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    • 专利摘要:
    In a process for regasifying cryogenic liquefied gas, such as e.g. Methane or air, in which a subset of the in a tank (1) located cryogenic liquefied gas from the tank (1) via a pressure lock an evaporator (17) is fed, in which evaporates the subset, whereupon the vaporized gas in a high-pressure gas storage (39 ), is fed into a pipeline network or fed to an energy converter for generating electrical energy, the pressure lock comprises two chambers (27,28) which are alternately filled with a subset of the cryogenic liquefied gas from the tank (1), wherein the with Subset filled chamber (27,28) after the respective filling of the tank (1) separated and connected to the evaporator (17), whereupon a pressure equalization between the evaporator (17) and the chamber connected thereto (27,28) established. Subsequently, at least one displacement body (21, 22) is displaced in such a way that the gas contained in the chamber (27, 28) which is under evaporator pressure is at least partially displaced into the evaporator (17).
    公开号:AT518299A1
    申请号:T8002/2017
    申请日:2016-02-18
    公开日:2017-09-15
    发明作者:
    申请人:Sasu Energiesysteme Gmbh；
    IPC主号:
    专利说明:

    The invention relates to a process for regasifying cryogenic liquefied gas, e.g. Methane or air, in which a subset of located in a tank cryogenic liquefied gas is supplied from the tank via a pressure lock an evaporator in which evaporates the subset, whereupon the vaporized gas filled into a high-pressure gas storage, fed into a pipeline network or an energy converter for generating electrical energy is supplied.
    The invention further relates to a device for carrying out this method.
    Refrigerated liquefied gases are becoming increasingly important. They are transported and stored at low pressure. The use usually requires the transfer from the liquid state to the gas phase. For further use in the high pressure range, the product is stored at the point of use in low pressure tanks (e.g., at most 37 bar) and then regasified the cryogenic liquefied gas. For this purpose, it is spent in evaporators in which the evaporation takes place with the supply of energy. The high-pressure phase previously required high-pressure pumps for cryogenic liquids, which push the liquids into the evaporator. The pump supplies the compression and evaporation energy with the evaporator.
    Alternatively, the compression can be done with a compressor. For this purpose, the liquid is transferred before compression in the evaporator with tank pressure in the gas phase and then compressed with the compressor.
    Both methods are energy-intensive processes that require high-maintenance, high-cost machines. So far, this application has been limited to a few facilities that are economically insignificant in their entirety. With increased market penetration of natural gas refueling (this has so far been done with conventional compressors), new gas supply solutions have to be found. In compressors, the compression energy must be supplied entirely through the mains and the supplying gas lines must have the required yield. Both are only conditionally available.
    The alternative is LNG, cryogenic liquefied natural gas. The liquefied gas is transported to the end user or gas station with special insulated tank trucks. There it is stored in special tanks and must be regasified and compressed. So far, this requirement can be met in the high pressure range only with known high-pressure piston pumps. The piston pump has the significant disadvantage that it has wear phenomena after a relatively short time, which gas slippage occurs, which is ecologically and safety extremely dangerous for example in methane and high maintenance costs are planned. In addition, the driving engine requires external energy (electricity).
    The documents WO 2007/128023 A1 and WO 2013/182907 A2 describe processes for the regasification of cryogenic liquefied gases, which enable the process to be continued by relieving or throttling into the storage tank. Both methods require no current for compression. The necessary re-liquefaction, but only a very small part of the regasified product is, as mentioned, solved by pressure relief or throttling.
    In the known processes for regasifying cryogenic liquefied gas, the liquid phase of the liquified liquefied gas is stored in an insulated tank. For this it must be brought to the evaporation in the high-pressure part, so that, depending on the amount of the liquid product supplied, the volume of the evaporation space and the corresponding energy supply, the gas pressure is adjusted. The tank has a much lower pressure than the evaporator, which prevails in the high pressure. Both systems must therefore be connected to each other via a so-called pressure lock. As pressure lock was used in the method according to the writings WO 2007/128023 Al and WO 2013/182907 A2 a Dosierspeicher.
    A disadvantage of the methods mentioned is that a relatively high proportion of energy must be used for the required re-liquefaction of a portion of the regasified product.
    The present invention therefore seeks to provide a method and apparatus for regasifying cryogenic liquefied gases which requires a smaller amount of product to be re-liquefied and / or which can reduce the energy required for re-liquefaction.
