Patent Application
20220120199
The invention relates to a device and a method for the utilization of low-temperature heat by decoupling the low-temperature heat from process gas, in particular in the context of hydrogen and/or synthesis gas. The invention further relates to the use of a process engineering component, such that energy utilization can proceed particularly advantageously. In particular, the invention relates to a device and a method according to the preamble of the respective independent or equal-ranking claim.
In the field of process engineering, in particular when interconnecting a plurality of plants or processes, in many cases different temperature levels are needed, in particular in each case a very specific, advantageous temperature level for each respective process. Example: linking of hydrogen and pressure swing adsorption plants. In particular, the temperature differences lie for example in the range from 100° C. to 150° C. If the process gas for the subsequent process has to be provided at a lower temperature level, cooling is required. In particular, cooling for example from a temperature level in the range from 150° C. to 200° C. to a temperature level in the range from 25° C. to 50° C. is desired.
The object of the invention is to provide a device and a method with the above-described features, as a result of which temperature stages in process engineering processes, in particular in the case of series-connected plants, may be elegantly overcome, in particular with regard to energy optimization.
This object is achieved by a device and a method according to the independent claims. Advantageous exemplary embodiments are listed in the subclaims.
This object is achieved according to the invention in particular by a low-temperature heat utilization assembly designed for decoupling low-temperature heat from process gas at temperatures below 200° C. or below 190° C., in particular at process gas temperatures in the range from 150° C. to 170° C., and designed to provide the process gas at a lowered intermediate temperature, in particular in the range from 80° C. to 100° C., specifically 90° C., or at a still further lowered final temperature, in particular in the range from 30° C. to 40° C., specifically 35° C., for at least one subsequent process, wherein in the low-temperature heat utilization assembly the process gas may be fed to a first unit, by means of which the temperature may be lowered to a/the intermediate temperature, wherein the process gas may optionally be provided to at least one heat exchanger stage for further lowering to a/the final temperature; wherein the first unit is an ORC unit for energy transformation of the heat energy into electrical energy, wherein the ORC unit is coupled to at least one electrical consumer unit or to a line for energy export and/or wherein the ORC unit is designed for energy feedback of electrical energy within the low-temperature heat utilization assembly or to a process upstream of the ORC unit. This yields high energy efficiency and may for example also ensure complete energy self-sufficiency for at least one of a number of coupled-together processes, in particular complete energy self-sufficiency of a hydrogen plant.
This low-temperature heat utilization assembly or the corresponding energy conversion process and the energy recovery achievable therewith may for example be implemented in the context of steam reformer plants.
Organic Rankine processes (Organic Rankine Cycles ORC) are used in the most varied process engineering contexts (for example in combined heat and power plants for biogas use), in particular for low-temperature heat utilization. It has now been identified that there might also be interest in utilization of the advantages of ORC for new applications or in new process or plant engineering contexts.
The assembly according to the invention for example enables the implementation of an ORC process in which the energy of the process gas is transferred directly to the working fluid of the ORC process.
The assembly according to the invention in this case for example also enables implementation of an ORC process in which the energy from the process gas is firstly transferred to an intermediate medium, such as for example a thermal oil, before the energy is transferred from the intermediate medium to the working fluid of the ORC process.
Through the coupling according to the invention of the ORC process with at least one plant in which temperature stages need to be overcome, in particular a hydrogen plant or other process technology, an efficient energy utilization concept may be provided for the provision of electrical energy in process plants. Waste heat flows that were previously conventionally dissipated may in this case be comparatively efficiently transformed into electrical energy and utilized. Interlinking of processes (in series and/or in parallel) is thus of greater interest than with previous plant/process concepts.
The invention is in this case also based on the concept of implementing ORC technology to increase energy efficiency or to recover energy. Although it is economic from the point of view of plant engineering to provide just one conventional cooler and optionally also further heat exchangers, for example, between a hydrogen plant and a pressure swing adsorption plant, it has been found that any increased complexity or increased capital expenditure which may be due to the ORC technology can be quickly compensated over the course of operation of the assembly, for example within a year. In other words, the cost savings resulting from energy savings may cancel out higher capital investment for example within as little as a few months or years, depending on the respective applicable energy price levels.
