure (e.g., one or more containers), or discharged (e.g., drained or otherwise disposed of). In other examples, the water may be put to further use within the system. Figure 14 shows an eleventh example of an integrated system 100 according to the invention, in which the heated water stream 108 produced by the hydrogen fuel cell 500 is conveyed to the electrolyser 300 for heat transfer thereto via a heat integration system 400. The example shown in Figure 14 may be substantially the same as that shown in Figure 13 except that in this case the thermal network 400 is arranged for heat transfer between the working fluid (i.e., heated water stream 108) and the electrolyser 300 and hence the thermal network may comprise a heat exchanger device 410 associated with the electrolyser 300, as shown. In some examples, the heat exchanger device 410 and the electrolyser 300 are provided as part of an electrolyser unit. The heat provided to the electrolyser 300 may be used to assist in accounting for the entropic term of the electrochemical reaction, and / or used by the electrolyser system to assist in vapourising the feed stream 102. Figure 15 shows a twelfth example of an integrated system 100 according to the invention, in which the heated water stream 108 produced by the hydrogen fuel cell 500 is conveyed to both the feed stream 102 and the electrolyser system 300 for heat transfer thereto via the heat integration system 400. In Figure 15, the thermal network 400 comprises a pair of heating loops 408a, 408b, each loop siphoning off a portion of the working fluid for delivery to a respective heat sink 102, 300, as shown. A serial arrangement is also possible, but the parallel arrangement may advantageously provide greater control over the heat distribution between heat sinks and may help to ensure that each of the heat sinks is provided with working fluid at sufficient temperature for desired heat exchange. A first heating loop 408a may be arranged for heat transfer to the feed stream 102, as described with respect to Figure 13. The first heating loop 408a may comprise a heat exchanger device 420 associated with the feed stream 102. A second heating loop 408b may be arranged for heat transfer to the electrolyser 300, as described with respect to Figure 14. The second heating loop 408b may comprise a heat exchanger device 410 associated with the electrolyser 300 as above. Figure 16 shows a thirteenth example of an integrated system 100 according to the invention. Here, unlike the previous examples, the heat integration system 400 does not employ the heated water stream produced by the hydrogen fuel cell 500 as a working fluid and instead comprises a thermal loop for circulating a working fluid between the heat source and heat sink. Thus, the working fluid may be considered a dedicated working fluid, which is isolated within the thermal loop of the heat integration system. The working fluid may be any working fluid suitable for the demands of the system. In some examples, the working fluid is water, but unlike the previous examples this water is not produced by the hydrogen fuel cell 500. The thermal loop comprises a pair of heating loops 408a, 408b, as per Figure 15, with each loop delivering heated working fluid 406b to a respective heat sink for heat transfer via heat exchanger devices 420, 410 associated with the feed stream 102 and electrolyser 300. However, in other examples, the thermal loop may be arranged for heat transfer to a single one of the heat sinks (i.e., either the feed stream 102 or the electrolyser 300). The thermal loop in Figure 16 may be considered to comprise of a cooling section 420 and one or more heating sections 408a, 408b. The cooling section 420 is arranged for heat transfer from the heat source (e.g., hydrogen fuel cell 500) to the working fluid and in particular to provide cooled working fluid 406 to be heated by heat exchange with the hydrogen fuel cell 500, thereby cooling the hydrogen fuel cell. Hence, unlike previous examples, the cooling section 420 of the thermal loop may comprise, or be coupled to, a heat exchanger device 424 associated with (i.e., integrated with, disposed within, or otherwise thermally coupled for suitable heat exchange) the hydrogen fuel cell 500. The heat exchanger device 424 may be arranged for heat exchange between the working fluid and the heated water by-product of the hydrogen fuel cell 500. The one or more heating sections 408a, 408b are arranged as already described for Figure 15 above. As will be appreciated, with this arrangement the heat source may be something other than a hydrogen fuel cell (i.e., another heat generating process, device or component of the system). In one example, the hydrogen produced by the electrolyser is combusted rather than being conveyed to a fuel cell (e.g., in an internal combustion engine of a vehicle). In some examples, a portion of the hydrogen generated by the electrolyser is combusted, which may be solely for the purposed of generating heat. Combusting hydrogen can generate more heat than other processes. In one example, the heat source includes a battery. In another example, the heat source includes a braking system of a vehicle. Equally, the integrated system may comprise multiple heat sources including a hydrogen fuel cell and another heat source (a battery, for example). In some examples, the electrolyser may be operated as a heat source. In particular, as discussed above, if the electrolyser is operating above the thermoneutral voltage, then the reaction takes place and any 'extra' energy provided as an overpotential, above the thermoneutral voltage, is converted to heat in direct proportion to the potential above the thermoneutral voltage. Indeed, as mentioned, there can be advantages in operating above the thermoneutral voltage to increase the rate of the reaction if generating greater quantities of hydrogen is desirable. Additionally, the dehydrogenated product may be produced at a temperature above boiling and in some circumstances it may be desirable to cool the product stream such that the stream can be handled in a predominantly liquid state. It is noted again that the electrolyser may still be operated at a relatively low potential to favour partial oxidation of the alcohol, as discussed in more detail below. Figure 17 shows a fourteenth example of an integrated system 100 according to the invention. Here, the electrolyser 300 is employed as a heat source and the heat integration system 400 is configured to transfer heat from the electrolyser 300 to the feed stream 102 to at least assist in vapourising the feed stream. Like Figure 16, the heat integration system comprises a thermal loop for circulating a working fluid between the heat source and heat sink. Hence, the heat integration system 400 comprises a heating section for heat exchange with the feed stream via a heat exchanger device 420 and a cooling section for heat exchange with the electrolyser via a heat exchanger device 410 associated with the electrolyser 300. In other examples, the heated co-product stream is employed as the working fluid and is conveyed, such as via co-product handling infrastructure, for heat transfer with the feed stream 102, such as via the heat exchanger device 420, in a manner similar to the heated water stream of the hydrogen fuel cell. In some examples, both the electrolyser and the hydrogen fuel cell are employed as heat sources for heat transfer to the feed stream and any other heat sinks in the system as desired. While the integrated system 100 in Figure 17 is shown to comprise a hydrogen fuel, this is optional in this example. The hydrogen may instead be combusted, or simply conveyed to hydrogen storage infrastructure. In any of the preceding examples, the integrated system may comprise additional heat sinks besides the feed stream and / or electrolyser. For example, in some circumstances the battery is a heat sink of the system. Central heat exchanger unit As per the foregoing discussion, one might expect the cooling load and the heating load of the integrated system to differ, such that the demand on the heat integration system 400 is different for the heat source(s) compared to the heat sink(s). For example, the preferred temperature for the operation of the heat sources, and the amount of heat generated, may be different from (e.g., lower than) the desired, or necessary, temperature for the feed stream 102 or electrolyser 300. Hence, there may be advantages in separating the cooling and heating loops of the heat integration system so that each can be controlled or operated independently. Accordingly, the optional section 422 discussed in relation to Figure 6 may be employed in the present examples, as shown by the presence of the dashed box. This may be employed in any of the heat integration systems described to provide greater control over the heat integration system for meeting the heating and cooling demands of the heat exchange at the either side of the system. In some examples, like those of Figures 13-15, the first working fluid is the heated water stream 102 from the hydrogen fuel cell, in which case the central unit 424 is configured to receive the heated water stream 102 (as 406b) and outturn a cooled water stream (as 406a) (after heat exchange with the second working fluid). The cooled water stream 406a may be conveyed to storage or to another part of the system, or simply disposed of (e.g., drained). In other examples, like that of Figure 16 in which the first working fluid is a dedicated working fluid employed for heat exchange with the hydrogen fuel cell via a heat exchanger device, as already discussed, the cooled first working fluid 406a outturned by the central unit 424 (after heat exchange with the second working fluid) may be recirculated back to the hydrogen fuel cell 500. The second working fluid may be a dedicated working fluid circulated in one or more heating loops of the thermal network 400 between the central unit 424 and the heat source(s). With the central unit 424, the cooling loop(s) and the heating loop(s), and in particular the movement of working fluid therewithin, can be controlled independently. The cooling loop and the one or more heating loops may comprise pumps 404, to affect movement of the working fluids, and that movement may be different. For example, the rate of flow of working fluid in the cooling loop 420 may be greater than the rate of flow of working fluid in the heating loop 408a, 408b. The central unit 424 may be arranged to provide further conditioning of the first working fluid to further remove heat (i.e., remove residual heat) before being circulated again at the desired temperature in the cooling loop. Equally, the central unit 424 may be arranged to provide further conditioning of the second working fluid to add additional heat (i.e., further increase the temperature of the second working fluid) to meet the demands of the heat sink(s) (i.e., for vapourising the feed stream and / or meeting the thermodynamic requirements of the dehydrogenation reaction in the electrolyser system). Additionally, the central unit 424 can enable the use of different (e.g., specialised) working fluids suitable for the cooling section 420 and the heating section 408a, 408b, though in some instances the first working fluid and the second working fluid may be the same substance (e.g., water). For example, it may be desirable when employing the heated water stream from the hydrogen fuel cell as a working fluid, for the heating duties at the heat sink(s) to be serviced by a separate working fluid. As in the preceding examples, the one or more cooling loop are arranged for heat transfer between the heat source(s) and the first working fluid and to provide cooled working