    To achieve this object, the invention according to a first aspect in a method of the aforementioned
    Kind essentially in that the pressure lock comprises two chambers which are alternately filled with a subset of the cryogenic liquefied gas from the tank, wherein the filled with the subset chamber is separated after the respective filling of the tank and connected to the evaporator, whereupon a pressure equalization between the evaporator and the chamber associated with this adjusts, and then at least one displacer is displaced so that the gas contained in the chamber located under evaporator pressure at least partially, preferably completely, displaced in the evaporator and the other chamber with a subset of the cryogenic liquefied gas is filled from the tank. Characterized in that at least one displacement body is provided, the remaining after the pressure equalization with the evaporator in the respective chamber amount of the regasified product is pressed into the memory. Due to the fact that, when displacing the displacement body, the amount of the regasified product remaining in one chamber is squeezed out and at the same time new liquid product is filled from the tank in the other chamber, a simple and reliable process management can be ensured. In this case, the displacement body can be guided displaceably in a cylinder, wherein the displacement body divides the cylinder into the two chambers, so that both chambers are realized in the same cylinder. Alternatively, the first and the second chamber may each be formed in a separate cylinder, in each of which an associated displacement body is displaceably guided. A preferred embodiment provides in this context that each chamber is associated with its own displacement body, wherein the displacement body for simultaneous
    Displacing the gas from one chamber into the evaporator and filling the other chamber with cryogenic liquefied gas are synchronously moved out of the tank.
    A preferred embodiment provides that the two chambers are alternately connected to the tank and to the evaporator. This means that the first chamber is connected to the tank and filled with liquid product from the tank and then separated from the tank and connected to the evaporator. After pressure equalization with the evaporator, the amount of gas or liquid left in the chamber is squeezed out and the process can start from the beginning, i. the chamber can be refilled with liquid product from the tank. The other chamber is also connected in an analogous manner alternately with the tank and the evaporator, but the individual steps are carried out offset in time to the other chamber.
    A particularly economical process management is made possible if the liquefied gas is preferably brought from the chamber into the evaporator under the geodetic pressure. Alternatively, the required pressure difference can also be applied or supported by a circulation pump. The filling of the chamber advantageously comprises the production of a pressure equalization between the tank and the chamber. In order to allow filling of the chamber under the geodetic pressure of the tank, it is preferably provided that the liquid feed is arranged in the chamber lower than the liquid outlet from the tank.
    The transfer of the gas from the chamber into the evaporator preferably takes place via a heat exchanger, in which heat is supplied to the liquid gas. In this case, the required heat, or a part thereof, can be withdrawn from a gas stream to be liquefied in order to allow it to be condensed and returned to the tank.
    A particularly energy-efficient process management is ensured if, as corresponds to a preferred embodiment, the pressure after the pressure equalization between the evaporator and the associated chamber is in the supercritical range.
    The displacement of the displacement body or bodies can in principle be carried out with any drives, such as e.g. with an electric drive. Advantageously, the drive is hydraulically or pneumatically, in particular by means of a fluid pressure generated by the process itself. In this case, the procedure is preferably such that the displacement of the displacement body or bodies takes place by applying gas pressure, in particular with gas pressure from a high-pressure gas reservoir fed by the evaporator.
    The pneumatic actuation takes place here preferably via a separate piston. A preferred procedure in this context provides that an actuating piston is slidably mounted in an actuating cylinder and for synchronous movement with the or the displacement body (s) and the displacement of the or the displacement body by unilaterally acting on the actuating piston with the preferably generated in the system Gas pressure occurs after or at the time of the
    Actuation of opposite side of the actuating piston a pressure release takes place (is). The gas pressure necessary for the displacement is preferably stored in a separate memory and, if necessary, filled from the system or retrieved into the system.
    The pressure release is preferably carried out in that the gas located at the opposite side of the actuating piston is preferably cooled to condensation and then relaxed and is recirculated during the expansion in the tank as a liquid and liquid / gas phase or only as a gas phase.
    A particularly energy-efficient procedure for liquefying the gas in connection with the pressure release provides that the gas is passed through the heat exchanger for its cooling and condensation and is cooled in heat exchange with the liquid fed into the evaporator from the chamber, the condensation in the heat exchanger being preferred to a point in the T, s diagram that is to the left of the critical point. It is advantageous if the pressure remains constant.
    The inventive method for regasifying cryogenic liquefied gas can be used according to a second aspect of the invention in a method for demand-dependent control and delivery of the electrical output of a regenerative energy powered energy converter, in particular electric generator. In regenerative energy powered energy converters, such as e.g. In the case of energy converters driven by wind energy, solar energy or tidal energy, the problem is that the respective conditions depend on external conditions
    Generation of electrical energy can not be easily reconciled with the respective needs. Thus, for example, the energy production in solar installations relies on sunlight, with a first peak of energy consumption usually occurring when electric lighting fixtures are switched on after sunset. For energy sources that are not readily predictable in their performance, and especially for the use of wind energy, these drawbacks become particularly clear when using regenerative energy sources.