An appropriate level for the intermediate temperature may in this case in particular be/have been defined as a function of the evaporation temperature of the working fluid, by way of example approx. 80° C. in the case of pentane for example (depending on specified pressure level). An advantageous process gas temperature then amounts for example to 90° C. or 85° C. 80° C., for example, may be stated as the lower limit for the process gas temperature.
An appropriate level for the final temperature, if a two-stage process is to be implemented, may in this case be/have been defined in particular as a function of the type of process arranged downstream of the low-temperature heat utilization assembly, for example in the case of pressure swing adsorption approx. 35° C. to 40° C.
The ORC unit may in this case automatically adjust itself, depending on available heat flow. An integrated closed-loop control concept specific to the ORC unit is not necessarily required. Instead, any closed-loop control-related problems in the context of the present invention may be focused on the feed-in or feedback of the obtained electrical energy.
It has been found that sufficient residual heat may advantageously also be provided in the case of an emergency shutdown, in order to operate boiler feedwater pumps, for example. Thus, dry running of evaporators may be prevented even in the case of an operating failure. In other words, the assembly according to the invention is also comparatively robust and may protect heat exchanger units from disadvantageous operating situations.
According to one exemplary embodiment, the low-temperature heat utilization assembly has a second unit with the at least one heat exchanger stage downstream of the ORC unit, by means of which second unit the temperature of the process gas may be lowered from a/the intermediate temperature to the final temperature. In this way, the concept according to the invention may be appropriately implemented in particular also in the context of pressure swing adsorption plants, namely between a first plant upstream (temperature level for example 150° C. to 200° C.) and a second plant downstream (desired inlet temperature level for example 25° C. to 50° C.).
According to one exemplary embodiment, the low-temperature heat utilization assembly is designed for decoupling of a heat energy flow in the range from 15 MW to 40 MW, in particular 2.5 MW to 55 MW. In this way, a quantity of electrical energy may also be provided which enables a high degree of process self-sufficiency, in particular in the context of hydrogen plants or steam reformer plants.
According to one exemplary embodiment, the low-temperature heat utilization assembly is designed to transform heat energy into electrical energy in a range from 1.5 MW to 4.0 MW, in particular 0.25 MW to 5.5 MW, in particular with a transformation factor in the range from 10% or 0.1, specifically in the range of 10%±5% positive/negative deviation. In this way, a hydrogen plant may in particular be autonomous from an energy standpoint, namely supplied with power solely by the energy recovered from the ORC process.
The thermodynamically maximum possible effective Carnot efficiency may be stated as around 20%. Accordingly, even a level of efficiency in the range of 10% may be described as good and advantageous.
For example, heat energy flows of 2.5 to 40 MW may be used in the configuration according to the invention, whereas hitherto these were in many cases output or dissipated to the surrounding environment wholly unused.
A heat energy flow of 30 MW is for example utilized at an efficiency of 10%, such that 3 MW of electrical power may be provided. The inherent requirement of a hydrogen plant is for example 1.5 MW, such that, in addition to supply of the hydrogen plant, some of the electrical energy may be fed back or exported (combination of a plurality of uses for the electrical energy generated from waste heat).
According to one exemplary embodiment, the low-temperature heat utilization assembly has at least one energy coupling or line by means of which the ORC unit is coupled to further consumers and/or by means of which the low-temperature heat utilization assembly is designed for energy feedback within the low-temperature heat utilization assembly or to a plant upstream of the low-temperature heat utilization assembly. In this way, energy utilization can be further differentiated depending on the field of application.
According to one exemplary embodiment, the low-temperature heat utilization assembly is arranged downstream of a hydrogen plant or synthesis gas plant, wherein the process gas is provided from the hydrogen plant or synthesis gas plant. In this way, an advantageous amount of low-caloric heat may be provided and transformed for the ORC process.
According to one exemplary embodiment, the low-temperature heat utilization assembly is arranged upstream of a pressure swing adsorption plant, wherein the process gas is provided from the low-temperature heat utilization assembly to the pressure swing adsorption plant. In this way, at least two processes may advantageously be interlinked energy-wise, in particular with a hydrogen plant as first process upstream of the low-temperature heat utilization assembly.