fluid 406a to be heated by heat exchange with the heat source(s), thereby cooling the heat source(s), or to extract heated fluid (i.e., the heated water stream) from the heat source (i.e., the hydrogen fuel cell), thereby cooling the heat source. The heated first working fluid 406ba is then conveyed back to the central unit 424. Likewise, the one or more heating loops are arranged for heat transfer between the second working fluid and the heat sink(s) and in particular to provide heated working fluid 406bb to be cooled by heat exchange with heat sink(s). The one or more heating loops are further arranged to recirculate the cooled working fluid 406b back to the central unit 424, where it is brought into thermal communication with the cooling loop to affect heat transfer therebetween. In particular, the central heat exchanger is arranged to provide for heat transfer from the heated first working fluid to the cooled second working fluid, so as to provide cooled first working fluid and heated second working fluid for the functions already described. In some examples, a central unit may be employed to combine a plurality of cooling loops for a plurality of heat sources, such that each of the heating loops contributes to heating a second working fluid, thereby elevating the temperature of the second working fluid above what might be achieved with any one heat source. In other examples, heat pumps may be employed for this purpose. Temperature sensing and control Preferably, the heat integration system 400 is configured to control the distribution of heat from one or more heat sources to one or more of the heat sinks, such as via one or more controller devices of a temperature control system 600. For example, the heat integration system may be configured to control an amount, or rate, of heat transferred, or to select among or switch between heat sources and / or heat sinks, to meet the demands or priorities of the system. In the illustrated examples, where the heat integration system 100 comprises of heat exchanger devices and circulating working fluid, the temperature control system 600 may be configured to control the flow of working fluid around heating and / or cooling loops, by communicating with (e.g., transmitting control signals to) flow control devices of the heat integration system, such as pumps 404. The temperature control system may also be configured to control the operation of the electrolyser system 300 and / or hydrogen fuel cell 500, such as via communicative coupling between the temperature control system 600 and the electrolyser system 300 and / or hydrogen fuel cell 500 or an associated controller device. For example, the temperature control system 600 may be configured adjust the potential applied across the electrochemical cell by the electrolyser system 300 to switch between particular operational states, such as above the thermoneutral voltage, at the thermoneutral voltage, between the thermoneutral voltage and the minimum voltage, at the minimum voltage, or even below the minimum voltage to cease the reaction. The temperature control system 600 may be configured to adjust the operation of the electrolyser system 300 between such states to control the rate of the reaction. As will be appreciated from the foregoing discussion, this may also control the amount of heat required by the electrolyser system. The same may be true of the hydrogen fuel cell 500 to control the amount of heat generated. Preferably, such control is based on information about environmental conditions (e.g., ambient temperature) and / or internal conditions (e.g., temperatures of infrastructure, or the feed stream, or rate of flow or composition of the feed stream). The integrated system 100 may comprise one or more sensors for monitoring (e.g., measuring) the temperature of the feed stream (either directly or via the infrastructure) and / or one or more sensors for monitoring the composition of the feed stream (or at least the presence, or prevalence, of one or more predetermined substances). The integrated system may comprise a device for monitoring the mass flow of the feed stream. The integrated system may comprise a sensor for monitoring the ambient temperature. The temperature control system 600 may be communicatively coupled to the one or more sensors (e.g., by wired or wireless communication technology) and configured to receive information (e.g., measurement data) from the sensors and to control the distribution of heat accordingly. The temperature control system 600 may be configured to process the received information, such as by comparing received values to one or more thresholds, or ranges, and to transmit control signals based on said processing. The temperature control system 600 may be configured to calculate, for example, the temperature of the feed stream 102 required to meet the demands of the system, such as for vapourising the feed stream 102 or meeting the thermodynamic requirements of the dehydrogenation reaction. Hence, with this arrangement, the thermal network 400 of the heat integration system may be considered a temperature control loop. Figure 18 shows a fifteenth example of an integrated system 100 comprising a temperature control system 600 (in this example having a central controller device 602) and a plurality of sensors 604-616. For explanatory purposes, the illustrated integrated system 100 is based on that of Figure 15, however one skilled in the art will recognise that the teaching could be applied to any of the described arrangements. Additionally, while various sensors and communication links are shown, it will be understood that the integrated system 100 can comprise any combination of sensor and controller function, or any single sensor and controller function. The integrated system 100 may comprise a temperature sensor 620 for monitoring the temperature of the feed stream 102, or the temperature of the infrastructure for handling the feed stream (or parts thereof), and to transmit data, such as temperature readings, to the temperature control system 600 (e.g., the central controller device 602). The temperature control system 600 may be configured to receive the data via communication link 620a and to process the data, and to transmit control signals (not shown) to a flow control device of the thermal network, such as the pump 404, (or an associated heating loop thereof) to adjust the rate of flow of the heated working fluid to the feed stream 102. The temperature control system 600 may be configured to transmit control signals to the hydrogen fuel cell 500 (e.g., a controller device thereof), or other heat source, to adjust the amount of heat produced. For example, the temperature control system 600 may be configured to monitor the temperature of the feed stream 102 and to control the thermal network 400 to maintain the temperature of the feed stream 102 at a particular temperature, or within a particular temperature range, such as from about 50°C to about 120°C (discussed further elsewhere in this specification). The integrated system 100 may comprise a temperature sensor 604 arranged to monitor the temperature of the electrolyser system 300 and to transmit data, such as temperature readings, via a communication link 604a to the temperature control system. The temperature control system 600 may be configured to receive and process the data, and to transmit control signals (not shown) to a flow control device of the thermal network (e.g., the pump 404) to adjust the rate of flow of the working fluid to the electrolyser system based on said processing. The temperature control system 600 may be configured to transmit control signals to the hydrogen fuel cell 500 (e.g., a controller device thereof), or other heat source, to adjust the amount of heat produced. For example, the temperature control system 600 may be configured to monitor the temperature of the electrolyser 300 and to control the thermal network 400 to maintain the electrolyser 300 at a particular temperature, or within a particular temperature range. Preferably, the temperature control system 600 is configured to maintain the temperature of the electrolyser 300 at about 100 degrees Celsius, or between 100 degrees Celsius and 150 degrees Celsius, though in some circumstances it may be desirable to operate the electrolyser 300 at a temperature as low as about 80°C, or as high as about 190°C or about 200°C or 250°C. The integrated system 100 may comprise a temperature sensor 606 arranged to monitor the temperature of the hydrogen fuel cell 500 and to transmit data, such as temperature readings, to the temperature control system 600. The temperature control system 600 may be configured to receive and process the data, and to transmit control signals to a flow control device of the thermal network (e.g., the pump 404) to adjust the rate of flow of the heated water stream 108 from, or cooled working fluid to, the hydrogen fuel cell 500 based on said processing. The temperature control system 600 may be configured to transmit control signals to the hydrogen fuel cell 500 (e.g., a controller device thereof), or other heat source, to adjust the amount of heat produced. For example, the temperature control system 600 may be configured to monitor the temperature of the hydrogen fuel cell 500 and to control the thermal network 400 to maintain the temperature of the hydrogen fuel cell 500 at a particular temperature, or within a particular temperature range. Preferably, the temperature control system 600 is configured to maintain the temperature of the hydrogen fuel cell 500 within the preferred operating temperatures discussed elsewhere in this specification (e.g., from about 60°C to about 80°C from a PEM fuel cell). Similarly, where the integrated system 100 comprises other, or alternative, heat sources, such as the battery, the integrated system 100 may comprise one or more temperature sensors for monitoring the temperature of those heat sources, and may be configured to control the associated thermal loop(s) in a manner analogous to that discussed above, mutatis mutandis. In cases where the integrated system 100 comprises multiple heat sources, the temperature control system 600 advantageously selects among or between the heat sources depending on which of the heat sources is generating heat at a particular time, or how much heat is being generated by each of the heat sources (as determined by the sensors, for example). For example, the temperature control system 600 may be configured to control the thermal network 400 such that the cooling demands of the heat sources, or heat extraction demands, are met. Such decisions may also, or alternatively, be based on cooling priorities (e.g., a hierarchy of heat sources). Preferably, the temperature control system 600 is configured to control the heat integration system 400 and / or the at least one heat source such that the feed stream 102 is substantially maintained at sufficient temperature for vapourisation. The sufficient temperature may be the boiling point of the feed stream under the conditions of handling. In some examples, the temperature is the boiling point of the alcohol used as the substrate for the reaction. Where the alcohol is ethanol, the temperature may be about 78°C. Where the alcohol is methanol, the threshold temperature may be about 65°C. Wherein the alcohol is propanol, the threshold temperature may be about 97°C. Where the alcohol is butanol, the threshold temperature may be about 118°C. Where the alcohol is pentanol, the threshold temperature may be about 113°C. In cases where the integrated system 100 comprises multiple heat sinks, the temperature control system 600 advantageously controls heat transfer via the heat integration system 