    For the purpose of equalization or smoothing of the electrical output power of such powered with regenerative energy energy converter has already been proposed to store the energy required in times of lower demand accordingly. The energy can e.g. be stored in the form of a liquefied gas, as described in AT 506779 B. For this purpose, the electrical energy supplied by the energy converter is used to liquefy a gas. The gas is stored in liquefied form and can be regasified with comparatively simple facilities as needed, and the energy released by the increase in volume during regasification can again be converted into electrical energy in a simple and conventional manner and made available to electrical consumers. The method is preferably suitable for the use of air or constituents thereof, e.g. Nitrogen, or other gases, e.g. Methane, as a storage medium.
    However, the achieved efficiency of the process described in AT 506779 B has proven to be unsatisfactory. In addition, in the case of the method described in AT 506779 B and in other similar methods, it is assumed that at the moment of air liquefaction, electricity is available in such a way that the operation of the air liquefier or air decomposer can take place at the optimum point. This seems unrealistic.
    Considering the calculation of efficiency more accurately, one always proceeds from the erroneously applied ratio of stored current to current fed into the grid instead of calculating the realistic ratio of current generated at the wind turbine / photovoltaic panel to the current fed into the grid. A storage by way of liquefaction is only useful if an electrical efficiency is achieved, which is well over 50%. For this purpose, except the pumped storage plant and their modifications so far no known solutions. The pumped storage power plant has the disadvantage that it is bound to exact geological conditions that are limited.
    With the invention, therefore, a method for storage and demand-dependent delivery of electrical energy generated by a regenerative energy converter energy to be created, which is characterized by a higher efficiency.
    To achieve this object, the invention according to a second aspect, a method for demand-dependent control and delivery of the electrical output of a regenerative energy energy converter, in particular electrical generator, before, wherein a gas, in particular air, is liquefied in a device coupled to the energy converter in that liquefied gas is preferably stored without pressure in a tank and the liquefied gas is regasified as needed and energy released from the gas is converted into electrical energy and made available to electrical consumers, wherein the conversion of the released energy into electrical energy comprises the steps of: driving a pressure-increasing device by means of the pressure of the regasified gas,
    Using the pressure increasing device to compress a liquid medium, such as water, and press it into a turbine,
    Driving an electric generator with the help of the turbine to obtain electrical energy.
    The invention further provides a method for utilizing energy stored in cryogenic liquefied gas, wherein the liquefied gas stored in a tank is regasified, and energy released from the regasified gas is converted into electrical energy and made available to electrical consumers, wherein the conversion the released energy into electrical energy comprises the following steps:
    Driving a pressure-increasing device by means of the pressure of the regasified gas,
    Using the pressure increasing device to compress a liquid medium, such as water, and press it into a turbine,
    Driving an electric generator with the help of the turbine to obtain electrical energy.
    The regasification of the liquefied gas can be carried out in a particularly advantageous manner with a method according to the first aspect of the invention.
    The gas pressure resulting from regasification, e.g. > 200 bar, if necessary it is expanded by a turbine. However, unlike the AT 506779 B, there is no direct relaxation, but an indirect use of the energy released from the gas. With the gas pressure, a pressure-increasing device, e.g. a piston driven instead of gas, a liquid medium, such as water in an expansion machine, such as. a turbine, presses. The expansion machine is coupled to a generator so that power is generated as needed.
    The liquid medium, for example water, is preferably expanded to atmospheric pressure by the expansion machine, wherein a preferred embodiment of the method provides that the liquid medium, for example water, expanded in the expansion machine is returned to the pressure-increasing device. The recirculated liquid medium is then recompressed in the pressure-increasing device. The liquid medium is thus circulated.
    For driving the pressure-increasing device, the regasified, high-pressure gas is preferably a driving chamber, such as e.g. a drive cylinder of the pressure-increasing device, wherein the gas located in the drive chamber preferably drives a piston which drives or acts on a pressure medium acting on the liquid medium pressure increasing means. The pressure increasing means may in turn comprise a piston of a piston pump.
    The pressure increasing device thus preferably has a drive element acted upon by the high pressure gas, such as e.g. a piston, and pressurizing means acting on the liquid medium, the urging member driving the pressure increasing means.
    After the outlet of the high-pressure gas from the pressure-increasing device, the gas is preferably passed through a heat exchanger. At the outlet, a residual pressure of the gas is preferably retained here, which lies to the left of the critical point in the Ts diagram. In the heat exchanger, the gas is preferably cooled at a constant pressure (preferably to the left of the critical point in the Ts diagram), so that a part of the gas is liquefied.
    Furthermore, it is advantageous if the cooled in the heat exchanger gas is expanded via a throttle point in the tank. The gas is liquefied using the Joule-Thomsen effect in the tank and is the regasification process again.
    The method according to the second aspect of the invention 'makes it possible to decouple the network requirements of the direct generation on the wind turbine or the photovoltaic system or the like and to supply the network exclusively from the liquid gas storage. Is the power on regenerative energy powered energy converters, e.g. on the wind turbine too low, the condenser is operated in stand-by mode. If the power generated at the energy converter rises above the possible
    Efficiency, the condenser is switched on. The prerequisite for this is that the efficiency allows power generation that exceeds the losses.