According to one exemplary embodiment, the low-temperature heat utilization assembly has an open-/closed-loop control device which is designed for open-/closed-loop control of flows of electrical energy from the ORC process internally in the low-temperature heat utilization assembly or externally. In this way, application-specific energy distribution is closed-loop-controllable in a particularly appropriate manner, in particular also, depending on the situation, as a function of the instantaneous energy requirement of individual consumers. Alternatively, all the recovered electrical energy may be provided to the process upstream of the low-temperature heat utilization assembly.
The above-described object is in particular also achieved according to the invention by a method for utilization of low-temperature heat by decoupling the low-temperature heat from process gas at temperatures of below 200° C. or below 190° C., in particular at process gas temperatures in the range from 150° C. to 170° C., wherein the process gas is provided at a lowered intermediate temperature, in particular in the range from 65° C. to 90° C., or at a still further lowered final temperature, in particular in the range of 35° C., for at least one subsequent process, wherein the process gas is fed to a first unit, by means of which the temperature is lowered to a/the intermediate temperature, wherein the process gas is optionally provided to at least one heat exchanger stage for further lowering to a/the final temperature; wherein at least one ORC process, which is performed in the first unit for decoupling the low-temperature heat and for providing electrical energy obtained from the low-temperature heat, wherein the electrical energy obtained in the ORC process is fed or exported to at least one electrical consumer unit coupled to the ORC process and/or wherein the electrical energy obtained in the ORC process is fed back within the low-temperature heat utilization process or to a process upstream of the ORC process. This yields the above-stated advantages, in particular an advantageous degree of energy- or process-related self-sufficiency.
Alternatively, all the energy provided by the ORC process, or part thereof, may be exported, i.e. decoupled from the low-temperature heat utilization assembly. The inherent energy requirement of the low-temperature heat utilization assembly may in this case optionally also be covered at least in part by energy imports. In this way, an ideal compromise between coverage of inherent requirements and energy supply to third parties may also be achieved, depending on energy availability.
According to one embodiment, the low-temperature heat is decoupled from the process gas to a/the intermediate temperature, in particular to a temperature of 90° C., wherein the process gas is lowered in a second unit in at least one heat exchange stage to a/the final temperature, in particular to 35° C., in particular to provide the process gas for pressure swing adsorption. This also promotes interconnection with a process downstream of the low-temperature heat utilization assembly, in particular with a pressure swing adsorption plant.
According to one embodiment, a heat energy flow in the range from 15 MW to 40 MW, in particular 2.5 MW to 55 MW is decoupled by the ORC process and transformed into electrical energy, in particular with an energy transformation factor in the range of 10%. According to one embodiment, the ORC process brings about the transformation of heat energy into electrical energy such that electrical energy in a range from 1.5 MW to 4.0 MW, in particular 0.25 MW to 5.5 MW may be provided, in particular with an energy transformation factor in the range of 10% or 0.1. This in each case yields energy of such magnitude that process self-sufficiency can be ensured, with advantageous effects, in particular in the context of steam reformer plants.
The above-described object is also achieved according to the invention by use of at least one ORC unit in a low-temperature heat utilization assembly to decouple heat energy from process gas of a plant, in particular a hydrogen plant or synthesis gas plant, and to provide electrical energy generated from the heat energy to at least one electrical consumer unit and/or to at least partially export the energy and optionally also to feed back (into the process) electrical energy generated from the heat energy into the plant, in particular hydrogen plant or synthesis gas plant, in particular in a previously described low-temperature heat utilization assembly, in particular downstream of a hydrogen plant for energy self-sufficient operation of the hydrogen plant, wherein the ORC unit is used instead of or as a replacement for dissipative cooling devices. Air coolers can be dispensed with, for example. Depending on the situation, distribution of the recovered energy may optionally proceed to suit the energy requirements of the individual consumer units. In particular, energy coupling of at least one first process is ensured, for which heat energy is recovered at the interface to at least one second process and provided as electrical energy.