400 and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of the plurality of heat sinks. The temperature control system 600 may control a distribution of heat (i.e., controlling a proportion of heat to each heat sink) or select among or between the heat sinks depending on which of the heat sinks requires heat at a particular time (as determined by the sensors, for example). For example, the temperature control system 600 may be configured to control heating loops such that the heating demands of the heat sinks are met (i.e., vapourising the feed stream and meeting the thermodynamic requirements of the dehydrogenation reaction). Such decisions may also, or alternatively, be based on heating priorities (e.g., a hierarchy of heat sinks). It will be appreciated that the aforementioned boiling point of the feed stream may depend on the composition of the feed stream. As the skilled person will appreciate, the presence of other substances (e.g., diluents, such as water, or any dehydrogenated alcohol recycled from the electrolyser system), may alter the temperature at which the feed stream vapourises and may therefore change the heating demands of the feed stream. Hence, the integrated system 100 preferably comprises one or more sensors for monitoring (e.g., measuring) the composition, or purity, of the feed stream, or for detecting the presence or prevalence (e.g., quantity or proportion) of one or more substances in the feed stream (e.g., water). The temperature control system 600 may be configured to adjust (preferably dynamically) the desired temperatures based on information pertaining to the composition of the feed stream, such as by data from such sensors. In some examples, the integrated system 100 comprises one or more sensors for monitoring (e.g., measuring) mass flow of the feed and information pertaining to such may be communicated to the temperature control system for managing the distribution of heat by the heat integration system. For example, an increase in mass flow of the substrate may be associated with an increased heating load and so the temperature control system may respond by increasing the amount of heat transferred to feed stream (e.g., by increasing the rate of flow of working fluid). It is also possible, alternatively or additionally, for the thermal network 400 (e.g., one or more of the heating or cooling sections) to comprise sensors 614, such as temperature sensors or mass flow measurement devices, for monitoring of the working fluid (temperature or flow rate) and for such information to be provided to and processed by the temperature control system. Such information may control, for example, the function of any central unit 424 to remove residual heat from the working fluid before delivering that working fluid to the heat sources. For example, the integrated system 100 may comprise a temperature sensor 614 for monitoring the temperature of the heated water stream 108 from the hydrogen fuel cell 500 (or, where a dedicated working fluid is employed, the temperature of that working fluid). The integrated system 100 may comprise one or more sensors 616 for monitoring the ambient temperature and transmit data, such as temperature readings, to the temperature control system 600. The temperature control system 600 may be configured to receive and process the data, and to transmit control signals to a flow control device of the thermal network 400 to adjust the rate of flow of the heated working fluid to the feed stream 106 and / or electrolyser system 300. The temperature control system 600 may also, or alternatively, be communicatively coupled to an external source of information 618, such as through a connection to the internet, or an online server, and be configured to receive information about current and forecasted weather. Such information may likewise be provided to and processed by the temperature control system 600. The temperature control system 600 may act pre-emptively to anticipate, for example, a forecasted temperature drop by increasing the temperature of, or transfer of heat to, one or more of the heat sinks in advance, and / or by increasing the heat generation of one or more heat sources. The specific example in Figure 18 shows various sensors and control devices of this kind that may advantageously be employed in the integrated system. Any combination of these elements may be provided. Combination While Figures 1-11 and 12-18 have to some extent been discussed separately, it will be appreciated that the two can be combined to provide an integrated system 100 advantageously configured to, for example, assist in preventing the dehydrogenated product from freezing during handling and / or storing (as per Figures 1-11) as well as assist in vapourising the feed stream for the electrolyser and / or meeting the thermodynamic requirements of the electrochemical process. Figure 19 generally illustrates an integrated system 100 comprising a combination of heat sources and heat sinks from the previous examples. The heat sink(s) may include one or more of: the feed stream; the electrolyser; the infrastructure for handling and / or storing the co-product stream. Equally, the heat source(s) may include one or more of: the hydrogen fuel cell, or hydrogen combustion means; the electrolyser (when not operated as a heat sink). Figure 20 shows a sixteenth example of an integrated system 100, in which the heated water stream 108 from the hydrogen fuel cell 500 is conveyed, by the heat integration system 400, to both the feed stream 102 and to the handling and storage infrastructure 202,204. This is just one example and the skilled person will readily appreciate the features of the previous examples that may be combined for specific desiderata. In particular, the benefits of a temperature control system 600 for such combinations of heat sources and heat sinks will be readily apparent. Electrochemical process The electrochemical dehydrogenation process is a process for partially oxidising an alcohol to produce hydrogen and a dehydrogenated product. In one example, it is a process for partially oxidising a mixture of water and alcohol (provided in a feed stream) to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product (e.g., organic acid). An example of this reaction generally may be represented by the following reactions (in which n is, e.g., 0 to 8): Anode reaction: CH3(CH2)nOH + H2O -CH3(CH2)n-1COOH + 4H+ + 4e - (in acidic conditions) CH3(CH2)nOH + 4OH - - CH3(CH2)n-1COOH + 3H2O + 4e - (in alkaline conditions) Cathode reaction: 4H+ + 4e - — 2H2 (in acidic conditions) 4H2O + 4e - — 4OH - + 2H2 (in alkaline conditions) Overall reaction (both acidic and alkaline conditions) CH3(CH2)nOH + H2O -CH3(CH2)n-1COOH + 2H2. The partial oxidation may be contrasted with full oxidation wherein the alcohol is fully oxidised to carbon dioxide or a carbonate. Selectivity for partial oxidation (vs full oxidation) is affected by various factors such as the choice of catalyst and potential applied to the electrolyser. Generally, a lower potential applied to the anode will favour the partial oxidation. The alcohol functions as an organic hydrogen carrier which may be oxidised to produce hydrogen via a hydrogen precursor. The alcohol is an organic compound comprising one or more hydroxyl groups attached to an alkyl group. The alcohol may be a straight chain alcohol, such as n-propanol, or a branched alcohol, such as iso-propanol. In some embodiments, the alcohol is a C1-8 alcohol. In some embodiments, the alcohol is a C1-5 alcohol. Preferably, the alcohol is a C1-3 alcohol, including but not limited to, methanol, ethanol, n-propanol, isopropanol, methylene glycol, ethylene glycol, propylene glycol, gylcerol or a combination of any two or more thereof. In some embodiments, the alcohol is ethanol. In some embodiments, the alcohol is a biofuel derived from a biological source, such as bioethanol derived from, e.g., biomass. The alcohol may be supplied to the anode as a liquid, a vapour or a combination thereof. The dehydrogenated product is a partial oxidation product of the alcohol. The dehydrogenated product is preferably a carboxylic derivative of the alcohol. For example, when the alcohol is ethanol, the dehydrogenated product may be acetic acid. Those persons skilled in the art will appreciate that depending on the conditions, e.g. at a basic pH, the carboxylic acid may instead exist as the corresponding acetate salt. As used herein, terms such as "carboxylic acid", "acetic acid" and other related terms are intended to describe the dehydrogenated product in the acid and acetate forms, as appropriate. The dehydrogenation product may include an aldehyde derivative of the alcohol. In some embodiments, the dehydrogenated product is a carboxylic acid, an aldehyde or a combination thereof. For example, the carboxylic acid may be a C1-5 carboxylic acid, including but not limited to, formic acid, acetic acid, glycolic acid, glyoxylic acid, oxalic acid, propanoic acid, glyceric acid, lactic acid, acrylic acid, butyric acid, pentanoic acid or a combination of any two or more thereof. As described, the dehydrogenated product may be a valuable commodity product, such as acetic acid. Accordingly, in some embodiments, the invention provides a process for partially oxidising an alcohol to produce a dehydrogenated product, wherein the dehydrogenated product is a commodity product. Alternatively, in some embodiments, the dehydrogenated product is reduced back to the alcohol such that it may be reused as a liquid organic hydrogen carrier. The hydrogen precursor is reduced to hydrogen at the cathode. The hydrogen precursor may be, e.g., a proton or water. The electrochemical process may also be seen as a process for the production of a dehydrogenated product from an alcohol, comprising the steps of (i) contacting the alcohol with the anode and (ii) applying a low voltage to an anode to partially oxidise the alcohol to produce the dehydrogenated product. The electrochemical process may also be seen as a process for the production of hydrogen from an alcohol, comprising the steps of (i) contacting the alcohol with the anode, (ii) applying a low voltage to the anode to partially oxidise the alcohol to produce a hydrogen precursor, and (iii) reducing the hydrogen precursor to hydrogen at a cathode. The oxidation process carried out by the electrolyser is selective for partial oxidation of the alcohol. Selectivity may be measured by the conversion of the alcohol to the dehydrogenated product. The electrolyser may achieve above 95% selectivity for partial oxidation of the alcohol, i.e. above 95% of the alcohol that is consumed at the anode is converted to the dehydrogenated product (on a mol% basis). Preferably, the electrolyser achieves above 98% selectivity for partial oxidation of the alcohol. Preferably, above 98% of the alcohol consumed at the anode is converted to the carboxylic acid (on a mol% basis). In some examples, the co-product stream comprises at least about 80% of the 5 dehydrogenated product (e.g., organic acid). In some examples, the co-product stream comprises at least about 90% of the dehydrogenated product (e.g., organic acid). In some examples, the co-product stream comprises at least about 95% of the dehydrogenated product (e.g., organic acid). In some examples, the co-product stream comprises at least about 98% of the dehydrogenated product (e.g., organic acid). In some examples, the co-10 product stream comprises at least about 99% of the dehydrogenated product (e.g., organic acid). In some examples, the co-product stream comprises at least about 95% of a carboxylic acid, an aldehyde or a combination thereof. In some examples, the co-product stream comprises at least about 98% of a