    Furthermore, the process of harnessing energy stored in cryogenic liquefied gas allows inexpensive storage of the energy in the form of liquefied gas and on-demand conversion of the energy stored therein into electrical energy.
    The liquid gas can be used, for example, to generate electricity in a motor vehicle. In the vehicle there is a vacuum-insulated low-pressure tank, in which the liquid is fueled. If necessary, the liquid can be regasified and energy converted into electrical energy.
    The vehicle drives as usual with a battery that can be small but powerful. The battery is used to map the driving cycle. When the voltage and current in the battery have dropped to a lower limit, power generation will start based on the liquefied gas and charge the battery while driving or while standing. An otherwise stationary charging of the battery is no longer necessary since the charging process takes place while driving. As "exhaust" air is released.
    According to a third aspect, the invention relates to a device for regasifying cryogenic liquefied gas, comprising a tank for the cryogenic liquefied gas, an evaporator and a pressure lock arranged between the tank and the evaporator, which is characterized in that the pressure lock comprises two chambers, which are alternately filled with a subset of the cryogenic liquefied gas from the tank and which are separable after the respective filling of the tank and connectable to the evaporator, and that at least one displacement body is provided, which contained for displacing the chamber located under the evaporator pressure Gas is arranged in the evaporator.
    A preferred embodiment (FIG. 1) provides that the at least one displacement body is designed as a displacer piston displaceably mounted in a cylinder.
    A further preferred embodiment provides that the two chambers are connected via shut-off devices respectively to the tank and to the evaporator, so that they can be connected alternately to the tank and to the evaporator.
    Advantageously, each chamber has its own displacement body, wherein the displacement body of both chambers are coupled to synchronous motion with each other inextricably.
    Preferably, the displacer formed in particular as displaceably mounted in a respective cylinder displacement piston is coupled to a displaceably mounted in an actuating cylinder actuating piston to synchronous movement.
    For actuating the actuating piston, an advantageous embodiment provides that at least one line which can be acted upon by gas pressure opens into the actuating cylinder, so that the displacement of the displacement body or bodies takes place by applying the actuating piston to the gas pressure on one side.
    In particular, two are provided on both sides of the actuating piston in the actuating cylinder, each acted upon by the gas pressure lines.
    According to a preferred embodiment, it is provided that the line connecting a chamber and the evaporator in each case leads via a heat exchanger.
    In order to keep the fluid in the tank and in the pressure lock in the liquid state, it is preferably provided that the tank and the chambers of the pressure lock are thermally insulated.
    Furthermore, the volume of the chambers is preferably in each case smaller than the volume of the evaporator.
    According to a fourth aspect, the invention relates to a device for utilization of stored in cryogenic liquefied gas potential energy, in particular for carrying out the method according to the second aspect of the invention, comprising a tank for storing the liquefied gas, connected to the tank Regasifizierungsseinrichtung for regasifying the liquefied gas, an energy converter for converting the energy released by the regasification into electrical energy, wherein the electrical energy supplied by the energy converter is provided to electrical consumers, the energy converter comprising a pressure booster which is drivable with the pressure of the regasified gas, wherein the Pressure increasing device is arranged to compress a pressure medium, for example, supplied to the pressure increasing device, for example, water, wherein the energy converter further an expansion machine, in particular Tu rbine, with which the pressure increasing device is connected to supply the expansion machine, the compressed liquid medium, and wherein the energy converter further comprises an electric generator which is drivable by the expansion machine.
    Preferably, the pressure-increasing device is designed as a pump, in particular a piston pump.
    The expansion machine is preferably connected to the pressure-increasing device via a return line in order to preferably recirculate the pressure-increasing device, which is expanded in the expansion machine, back through the inlet via the geodetic height.
    Preferably, the drive side is the
    Pressure-increasing device connected to a heat exchanger to guide the gas leaving a drive chamber of the pressure-increasing device through the heat exchanger.
    Preferably, the heat exchanger is connected via a throttle point to the tank to supply the cooled in the heat exchanger gas to the tank.
    Particularly preferably, the regasification device is designed according to the third aspect of the invention.
    The above-described device for utilization of energy stored in liquefied gas can be used particularly advantageously in the following context, namely in a device for demand-dependent regulation and delivery of the electrical output of a regenerative energy converter, in particular an electric generator comprising one with the energy converter coupled gas liquefaction device, a tank for storing the liquefied gas and the device for converting the energy stored in the cryogenic liquefied gas into electrical energy.
    The invention will be explained in more detail with reference to an embodiment schematically illustrated in the drawing. 1 shows a block diagram of a regasification system for the purpose of pressure storage and FIG. 2 shows a block diagram of a system for demand-dependent regulation and delivery of the electrical output of a regenerative energy-operated energy converter.