It has been found that in particular a hydrogen plant may be operated self-sufficiently with regard to energy thanks to the implementation of ORC technology. In other words, all electrical consumer units provided and installed in the hydrogen plant may be supplied by the electrical energy generated using the ORC technology. In this case, implementation of the ORC technology may also be so efficient that excess electrical energy arises, which may be exported from the process. The assembly according to the invention therefore enables a high degree of self-sufficiency and may enable the implementation of plants and processes even when no external power grid is present at all, or an external power grid is unreliable or would lead to high costs. For a start-up process, energy inflow from outside may optionally be provided.
The above-described object is also achieved according to the invention by use of at least one ORC unit in a low-temperature heat utilization assembly to decouple heat energy from the process gas of a hydrogen plant or synthesis gas plant and to provide electrical energy generated from the heat energy in the hydrogen plant or synthesis gas plant for energy-wise self-sufficient operation of the hydrogen plant or synthesis gas plant, in particular in an above-described low-temperature heat utilization assembly. This results, especially in the context of hydrogen plants, in a very advantageous degree of energy self-sufficiency. Stand-alone operation is possible, for example, i.e. operation without external power supply.
Further features and advantages of the invention are revealed by the description of at least one exemplary embodiment with reference to drawings, and by the drawings themselves, in which
In the case of reference signs which are not explicitly described in relation to an individual figure, reference is made to the other figures.
Process gas M1 is supplied to a cooler 1 at temperatures of below 170° C. to 190° C., in particular in the range from 150° C. to 170° C., in order to be able to provide the process gas downstream thereof as process gas M11 at a temperature level of for example 65° C. (intermediate temperature). In this case, heat flow is output E1 to the surrounding environment (loss of low-temperature heat), in particular a heat energy loss occurs in the range from 15 MW to 40 MW, in particular 2.5 MW to 55 MW, depending on the plant or the process. Downstream of a heat exchanger stage 2 the process gas M12 is present at a temperature level of for example 35° C. (final temperature) and may be put to further use, for example in a pressure swing adsorption plant or in a synthesis gas compressor. For pressure swing adsorption plants in particular, an advantageous final temperature at the inlet of the plant is in the range from 35° C. to 40° C.
The process gas M1 originates for example from a plant 3 upstream of the energy conversion, in particular from a hydrogen plant. The process gas M12 is fed for example to a plant 4 downstream of the energy conversion, in particular a pressure swing adsorption plant.
Low-temperature heat (low caloric heat) is used in an ORC process 10 or in a corresponding unit, in particular such that the process gas M21 is cooled down downstream thereof to approx. 90° C. (intermediate temperature). This temperature downstream of the ORC process is defined for example as a function of the type and pressure of a used working fluid. The intermediate temperature is as low as possible, but for many applications is advantageously above 80° C.
Downstream of the heat exchanger stage 2, the forwarded process gas M22 may be present in particular at approx. 35° C., as also in the example of
The heat energy utilization E2 achievable with the implemented ORC process 10 proceeds in particular by conversion/transformation of the heat energy into electrical energy, in particular for the provision of at least 1.5 MW to 4.0 MW (or 0.25 MW to 5.5 MW) electrical energy from 15 MW to 40 MW (or 2.5 MW to 55 MW) heat energy, in particular with a transformation factor in the range from 10% or 0.1.
The energy flow E2 may be provided for the individual plant/process engineering components or consumer units 12 involved, in particular for a hydrogen plant, and/or the generated electrical energy may be exported from the process described here out to separate external processes/plants or into a power grid independent of the present ORC process. To this end, an energy coupling 11, in particular line may be provided, which connects the ORC unit 10 with the further plant engineering components or processes (in particular within the plant or externally to further consumers).
The process gas M1 originates for example from a plant 3 upstream of the energy conversion, in particular from a hydrogen plant. The process gas M22 is for example fed to a plant 4 downstream of the energy conversion, in particular a pressure swing adsorption plant.
Thanks to the ORC implementation according to the invention, a high degree of self-sufficiency may be ensured. In particular, the present process is independent of an external power supply, and is thus also resistant to mains power variance and unstable power grids. In particular, this may also be very useful at locations with poor infrastructure, or may indeed enable use for the first time of the technology described herein.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10 2019 207 957.1 | May 2019 | DE | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2020/063321 | 5/13/2020 | WO | 00 |