carboxylic acid, an aldehyde or a combination thereof. In some embodiments, the co-product stream comprises at least about 99% of a carboxylic 15 acid, an aldehyde or a combination thereof. In some examples, the alcohol is a C1-3 alcohol and the co-product stream comprises at least about 80% of a C1-3 carboxylic acid, a C1-3 aldehyde or a combination thereof. In some examples, the alcohol is a C1-3 alcohol and the co-product stream comprises at least about 90% of a C1-3 carboxylic acid, a C1-3 aldehyde or a combination 20 thereof. In some examples, the alcohol is a C1-3 alcohol and the co-product stream comprises at least about 95% of a C1-3 carboxylic acid, a C1-3 aldehyde or a combination thereof. In some examples, the alcohol is a C1-3 alcohol and the co-product stream comprises at least about 98% of a C1-3 carboxylic acid, a C1-3 aldehyde or a combination thereof. In some examples, the alcohol is a C1-3 alcohol and the co-product stream 25 comprises at least about 98% of a C1-3 carboxylic acid, a C1-3 aldehyde or a combination thereof. In some examples, the alcohol is ethanol and the co-product stream comprises at least about 95% of acetic acid, acetaldehyde or combination thereof. In some examples, the alcohol is ethanol and the co-product stream comprises at least about 98% of acetic acid, acetaldehyde or combination thereof. In some examples, the alcohol is ethanol and the co-30 product stream comprises at least about 99% of acetic acid, acetaldehyde or combination thereof. In some examples, the product stream consists of the dehydrogenated product (e.g., organic acid), wherein the dehydrogenated product is a carboxylic acid, an aldehyde or a combination thereof. In some examples, the product stream consists essentially of the dehydrogenated product, wherein the dehydrogenated product is a carboxylic acid, an aldehyde or a combination thereof. In some examples, the product stream consists of a carboxylic acid. In some examples, the product stream consists essentially of a carboxylic acid. In some embodiments, it may be beneficial to minimise the amount of full oxidation products (e.g. CO2 and CO). For example, hydrogen gas to be used in a fuel cell or other power generating device preferably contains minimal CO2 and CO contamination. Accordingly, it is beneficial to minimise the amount of CO2 and / or CO contamination in the hydrogen output from the electrolyser. The hydrogen output from the electrolyser may comprise about 2 vol% or less CO2. Preferably, the hydrogen output from the electrolyser contains less than about 0.5 vol% CO2, more preferably, less than 0.1 vol%. The hydrogen output from the electrolyser comprises less than 10 ppm CO. In some examples, the product stream comprising hydrogen comprises about 2 vol% or less CO2. In some examples, the product stream comprising hydrogen comprises less than about 0.5 vol% CO2. In some examples, the product stream comprising hydrogen comprises less than 0.1 vol% CO2. In some examples, the product stream comprising hydrogen comprises less than 10 ppm CO. In some examples, the product stream comprising hydrogen comprises 2 vol% or less CO2 and less than 10 ppm CO. Electrolyser The electrolyser 300 may be part of the electrolyser system for partially oxidising an alcohol to produce hydrogen and a dehydrogenated product. The electrolyser may be arranged for connection to an energy source, such as a battery, for applying a potential to the electrolyser. Preferably, this potential is applied and / or controlled via an electrolyser system or controller as already described. In some examples, the integrated system comprises the electrolyser and the energy source. The electrolyser comprises a vessel divided by a separator into a first volume and a second volume. The first volume houses an anode comprising a partial oxidation catalyst capable of partially oxidizing a mixture of an alcohol and water to produce a partial dehydrogenation product and a hydrogen precursor. The second volume houses a cathode comprising a reduction catalyst capable of converting the hydrogen precursor to hydrogen. An anode of the electrolyser comprises a partial oxidation catalyst. The term "partial oxidation catalyst" as used herein refers to any catalyst capable of partially oxidising 5 the alcohol to produce a hydrogen precursor and a dehydrogenated product. A person skilled in the art could select a suitable catalyst and appropriate conditions for achieving partial oxidation. Suitable catalysts include, but are not limited to, a transition metal or a transition metal oxide, such as a Pd catalyst, Pt catalyst and / or a Pt-Sn catalyst. The anode may comprise the catalyst embedded on a substrate. Suitable substrates may include a 10 carbon-substrate (such as graphite, carbon black or carbon paper), a Ti substrate and / or Ni substrate. The anode may comprise 1 to 50 wt% of the catalyst, e.g., about 5 to 40 wt%, 10 to 30 wt%, 15 to 25 wt% or 20 wt%. The catalyst may be in the form of nanoparticles, e.g. particles having an average particle size of about 1 to 10 nm. In some embodiments, the anode comprises Pd nanoparticles on carbon black. In some embodiments, the anode 15 comprises 20 wt% Pd nanoparticles on carbon black. The partial oxidation catalyst may also be in the form of a single atom catalyst. A cathode of the electrolyser comprises a reduction catalyst. The term "reduction catalyst" as used herein refers to any catalyst capable of reducing the hydrogen precursor to hydrogen. A person skilled in the art could select a suitable catalyst and conditions to 20 reduce the hydrogen precursor to hydrogen. Suitable catalyst include, but are not limited to, a Pt catalyst, a Ni catalyst a Ru catalyst, a Fe catalyst or a combination of two or more thereof. The cathode may comprise the reduction catalyst embedded on a substrate. Suitable substrates may include a carbon substrate (such as graphite, carbon black or carbon paper), a Ti substrate and / or an Ni substrate. The reduction catalyst may be in the form of 25 nanoparticle, e.g. particles having an average particle size of about 1 to 10 nm.The reduction catalyst may be in the form of a single atom catalyst. The electrolyser comprises a separator between the anode and cathode. The separator functions to restrict flow of fluids between the anode to the cathode. Flow of fluids from the anode to the cathode, or vice versa, can reduce the efficiency of the process, 30   e.g., exposing the cathode to the alcohol can lead to poisoning of the reducing catalyst and reduce the efficiency and lifespan of the catalyst. Ideally, only the hydrogen precursor produced at the anode may pass through the separator to react at the cathode. In some embodiments, the separator is a porous non-conductive membrane, such as Celgard microporous polymer. In some embodiments, the separator is an ionically-conductive membrane, such as a cation exchange membrane, an anion exchange membrane or a proton exchange membrane (PEM). Suitable ionically-conductive membranes include, but are not limited to, Nation, Piperion, Sustainion and Fumatech. In some examples, the PEM comprises a polybenzimidazole (PBI) polymer. In some examples, the PEM is a phosphoric acid doped PBI membrane or an ion-pair PBI membrane. Those persons skilled in the art will appreciate other conventional separators known in the art may be useful in the invention. Advantageously, an ionically conductive membrane may also function as the electrolyte removing the need for a further electrolyte. In some embodiments, there is a fluid between the separator and the cathode (e.g. in the second housing) to provide a medium for transporting the hydrogen precursor to the cathode. For example, when the separator is an anion exchange membrane, the electrolyser may comprise a fluid such as water or water vapour between the separator and the cathode. Advantageously, when the separator is a PEM, the hydrogen precursor (e.g. proton) may directly contact the cathode without the need for a fluid. The electrolyser may comprise an electrolyte chosen from those known to those persons skilled in the art. Electrolytes include acidic electrolytes, basic electrolytes, salt electrolytes and ionic liquid electrolytes. While a vast array of acids, bases, or ionic liquids can be used as electrolytes, electrochemical processes are affected by the choice of electrolytes and in particular, are different in basic vs acidic electrolytes. In some embodiments, the electrolyte is an aqueous solution comprising a salt, such as a potassium or sodium salt. In some embodiments, the potassium or sodium salt is a chloride or hydroxide salt. In some embodiments, the electrolyte is a 1-30 wt% aqueous salt solution, e.g., a 1-30 wt% aqueous KCI or KOH. The potential is selected to favour partial oxidation of the alcohol (vs full oxidation). For this purpose, generally the potential should be as low as possible. For example, from above 0 to about 1.2 V, about 0.01 to 0.5 V or about 0.05 to 0.2 V. In some examples, the potential is less than 1.0 V. In some examples, the potential is less than 0.8V. When operated in combination with a fuel cell, the potential applied to the anode should be lower than the output voltage of the fuel cell. Therefore, when combined with a fuel cell, the potential applied to the electrochemical cell is preferably less than about 1.2V. In situations where the electrolyser is a heat sink, the potential is preferably below a thermoneutral voltage, which may be about 0.2 V. Preferably, the potential is within a range having a lower bound defined by the minimum voltage (e.g., 60 mV) and an upper bound defined by the thermoneutral voltage (e.g., 0.2 V). In situations where the electrolyser is operated as a heat source, the potential is preferably above a thermoneutral voltage, which may be about 0.2 V. Preferably the potential is within a range having a lower bound defined by the thermoneutral voltage (for the purposes of generating heat) and an upper bound selected to favour partial oxidation of the alcohol. The operating conditions for the electrolyser may be selected according to the intended application and components of the system. For example, when the alcohol is supplied to the anode as a liquid, the electrolyser is preferably operated at a temperature of less than, or at most, about 100°C and more preferably within a range of about 25 to 78°C. When the alcohol is supplied to the anode as a vapour, the electrolyser is preferably operated at a temperature of less than, or at most, about 250°C, or less than, or at most, about 200°C, or less than, or at most, about 150°C and more preferably at a temperature of about 55 to 110°C. Generally, the electrolyser is operated in a temperature range of about 0 to 150°C or 0 to 200°C or 0 to 250°C. Generally, the electrolyser is operated at a pressure of about 1 to 50 bar. In some embodiments, the electrolyser is operated in at a pressure of about 10-20 bar. In some examples, the electrolyser is operated at a temperature in a temperature range of about 50 to 250°C, 50 to 200°C, 50 to 150°C, 50 to 100°C, 80 to 250°C, 80 to 200°C, 80 to 150°C, 80 to 100°C, 100 to 250°C, 100 to 200°C, 100 to 150°C, 150 to 250°C or 150 to 200°C. In some examples, the electrolyser is operated at a temperature of about 55 to 110°C. In some examples, the electrolyser is operated at a temperature above about 50°C. In some examples, the electrolyser is operated at a temperature above about 60°C, 70°C, 80°C, 90°C or 100°C. In some examples, the electrochemical cell is operated at a temperature above about 150°C. The electrolyser may be operated at a pH of 0 to 14. The preferred pH range may be selected based on various factors, such as the components of the system and desired hydrogenation