    The plant according to Fig. 1 comprises a vacuum-insulated tank 1 in which cryogenic liquefied gas, e.g. Methane or other cryogenic liquefied gas is stored. The tank 1 is connected via a line 2 and shut-off valves 3 and 4 optionally to the inlet 5 of the cylinder 6 or the inlet 7 of the cylinder 8. The cylinders 6 and 8 are thermally insulated, in particular vacuum-insulated. The gas return 9 of the cylinder 6 and the gas return 10 of the cylinder 8 are each connected via a shut-off device 11 and 12 with the gas space of the tank 1. The inlet 5 of the cylinder 6 and the inlet 7 of the cylinder 8 are each connected via a shut-off device 13 and 14, a line 15 and a heat exchanger 16 with an evaporator 17. The gas return 9 of the cylinder 6 and the gas return 10 of the cylinder 8 are also connected via a shut-off device 18 and 19 and a line 20 also connected to the evaporator 17.
    In the cylinder 6, a displacement piston 21 is slidably mounted and in the cylinder 8, a displacement piston 22 is slidably mounted. The two pistons 21,22 are connected to each other by means of a rigid connection on the rod 23 and thus mounted together displaceable. The outer chambers 25 and 26 of the cylinder 6 and 8 are constantly connected to each other in operation, which takes place for example by means of an axial pressure compensation bore 24. The inner chambers 27 and 28 of the cylinders 6 and 8 are those chambers of the cylinders 6 and 8, which can be filled via the inlet 5 and 7 with fluid from the tank 1.
    For actuating the displacement piston 21 and 22 in the direction of the double arrow 30, an actuating piston 40 is displaceably guided in a cylinder 29 and rigidly connected to the rod 23. The cylinder has at its opposite ends via inlets and outlets 30 and 31, via which pressure medium can be supplied on one side, while on the other side a pressure relief is made. For supply of pressure medium, the inlets and outlets 30 and 31 are connected via shut-off valves 32 and 33 to a pressure accumulator 34. For pressure relief, the inlets and outlets 30 and 31 via shut-off valves 35 and 36, a line 37 and the heat exchanger 16 are connected to the gas space of the tank 1.
    To the evaporator, a gas cylinder 39 is connected via a shut-off device 38, which are filled with the medium regasified in the evaporator 17 and can then be removed. The pressure vessel 34 may also be fed by the evaporator 17.
    The operation of the regasification plant shown in FIG. 1 is now as follows. From the vacuum-insulated tank 1 flows through the geodesic pressure alone, the liquefied gas into the chamber 27. For this purpose, the obturator 3 is opened and made by opening the obturator 11, a connection to the gas space of the tank 1 (gas decrease). If the chamber 27 is filled and the possibly resulting gas has flowed out of the chamber 27 into the tank 1, the chamber 27 is separated from the tank 1 by closing the shut-off elements 3 and 11. Now the connection to the evaporator 17 is established by opening the obturator 13. Again, by opening the obturator 18, a gas return from the evaporator outlet via the line 20 to the gas return 9 of the chamber 27, which produces a pressure equalization and allows the rapid emptying of the chamber 27 by the geodesic pressure.
    Between chamber 27 and evaporator 17, a heat exchanger 16 is interposed in series. The product flows through the geodesic pressure from the chamber 27 first in the heat exchanger 16 upstream of the evaporator 17. This is below the chamber 27, but above the evaporator 17. Therefore, the liquid flows only through the geodetic pressure in the heat exchanger 16 and fills it , Excess product flows through this into the underlying evaporator 17. There it comes to a sudden evaporation, so that the product can flow in until the chamber 27 is emptied.
    In the chamber 27, the same pressure as in the evaporator 17. In the chamber 27 is the piston rod 23, on which the pistons 21, 40 and 22 are located. It is assumed that the piston 21 is in the end position on one side of the chamber. The piston 21 is driven by the piston 40, which also moves on the other side a piston 22 with the same function. The piston 40 is acted upon by the gas pressure from the gas reservoir 34, so that the piston 40 is moved by the gas pressure. The piston 40 has a larger engagement surface than the piston 21 and 22 and pushes the piston 21 and 22 to the other chamber wall, whereby the gas from the chamber 27 is pressed into the evaporator 17 until the chamber 27 is depressurized on this page , While one chamber 27 is emptied, the other chamber 28 is filled with open shut-off valves 4 and 12 with medium from the tank 1.
    For movement of the piston 40, the pressurization by the gas from the gas reservoir 34 opposite side of the cylinder 29 must be relieved of pressure. For this purpose, the pressure on this side of the cylinder 29 is lowered depending on the substance data, with a reduction to preferably 100 bar in the case of methane. The chamber to be relieved of the cylinder 29 is therefore set by opening the obturator 36 with the gas space of the tank 1 in conjunction, so that the gas sinks by throttling or a relaxation machine in the connecting line 37 to the predetermined pressure. The pressure is set by a tank 1 upstream Überströmer. Before the gas reaches the overflow, it flows through the heat exchanger 16 and is cooled there with the standing at boiling temperature liquid of the tank 1. The gas temperature drops in the heat exchanger 16 below the critical temperature and the gas condenses. At the overflow liquid is under very high pressure.