product(s). For example, in some embodiments, the electrolyser comprises a Nation separator with no additional electrolyte and is operated at a pH of about 0 to 2. In some other embodiments, the electrolyser is operated at a pH of 7 or above to minimise formation of a condensation by-product of the dehydrogenated product (e.g., ethyl acetate when the alcohol is ethanol). In some examples, the electrolyser comprises a single electrochemical cell as described above. In some other examples, the electrolyser comprises two or more electrochemical cells operating in series. The electrochemical cell may be provided in the form of a layered cell. For example, the electrochemical cell may comprise an anode layer, e.g. carbon paper embedded with the partial oxidation catalyst, contacting one side of the separator and a cathode layer, e.g. carbon paper embedded with the reducing catalyst, contacting an opposing side of the separator. Alternatively, the electrochemical cell may comprise the anode, the cathode and the separator, wherein the partial oxidation catalyst of the anode is coated on a surface of the separator the reducing catalyst of the cathode is coated on an opposing surface of the separator. In the layered electrochemical cell, the separator is preferably a proton exchange membrane. The layered electrochemical cell may be preferable in some embodiments, e.g., when providing a electrolyser comprising two or more electrochemical cells. In those embodiments, the electrolyser may comprise a stack of electrochemical cells. Electrolyser and fuel cell As already discussed, the electrolyser may operate in combination with a power generating device for converting the hydrogen to power, e.g. a combustion engine or fuel cell. Accordingly, in some embodiments, at least a portion of the hydrogen may be conveyed to a combustion engine. The combustion engine may be for powering a vehicle, such as a car, ship, train or plane. In some examples, at least a portion of the hydrogen produced in the electrolyser is conveyed to a fuel cell in which the hydrogen is converted to electricity and water. The combination of electrolyser and fuel cell provides a closed system for producing hydrogen and converting the hydrogen to electricity (i.e. the hydrogen produced in the electrolyser is utilised directly within the system). Accordingly, the combination of electrolyser and fuel cell may be utilised in mobile applications, e.g. for powering a vehicle wherein the vehicle is fuelled by the alcohol. For this purpose, vehicle may be refuelled by replenishing the alcohol consumed by in the electrolyser. Alternatively, the combination of electrolyser and fuel cell may be utilised in stationary applications. Advantageously, producing hydrogen in a separate component (the electrolyser) from the fuel cell reduces poisoning of the fuel cell cathode, e.g. by the alcohol, compared to direct ethanol fuel cells. In some examples, the fuel cell is a single cell. In some other examples, the fuel cell is two or more cells operating in series. The operating conditions for the hydrogen fuel cell may be selected according to the intended application and components of the system. The temperature range for the fuel cell may be dependent upon, for example, the fuel cell technology and the pressure of the substrate feed, and as such could be as wide as from about 50°C to about 1000°C. The preferred operating temperature could be from about 50°C to about 200°C, preferably from about 60 to about 80°C, or from about 55°C to about 70°C, such as for low temperature polymer electrolyte membrane (PEM) fuel cells. The preferred operating temperature could be from about 600°C to about 1000°C, such as for solid oxide fuel cells. The electrolyser may be directly connected to the fuel cell. Alternatively, there may be an intermediate component between the electrolyser and the fuel cell, e.g. a gas cleaner. For some applications, the hydrogen produced by the electrolyser is cleaned, e.g. to remove contaminants such as carbon dioxide or ethanol, before being conveyed to the power generating device. Accordingly, the system may further comprise a gas cleaner between the electrolyser and power generating device. The system may also, or alternatively, comprise a device, or equipment, for raising the pressure of the hydrogen for use by the hydrogen fuel cell. For example, it may be that some hydrogen fuel cells operate preferably with hydrogen at a pressure of 12barG. This may be above the pressure of the product stream from the electrolyser. Advantageously, operating the electrolyser at a higher temperature enables the use of higher pressures, which can improve compatibility with a hydrogen fuel cell (thereby avoiding the need for equipment to increase the pressure of the hydrogen gas produced, or at least reducing the demands on such equipment). In some circumstances, it may be desirable to operate the electrolyser at a pressure above 10 barG (such as to 15 barG). This may be achieved by operating the electrolyser at a temperature above about 160°C (e.g., at about 190°C). Some or all of the electricity produced by the fuel cell may be transmitted to operate the electrolyser. Advantageously, in those embodiments, the electrolyser and fuel cell combination may be self-sufficient. In those embodiments in which all of the electricity produced by the fuel cell is transmitted to the electrolyser, the remaining hydrogen may be conveyed to a tank for transport or storage or conveyed to a separate device for converting the hydrogen to power. In some embodiments, at least a portion of the hydrogen may be conveyed to multiple fuel cells, e.g., a small fuel cell for powering the electrolyser and a larger fuel cell for producing electricity for external applications. The electricity produced by the fuel cell may be used for powering a vehicle, such as a land vehicle (e.g. a car truck or train), ship or aircraft. In some embodiments, the fuel cell may be used for driving the motor of the vehicle. Preferably, the outlet pressure from the electrolyser is higher than the fuel cell inlet pressure. For example, the outlet pressure from the electrolyser may be about 2 to 10 bar higher than the fuel cell inlet pressure. In some embodiments, the apparatus further comprises a hydrogen buffer volume between the electrolyser and fuel cell. The buffer volume is a space in which hydrogen may collect before entering the fuel cell. The size of the buffer volume may be selected depending on the system requirements, e.g., the rate of hydrogen production in the electrolyser versus hydrogen consumption by the fuel cell. For example, a minimal buffer volume may be necessary if the rate of hydrogen product is similar to the rate of hydrogen consumption, while a larger buffer volume (or buffer tank) may be useful if there is a significant different between the rate of hydrogen production versus consumption. The purpose of the buffer volume is to ensure constant flow of hydrogen to the fuel cell. Additionally or alternatively, the electricity produced by the fuel cell may be transmitted to a battery for later use. Accordingly, in some examples, the integrated system comprises the electrolyser in fluid connection with a fuel cell. The integrated system may comprise an energy source for applying a potential to the electrolyser. When the electrolyser is operated in combination with a fuel cell that transmits electricity back to the electrolyser, the energy source may function as a "starter" to initiate operation of the process. In some examples, the integrated system further comprises a battery for storage of the electricity produced by the fuel cell. In some embodiments, the battery is used as the energy source to apply a potential to the electrolyser. Mobile implementations The integrated systems 100 described may be implemented on a vehicle, or floating or fixed platform. Figures 21a-e show various examples of such platforms incorporating the integrated system. The integrated system may be a unit for example, that is secured to, carried, or supported on, a platform including for example any of the following: Figure 21a shows a first example implementation in which the integrated system 100 is carried by a marine vessel (e.g., a ship). Figure 21b shows a second example implementation in which the integrated system 100 is carried by a floating platform (e.g., an offshore rig). Figure 21c shows a third example implementation in which the integrated system 100 is carried by a passenger motor vehicle (e.g., a car, such as a fuel cell electric vehicle). Figure 21 d shows a fourth example implementation in which the integrated system 100 is carried by a larger commercial vehicle (e.g., a truck). Figure 21e shows a fifth example implementation in which the integrated system 100 is carried by a flying vehicle (e.g., an aeroplane). Preferably, the integrated system in these onboard applications comprises both the electrolyser system for carrying out the dehydrogenation process and the hydrogen fuel cell for generating electricity using the hydrogen from the electrolyser system. Preferably, the integrated system further comprises the battery, which may be electrically coupled to the hydrogen fuel cell for charging. In turn, the battery may be used to provide motive power for the vehicle, such as via an electric motor (as per a fuel cell electric vehicle). The battery may also be used to provide power to the electrolyser system for carrying out the electrochemical dehydrogenation process. In other words, the battery may be electrically coupled to a motor and the electrolyser system and configured to provide a portion of the total charge to each. In other implementations, the vehicle or platform may not have a hydrogen fuel cell and instead achieve motive power through, say, combustion of the produced hydrogen. As will be appreciated, moving platforms may encounter a range of environments and temperatures and may have limited access to external power and resources for 5 managing the temperature of the system and in particular that of the co-product, which renders the benefits of the present invention all the more relevant for such applications. The latter consideration may also be true for fixed or floating platforms in remote locations, such as an offshore floating platform (e.g., Figure 21b). Additionally, there may be a further desire for fast and efficient refuelling for these mobile applications, which in the present 10 example may include the unloading (emptying) of accumulated co-product and the loading of a supply of the alcohol-containing substrate chemical to provide the feed stream for the electrolyser system. It will be clear, for example, that the driver of a passenger car is unlikely to want to wait for an accumulation of co-product to be thawed when refuelling, if the ambient temperature happens to have fallen below the freezing point of the co-product. 15 This may be no more desirable from a commercial perspective for a truck, plane or ship. To those skilled in the art to which the invention relates, many changes in construction and widely differing embodiments and applications of the invention will suggest themselves without departing from the scope of the invention as defined in the appended claims. 20          This invention may also be said broadly to consist in the parts, elements and features referred to or indicated in the specification of the application, individually or collectively, and any or all combinations of any two or more of said parts, elements or features, and where specific integers are mentioned herein which have known equivalents in the art to which this invention relates, such known equivalents are deemed to be 25 incorporated herein as if individually set forth.

Claims

1. An integrated system for preparing hydrogen from an alcohol, the integrated system comprising:(a) at least one heat sink including:(i) a feed stream of a substrate liquid comprising an alcohol; and / or(ii) an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream;(b) at least one heat source including a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat;(c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink.

2. The integrated system of claim 1, wherein the heat integration system is arranged to transfer at least a portion of the heat generated by the at least one heat source to the feed stream.

3. The integrated system of claim 1 or claim 2, wherein the heat integration system is arranged to transfer at least a portion of the heat generated by the at least one heat source to the electrolyser system.

4. The integrated system of claim 3, wherein the electrolyser system is configured to operate the electrochemical cell below a thermoneutral voltage, optionally wherein the thermoneutral voltage is about 0.2 volts.

5. The integrated system of claim 3 or claim 4, wherein the electrolyser system is configured to account for the entropic term of the dehydrogenation process, wherein the heat transfer at least assists in accounting for the entropic term.

6. An integrated system for preparing hydrogen from an alcohol, the integrated system comprising:(a) at least one heat sink including a feed stream of a substrate fluid comprising an alcohol;(b) at least one heat source including an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat;(c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink.

7. The integrated system of claim 6, wherein the at least one heat source further includes a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat.

8. The integrated system of claim 6 or claim 7, wherein the electrolyser system is configured to operate the electrochemical cell at a cell voltage at or above a thermoneutral voltage, optionally wherein the thermoneutral voltage is about 0.2 volts.

9. The integrated system of any proceeding claim, wherein the electrolyser system is configured to vapourise the feed stream for the electrochemical cell, wherein the heat transfer at least assists in vapourising the feed stream.

10. The integrated system of any preceding claim, wherein the heat integration system comprises a thermal network for conveying heat via working fluid.

11. The integrated system of claim 10, wherein operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey the heated water stream for heat transfer to one or more of the at least one heat sink, such that the heated water stream provides a working fluid of the thermal network.

12. The integrated system of claim 11 when dependent on claim 6, wherein the heat integration system is configured to convey the co-product stream for heat transfer to one or more of the at least one heat sink, such that the co-product stream provides a working fluid of the thermal network.

13. The integrated system of claim 10, wherein the thermal network is arranged to circulate a working fluid between the at least one heat source and the at least one heat sink.

14. The integrated system of claim 10, where the thermal network comprises:one or more cooling sections for conveying a first working fluid for heat exchange with one or more respective heat sources of the at least one heat source;one or more heating sections for conveying a second working fluid for heat exchange with one or more respective heat sinks of the at least one heat sink;a central unit for heat exchange between the first working fluid and the second working fluid.

15. The integrated system of claim 14, wherein the first working fluid is a heated water stream generated by the hydrogen fuel cell during operation.

16. The integrated system of claim 14 when dependent on claim 6, wherein the first working fluid the co-product stream.

17. The integrated system of any one of claims 14-16, wherein the central unit comprises a heat exchanger for heat transfer from the first working fluid to the second working fluid.

18. The integrated system of any one of claims 10-17, wherein the heat integration system comprises one or more heat exchangers for transferring heat between said working fluid and one or more of the at least one source and / or one or more of the at least one heat sink.

19. The integrated system of any preceding claim, further comprising a temperature control system for controlling:(i) heat transfer, via the heat integration system, from the at least one heat source and / or to the at least one heat sink, and / or(ii) heat production, via the at least one heat source.

20. The integrated system of claim 19, comprising a plurality of heat sinks including the feed stream and the electrolyser system, wherein the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of the plurality of heat sinks.

21. The integrated system of claim 19 or claim 20, wherein the temperature control system is configured to control the heat integration system and / or the at least one heat source such that:(i) the feed stream is substantially maintained above a threshold temperature for vapourisation, and / or(ii) the electrolyser system is substantially maintained at or above a threshold temperature, preferably at a temperature of about 100 degrees Celsius.

22. The integrated system of claim 21, wherein:the alcohol is ethanol and the threshold temperature for vapourisation is about 78 degrees Celsius; orthe alcohol is methanol and the threshold temperature is about 65 degrees Celsius; orthe alcohol is propanol and the threshold temperature is about 97 degrees Celsius;the alcohol is butanol and the threshold temperature is about 118 degrees Celsius;the alcohol is pentanol and the threshold temperature is about 138 degrees Celsius.

23. The integrated system of any one of claims 19 to 22, wherein the temperature control system is configured to control a flow rate and / or distribution of working fluid for the at least one heat source and / or for the at least one heat sink.

24. The integrated system of claim 23, wherein the heat integration system comprises one or more pumps for conveying working fluid and wherein the temperature control system iscommunicatively coupled to the one or more pumps so as to control the flow rate of working fluid.