    The pressure is reduced by opening the overflow to the set pressure by relaxing in the tank, whereby due to the throttling liquid and gas phase or liquid only. In the tank 1 liquefied gas and possibly some gas passes. The pressure does not rise because liquid previously flowed from the tank 1 into the chamber 28 and the liquid level was lowered.
    The process described is now repeated by the chamber 28, which was filled with liquid medium from the tank 1, is connected to the evaporator 17.
    The plant according to Fig. 2 comprises a vacuum-insulated tank 41 in which cryogenic liquefied gas, e.g. Methane or other cryogenic liquefied gas is stored. The tank 41 is connected via a line 42 and shut-off valves 43 and 44 selectively connected to the chamber 45 or the chamber 46 of the cylinder 47. The cylinder 47 is thermally insulated, in particular vacuum-insulated. The gas return 48 of the chamber 45 and the gas return 49 of the chamber 46 are each connected via a shut-off device 50 and 51 with the gas space of the tank 41. The inlet of the chamber 45 and the chamber 46 are each a shut-off device 52 and 53, a line 54 and a heat exchanger 55 with a
    Evaporator 56 connected. The gas return 48 of the chamber 45 and the gas return 49 of the chamber 46 are each connected via a shut-off device 57 and 58 and a line 59 also connected to the evaporator 56.
    In the cylinder 47, a displacement piston 60 is slidably mounted. The piston 60 is connected by means of a rigid connection on the rod 61 with an actuating piston 62 which is slidably guided in a cylinder 63. The cylinder 63 has at its opposite ends via inlets and outlets 64 and 65, via which pressure medium can be supplied on one side, while on the other side a pressure relief is made. For supply of pressure medium, the Zu- or. Runs 64 and 65 connected via shut-off devices 66 and 67 with a pressure accumulator 68. For pressure relief, the inlets and outlets 64 and 65 via shut-off valves 69 and 70, a line 71 and the heat exchanger 55 are connected to the overflow valve 72, where the gas to tank pressure (intermediate tank 73, which is in communication with the tank 41) relaxed becomes.
    To the evaporator 56, a pressure accumulator 75 is connected via a shut-off device 74, which are filled with the medium regasified in the evaporator 56 and then can be removed. The pressure vessel 68 may also be powered by the evaporator 56 via a shut-off device 76.
    The operation of the regasification plant shown in FIG. 2 is now as follows. From the vacuum-insulated tank 41, the liquefied gas flows into the chamber 46 solely by the geodesic pressure.
    For this purpose, the obturator 43 is opened and made by opening the obturator 51, a connection to the gas space of the tank 41 (gas decrease). If the chamber 46 is filled and the gas that may have formed has flowed out of the chamber 46 into the tank 41, the chamber 46 is separated from the tank 41 by closing the shut-off elements 43 and 51. Now the connection to the evaporator 56 is established by opening the obturator 52. Again, there is a gas return from the evaporator outlet via the line 59 to the gas return 49 of the chamber 46 by opening the obturator 58, which produces a pressure equalization and allows the rapid emptying of the chamber 46 by the geodesic pressure.
    Between chamber 46 and evaporator 56, a heat exchanger 55 is interposed in series. The product flows through the geodesic pressure from the chamber 46 first in the evaporator 56 upstream heat exchanger 55. This is below the chamber 46, but above the evaporator 56. Therefore, the liquid flows only through the geodetic pressure in the heat exchanger 55 and fills it , Excess product flows through it into the underlying evaporator 56. There it comes to a sudden evaporation, so that the product can flow in until the chamber 46 is emptied.
    In the chamber 46, the same pressure is established as in the evaporator 56. In the current process, this must be a pressure in the supercritical range. On the piston rod 61 are the pistons 60 and 62. It is assumed that the piston 60 is in the end position on the one (right) side of the cylinder 47. The piston 60 is driven by the actuating piston 62. The piston 62 is acted upon by the gas pressure from the gas reservoir 68, so that the piston 62 is moved by its gas pressure. The piston 62 has a larger engagement surface than the piston 60 and pushes the piston 60 to the other wall of the cylinder 47, whereby the gas from the chamber 46 is pressed into the evaporator 56 until the chamber 46 is depressurized. While one chamber 46 is emptied, the other chamber 45 is filled with open shut-off valves 44 and 50 with medium from the tank 41.