25. The integrated system of any one of claims 19 to 24 comprising a plurality of heat sinks, wherein the temperature control system is configured adjust a distribution of heat to the plurality of heat sinks via the heat integration system.

26. The integrated system of any one of claims 19 to 25 comprising a plurality of heat sinks, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sinks for heat transfer via the heat integration system.

27. The integrated system of any one of claims 19 to 26 comprising a plurality of heat sources, wherein the temperature control system is configured to adjust a distribution of heat from the plurality of heat sources to the heat integration system.

28. The integrated system of any one of claims 19 to 27 comprising a plurality of heat sources, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sources via the heat integration system.

29. The integrated system of any one of claims 19 to 28, wherein the temperature control system is configured to cause the electrolyser system to adjust the cell voltage of the electrochemical cell to change a thermodynamic voltage.

30. The integrated system of any one of claims 19 to 29, wherein the temperature control system is further configured to:(i) receive information pertaining to one or more of:(a) a temperature of the feed stream;(b) a temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell;(c) a temperature of the ambient environment and / or a forecasted temperature of the ambient environment;(d) a composition of the feed stream;(d) a mass flow of the feed stream and / or a mass flow of working fluid;and(ii) control the heat transfer via the heat integration system and / or heat production via the at least one heat source based on said information.

31. The integrated system of claim 30, further comprising one or more sensors for monitoring, such as by measuring or detecting:(a) the temperature of the feed stream during handling and / or storing by the infrastructure;(b) the temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell;(c) the temperature of the ambient environment;(d) the composition of the feed stream and / or purity of the feed stream with respect to the alcohol and / or the presence or quantity of one or more predetermined substances in the feed stream;(d) the mass flow of the feed stream and / or a mass flow of working fluid;wherein the one or more sensors are communicatively coupled to the temperature control system.

32. The integrated system of claim 30 or claim 31, when dependent on claim 21, wherein the threshold temperature is adjusted based on the information pertaining to the composition of the feed stream.

33. The integrated system of any preceding claim, wherein the alcohol is a C1-5 alcohol, preferably a C1-3 alcohol.

34. The integrated system of claim 33, wherein the alcohol is ethanol, methanol, propanol, butanol, or pentanol and wherein the dehydrogenated product is acetic acid, formic acid, propanoic acid, butyric acid, or pentanoic acid, respectively.

35. The integrated system of any preceding claim, wherein the substrate liquid comprises a mixture of one or more alcohols and water.

36. The integrated system of any preceding claim, wherein the at least one heat sink further includes a battery.

37. The integrated system of any one of claims 1 to 35, wherein the at least one heat source further includes a battery.

38. A vehicle comprising the integrated system of any preceding claim.

39. The vehicle of claim 38, wherein the integrated system comprises a hydrogen fuel cell and a battery configured for electrical connection to the hydrogen fuel cell, wherein the vehicle is configured to be motively powered by the battery.

40. The vehicle of claim 38, configured to be motively powered by the hydrogen produced by the electrolyser system.

41. A floating or fixed platform, or a power station, comprising integrated system of any one of claims 1-37.

42. A method for preparing hydrogen from an alcohol, the method comprising:(a) providing a feed stream of a substrate liquid comprising an alcohol for use in an electrochemical dehydrogenation process;(b) performing an electrochemical dehydrogenation process, by an electrolyser, to partially dehydrogenate the feed stream to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream;(c) performing at least one heat generating process including generating electricity by a hydrogen fuel cell from the hydrogen produced by the electrochemical dehydrogenation process;(d) transferring at least a portion of the heat generated by the at least one heat generating process to the feed stream and / or the electrolyser.

43. A method for preparing hydrogen from an alcohol, the method comprising:(a) providing a feed stream of a substrate liquid comprising an alcohol for use in an electrochemical dehydrogenation process;(b) performing at least one heat generating process including an electrochemical dehydrogenation process, by an electrolyser, to partially dehydrogenate the feed stream to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream, wherein the electrolyser is operated so as to generate heat;(c) transferring at least a portion of the heat generated by the at least one heat generating process to the feed stream.

44. An integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising:at least one heat source, including an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat;at least one heat sink, including an infrastructure for handling and / or storing the coproduct stream;a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure.

45. The integrated system of claim 44, wherein the electrolyser system is configured to operate the electrochemical cell at a cell voltage above a thermoneutral voltage.

46. The integrated system of claim 44 or claim 45, wherein the electrolyser system is configured to operate the electrochemical cell above a cell voltage of about 0.2 volts.

47. An integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising:an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a coproduct stream comprising a dehydrogenated product from a feed stream comprising an alcohol;at least one heat source including a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat;at least one heat sink including an infrastructure for handling and / or storing the coproduct stream;a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink, such that at least a portion of the heat generated by the at least one heat source is transferred to the co-product stream during handling and / or storing by the infrastructure.

48. The integrated system of claim 47, wherein the electrolyser system is configured to operate the electrochemical cell at a cell voltage at or below a thermoneutral voltage.

49. The integrated system of claim 47 or claim 48, wherein the electrolyser system is configured to operate the electrochemical cell at or below a cell voltage of about 0.2 volts.

50. The integrated system of any one of claims 44 to 49, wherein the infrastructure comprises a handling infrastructure for conveying the co-product stream and wherein the heat integration system is configured for heat transfer to the handling infrastructure or to the coproduct stream during handling by the handling infrastructure.

51. The integrated system of any one of claims 44 to 50, wherein the infrastructure comprises a storage infrastructure for storing the co-product stream and wherein the heat integration system is configured for heat transfer to the storage infrastructure or to the coproduct stream during storing by the storage infrastructure.

52. The integrated system of any one of claims 44 to 51, wherein the heat integration system comprises a thermal network for conveying heat via working fluid.

53. The integrated system of claim 52, wherein the thermal network is arranged to circulate a working fluid between the at least one heat source and the at least one heat sink.

54. The integrated system of claim 52, where the thermal network comprises:one or more cooling loops for circulating a first working fluid for heat exchange with one or more respective heat sources of the at least one heat source;one or more heating loops for circulating a second working fluid for heat exchange with one or more respective heat sinks of the at least one heat sink;a central unit for heat exchange between the first working fluid and the second working fluid.

55. The integrated system of claim 54, wherein the central unit comprises a heat exchanger for heat transfer from the first working fluid to the second working fluid.

56. The integrated system of claim 54 or claim 55, wherein the central unit is configured to further cool the first working fluid by removing residual heat.

57. The integrated system of any one of claims 52-56, wherein the heat integration system comprises one or more heat exchangers for transferring heat between said working fluid and one or more of the at least one source and / or one or more of the at least one heat sink.

58. The integrated system of any one of claims 44 to 57, wherein the heat integration system is arranged to extract heat from the co-product stream and / or the product stream of the electrolyser system.

59. The integrated system of any one of claims 44 to 58, when dependent on claims 44-47, wherein the at least one heat source includes a hydrogen fuel cell arranged to generate electricity from the product stream produced by the electrolyser system, wherein operation of the hydrogen fuel cell generates heat.

60. The integrated system of claims 47-49 or claim 59, wherein operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey said heated water stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated water stream provides a working fluid of the thermal network.

61. The integrated system of any one of claims 44-60, wherein the at least one heat source includes a battery, wherein charging and / or discharging of the battery generates heat.

62. The integrated system of claim 61, wherein the battery is electrically coupled to the electrolyser system and / or the hydrogen fuel cell.

63. The integrated system of any one of claims 44 to 62, wherein the at least one heat sink includes a battery.

64. The integrated system of any preceding claim, further comprising a temperature control system for controlling:(i) heat transfer, via the heat integration system, from the at least one heat source and / or to the at least one heat sink, and / or(ii) heat production, via the at least one heat source.

65. The integrated system of claim 64, comprising a plurality of heat sinks, wherein the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a heating demand and / or priority of each of the heat sinks of the plurality of heat sinks.

66. The integrated system of claim 64 or claim 65, wherein the temperature control system is configured to control the heat integration system and / or the at least one heat source such that:(i) the co-product stream is substantially maintained above a threshold minimum temperature during handling and / or storage, and / or(ii) the battery is substantially maintained above a threshold minimum temperature of preferably 0 degrees Celsius, more preferably 20 degrees Celsius, more preferably 30 degrees Celsius, more preferably 35 degrees Celsius.

67. The integrated system of claim 66, wherein the threshold minimum temperature for the co-product stream is the freezing point of the co-product stream, optionally the freezing point of the dehydrogenated alcohol of the co-product stream.