    To move the piston 62 has the
    Pressurization by the gas from the gas storage 68 opposite side of the cylinder 63 are relieved of pressure. For this purpose, the pressure on this side of the cylinder 63 is lowered depending on the substance data, with a reduction to preferably 100 bar in the case of methane. The pressure moves on an isobar, which in no state reaches the vapor space of the gas. The chamber to be relieved of the cylinder 63 is therefore set by opening the obturator 69 and 70 via the line 71 with the gas space of the tank 41 in conjunction, so that the gas drops by throttling or a relaxation machine in the connecting line to the predetermined pressure. The pressure is established by an overflow 72 upstream of the tank 41. Before the gas reaches the overflow 72, it flows through the heat exchanger 55 and is cooled there with the standing at boiling temperature liquid of the tank 41. The gas temperature drops in the heat exchanger 55 below the critical temperature and the gas condenses. At the overflow 72 fluid is under very high pressure. The pressure is reduced by opening the spill 72 to the set pressure by relaxing in the tank 41, wherein by the
    Throttling liquid and gas phase or only liquid incurred. In the tank 41 liquefied gas and possibly some gas passes. The pressure does not rise because liquid previously flowed from the tank 41 into the chamber 45 and the liquid level was lowered.
    The process described is now repeated by the chamber 45, which was filled with liquid medium from the tank 41, is connected to the evaporator 56.
    Up to here, the exemplary embodiment according to FIG. 2 essentially corresponds to the exemplary embodiment according to FIG. 1.
    It will now be shown with reference to FIG. 2 that the regasification method described above can be used in the context of a system for demand-dependent regulation and delivery of the electrical output power of an energy converter operated with regenerative energy. For this purpose, an energy converter is provided as a wind turbine 77. The power generated by the wind turbine 77 is supplied to a device 78 which is capable of switching between different power sources or interconnecting them to one another
    Air liquefaction plant or an air separator 79 to supply power. The system 79 now liquefies, for example, the ambient air, wherein the liquid product is stored in an atmospheric tank 80. From there, the liquid product passes through a pump 81 in the low-pressure tank 41st
    In times of supply surplus of electricity, the electricity generated by the wind turbine 77 is used for the operation of the air liquefaction plant 79. The energy stored in the liquid product can be recovered as needed by regasifying the liquefied gas, which can be done by the method described above. The high-pressure gas thus generated is stored in the gas storage such as e.g. stored in gas cylinders 75. As described below, the energy released by the regasification can be converted into electrical energy as follows:
    Driving a pressure-increasing device by means of the pressure of the regasified gas,
    Using the pressure increasing device to compress a liquid medium, such as water and press it into a turbine, where it is relaxed,
    Driving an electric generator with the help of the turbine to obtain electrical energy.
    In the embodiment according to FIG. 2, the pressure-increasing device comprises a pressure lock 82 which comprises a cylinder 83 on one side and a cylinder 84 of smaller cross-section on the other side. In the cylinder 83 and in the cylinder 84, a piston 85,86 is displaceably guided, wherein the two pistons 85,86 are rigidly coupled together. On the side with the larger piston diameter, the pressure lock is acted upon by opening the obturator 87 or 88 with the gas from the gas reservoir 75. The pressure relief of the respective opposite side of the cylinder 83 via the obturator 89 and 90, the heat exchanger 91 and the spill valve 93 to tank pressure of the tank 41 and 73rd
    The smaller side of the pressure lock 82, i. the chambers of the cylinder 85 are alternately filled with a liquid, preferably water. This water comes with the
    Gas pressure in the turbine 94 is pressed, which is coupled to a generator 95. The generator generates the power for the network requirement. As the piston 86 moves in one direction, the liquid or water is forced into the turbine 94 and water flows back on the piston back. The gas pressure, and thus the pressure at the smaller piston 86, is provided by the piston 85 of the large cylinder 83. For this to move, the gas pressure is lowered at the other side of the piston so that the resulting differential pressure defines the inlet pressure to the turbine 94.
    The process is controlled by shut-off valves. Through the opening of the respective cylinder chamber is filled with an advantageous manner of pressureless water, or lowered the pressure gas side leading to a low pressure. The pressure should be left of the critical point in the TS diagram. The effluent gas is passed into the heat exchanger 91, where it is cooled below the critical temperature, so that a portion of the gas condenses. In the overflow valve 92, the relaxation takes place on tank pressure. The gas content describes the possible efficiency of the process.
    With regard to process control, the energy storage process consists of two completely independently operating circuits. One is the gas liquefaction process. In this case, the volatilely occurring electricity of the wind turbine or a photovoltaic system in the condenser 79 is used entirely for gas liquefaction. The liquefied gas is the storage medium and is stored in appropriate tanks. In the case of the electricity demand of the network to be supplied
    Liquid taken from this memory and fed to the regasification, so that with this gas, the power generating turbine 94, coupled to the generator 95, can be driven and supplied the power grid needs.
    It is unlikely that the wind turbine / photovoltaic system supplies power that ensures the operation of the condenser 79 at the optimum point. If the condenser 79 does not operate at the optimum operating point, the liquid yield is low, so that the achievable under favorable conditions efficiency is not achieved.