68. The integrated system of claim 67, wherein:the alcohol is ethanol, the organic acid is acetic acid and, optionally, the threshold temperature is about 17 degrees Celsius; orthe alcohol is methanol, the organic acid is formic acid and, optionally, the threshold temperature is about 9 degrees Celsius; orthe alcohol is propanol, the organic acid is propanoic acid and, optionally, the threshold temperature is about -20 degrees Celsius;the alcohol is butanol, the organic acid is butyric acid and, optionally, the threshold temperature is about -7 degrees Celsius;the alcohol is pentanol, the organic acid is pentanoic acid and, optionally, the threshold temperature is about -33 degrees Celsius.

69. The integrated system of any one of claims 64 to 68, wherein the temperature control system is configured to control heat transfer via the heat integration system and / or heat production via the at least one heat source based on a cooling demand and / or priority of each of the heat sources of the plurality of heat sources.

70. The integrated system of any one of claims 64 to 69, wherein the temperature control system is configured to control the heat integration system and / or the at least one heat source such that:(i) the electrolyser system is maintained within a predetermined temperature range during operation, such as below about 200 degrees Celsius, below about 150 degrees Celsius or below, or at, about 100 degrees Celsius.(ii) the hydrogen fuel cell is maintained within a predetermined temperature range during operation, such as from about 70°C to about 200°C, or from about 600°C to about 1000°C.

71. The integrated system of any one of claims 64 to 70, wherein the temperature control system is configured to control a flow rate and / or distribution of working fluid for the at least one heat source and / or for the at least one heat sink.

72. The integrated system of claim 71, wherein the heat integration system comprises one or more pumps for conveying working fluid and wherein the temperature control system is communicatively coupled to the one or more pumps so as to control the flow rate of working fluid.

73. The integrated system of any one of claims 64 to 72 comprising a plurality of heat sinks, wherein the temperature control system is configured adjust a distribution of heat to the plurality of heat sinks via the heat integration system.

74. The integrated system of any one of claims 64 to 73 comprising a plurality of heat sinks, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sinks for heat transfer via the heat integration system.

75. The integrated system of any one of claims 64 to 74 comprising a plurality of heat sources, wherein the temperature control system is configured to adjust a distribution of heat from the plurality of heat sources to the heat integration system.

76. The integrated system of any one of claims 64 to 75 comprising a plurality of heat sources, wherein the temperature control system is configured to dynamically select between, or from among, the plurality of heat sources via the heat integration system.

77. The integrated system of any one of claims 64 to 76, wherein the temperature control system is configured to cause the electrolyser system to adjust the operation of the electrochemical cell such that the electrochemical cell generates more or less heat.

78. The integrated system of any one of claims 64 to 77, wherein the temperature control system is further configured to:(i) receive information pertaining to one or more of:(a) a temperature of the co-product stream during handling and / or storing by the infrastructure;(b) a temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell and / or a temperature of the battery;(c) a temperature of the ambient environment and / or a forecasted temperature of the ambient environment;(d) a composition of the co-product stream;(d) a mass flow of the co-product stream and / or a mass flow of working fluid;and(ii) control the heat transfer via the heat integration system and / or heat production via the at least one heat source based on said information.

79. The integrated system of claim 78, further comprising one or more sensors for monitoring, such as by measuring or detecting:(a) the temperature of the co-product stream during handling and / or storing by the infrastructure;(b) the temperature of the electrolyser system and / or a temperature of the hydrogen fuel cell and / or a temperature of the battery;(c) the temperature of the ambient environment;(d) the composition of the co-product stream and / or purity of the co-product stream with respect to the dehydrogenated alcohol and / or the presence or quantity of one or more predetermined substances in the co-product stream;(d) the mass flow of the co-product stream and / or a mass flow of working fluid;wherein the one or more sensors are communicatively coupled to the temperature control system.

80. The integrated system of claim 78 or claim 79, when dependent on claim 66, wherein the threshold minimum temperature is adjusted based on the information pertaining to the composition of the co-product stream.

81. The integrated system of any one of claims 44 to 80, wherein the alcohol is a C1-5 alcohol, preferably a C1-3 alcohol.

82. The integrated system of claim 81, wherein the alcohol is ethanol, methanol, propanol, butanol, or pentanol and wherein the dehydrogenated product is acetic acid, formic acid, propanoic acid, butyric acid, or pentanoic acid, respectively.

83. An integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising:(i) at least one heat source including:(a) an electrolyser system having an electrochemical cell configured for carrying out a selective partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from a feed stream comprising an alcohol, wherein the electrolyser system is configured to operate the electrochemical cell such that the electrochemical cell generates heat;(b) a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat;(ii) at least one heat sink including a battery; and(iii) a heat integration system configured for heat transfer from the at least one heat source to the at least one heat sink.

84. The integrated system of claim 83, wherein operation of the hydrogen fuel cell generates a heated water stream and wherein the heat integration system is configured to convey said heated water stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated water stream provides a working fluid of the thermal network.

85. The integrated system of claim 83 or claim 84, wherein operation of the electrochemical cell generates a heated co-product stream and wherein the heat integration system is configured to convey said heated co-product stream for heat exchange at one or more of the at least one heat sink or at the central unit, such that the heated co-product stream provides a working fluid of the thermal network.

86. A vehicle comprising the integrated system of any one of claims 44 to 85.

87. The vehicle of claim 86, wherein the integrated system comprises a hydrogen fuel cell and a battery configured for electrical connection to the hydrogen fuel cell, wherein the vehicle is configured to be motively powered by said battery.

88. The vehicle of claim 86, configured to be motively powered by the hydrogen produced by the electrolyser system.

89. A floating or fixed platform, or a power station, comprising integrated system of any one of claims 44-85.

90. A method for preparing a dehydrogenated product from an alcohol, the method comprising:performing at least one heat generating process including an electrochemical process, by an electrolyser, to partially dehydrogenate an alcohol to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product, wherein the electrochemical dehydrogenation process is performed such that the electrolyser generates heat;handling and / or storing the co-product stream via an infrastructure;transferring at least a portion of the heat generated by the at least one heat generating process to at least one heat sink including to the co-product stream during handling and / or storing by the infrastructure.

91. The method of claim 90, comprising performing the electrochemical dehydrogenation process at a cell voltage above a thermoneutral voltage.

92. The method of claim 90 or claim 91, comprising performing the electrochemical dehydrogenation process above a cell voltage of about 0.2 volts.

93. A method for preparing a dehydrogenated product from an alcohol, the method comprising:performing an electrochemical process, by an electrolyser, to partially dehydrogenate an alcohol to produce a product stream comprising hydrogen and a coproduct stream comprising a dehydrogenated product;handling and / or storing the co-product stream via an infrastructure;performing at least one heat generating process including operating a hydrogen fuel cell, wherein the operation of the hydrogen fuel cell generates heat;transferring at least a portion of the heat generated by the at least one heat generating process to at least one heat sink including to the co-product stream during handling and / or storing by the infrastructure.

94. The method of claim 93, comprising operating the electrochemical cell at a potential at or below a thermoneutral voltage.

95. The method of claim 93 or claim 94, comprising operating the electrochemical cell at or below a cell voltage of about 0.2 volts.

96. The method of any one of claims 90 to 95, further comprising draining the co-product stream from a handling infrastructure of the infrastructure when the at least one heat generating process is inactive.

97. The method of any one of claims 90 to 96, comprising transferring the at least a portion of the heat to the co-product stream during handling.

98. The method of any one of claims 90 to 97, comprising transferring the at least a portion of the heat to the co-product stream during storing.

99. An integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising:(a) at least one heat sink including one or more of:(i) a feed stream comprising an alcohol;(ii) an electrolyser system having an electrochemical cell configured for carrying out a partial dehydrogenation process to produce a product stream comprising hydrogen and a co-product stream comprising a dehydrogenated product from the alcohol of the feed stream;(iii) an infrastructure for handling and / or storing the co-product stream;(b) at least one heat source including one or more of:(iv) a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat;(v) the electrolyser system, wherein the electrolyser system is configured to operate the electrochemical cell so as to generate heat;(c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink.

100. An integrated system for preparing a dehydrogenated product from an alcohol, the integrated system comprising:(a) at least one heat sink including one or more of:(i) a feed stream comprising a mixture of an alcohol and water;(ii) an electrolyser system having an electrochemical cell configured for carrying out a partial oxidation process to produce a product stream comprising hydrogen and a coproduct stream comprising a dehydrogenated product from the feed stream;(iii) an infrastructure for handling and / or storing the co-product stream;(b) at least one heat source including one or more of:(iv) a hydrogen fuel cell for generating electricity from the product stream of the electrolyser system, wherein operation of the hydrogen fuel cell generates heat;(v) the electrolyser system, wherein the electrolyser system is configured to operate the electrochemical cell so as to generate heat;(c) a heat integration system for heat transfer from the at least one heat source to the at least one heat sink.

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