    In order to avoid this condition, so much power can be generated at the turbine 95 of the mains supply that current is diverted for optimum operation of the condenser 79 (power connection 96) and, if necessary, the network is supplied 100%.
    If the power requirement for the condenser 79 to be produced by the turbine 95 is less than the loss due to a poor efficiency of the condenser 79, the condenser 79 may be switched off or go into stand-by mode.
    Example: The condenser 79 has a requirement of 100 units, the efficiency of the liquefaction is 80%. If the turbine 94 is 100 units and the wind turbine 77 produces 10 units, the condenser will go into stand-by mode. If the windmill produces 30 units, then 10 units will be stored net.
    权利要求:
    Claims (36)
    [1]
    Claims:
    A process for regasifying cryogenic liquefied gas, e.g. Methane, in which a subset of located in a tank cryogenic liquefied gas is supplied from the tank via a pressure lock an evaporator in which evaporates this subset, whereupon the vaporized gas filled into a high-pressure gas storage, fed into a network or an energy converter for generating electrical energy is supplied, characterized in that the pressure lock comprises two chambers (27,28) which are alternately filled with a subset of the cryogenic liquefied gas from the tank (1), wherein the filled with the subset chamber (27, 28) after the each filling operation of the tank (1) is separated and connected to the evaporator (17), whereupon a pressure equalization between the evaporator (17) and the chamber connected thereto (27, -28) adjusts, and then at least one displacement body ( 21, 22) is displaced in such a way that it contains the chamber (27, 28) which is under evaporator pressure at least partially displaced into the evaporator (17) and the other chamber (28; 27) is filled with a portion of the cryogenic liquefied gas from the tank (1).
    [2]
    2. The method according to claim 1, characterized in that the two chambers (27,28) alternately with the tank (1) and with the evaporator (17) are connected.
    [3]
    3. The method according to claim 1 or 2, characterized in that the subset of the cryogenic liquefied gas from the tank (1) under the geodetic pressure in the chamber (27,28) is filled.
    [4]
    4. The method according to claim 1, 2 or 3, characterized in that the gas under the geodetic pressure from the chamber (27,28) in the evaporator (17) is spent.
    [5]
    5. The method according to any one of claims 1 to 4, characterized in that the movement of the gas from the chamber (27,28) in the evaporator (17) via a heat exchanger (16) takes place, in which the liquefied gas heat is supplied.
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that each chamber (27; 28) is associated with its own displacement body (21; 22), wherein the displacement body (21; 22) for simultaneously displacing the gas from the one chamber (27; 28) in the evaporator (17) and filling the other (28; 27) chamber with cryogenic liquefied gas from the tank (1) are moved synchronously.
    [7]
    7. The method according to any one of claims 1 to 6, characterized in that the displacement of the or the displacement body (21,22) takes place by applying gas pressure, in particular with gas pressure from a from the evaporator (17) fed high-pressure gas storage (34).
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that an actuating piston (40) in an actuating cylinder (29) displaceable and for synchronous movement with the or the displacement body (s) (21,22) is mounted and the displacement the or the displacement body (21,22) by biasing the actuating piston (40) is applied with gas pressure after or at the opposite side of the actuating piston (40), a pressure release is (is).
    [9]
    9. The method according to claim 8, characterized in that the pressure release takes place in that the gas located on the opposite side of the actuating piston (40) is preferably cooled to condensation and expanded by throttling and liquefied and gaseous gas to the tank ( 1) is returned.
    [10]
    10. The method according to claim 9, characterized in that the gas is led to its condensation via the heat exchanger (16) and cooled in heat exchange with the of the chamber (1) in the evaporator (17) guided liquid, wherein the condensation in the heat exchanger (16) is preferably carried out at constant pressure and a cooling is made up to an isobar in the T, s diagram, which is on the left of the critical point and outside the steam range.
    [11]
    11. A method of harnessing energy stored in cryogenic liquefied gas, wherein the liquefied gas stored in a tank is regasified and energy released from the regasified gas is converted into electrical energy and made available to electrical consumers, characterized in that the conversion of the releasing energy into electrical energy comprising the steps of: driving a pressure-increasing device by means of the pressure of the regasified gas, using the pressure-increasing device to compress a liquid medium, for example water and press it into a turbine, where it is relaxed, driving an electric generator Help the turbine to get electrical energy.
    [12]
    12. The method according to claim 11, characterized in that a piston engine is used as the pressure increasing device.
    [13]
    13. The method according to claim 11 or 12, characterized in that the relaxed in the expansion machine liquid medium, such as water, the pressure-increasing device is returned.
    [14]
    14. The method of claim 11, 12 or 13, characterized in that the regasified gas is supplied to drive the pressure increasing device of a drive chamber of the pressure-increasing device and the gas leaving the drive chamber is passed through a heat exchanger in which it preferably at constant pressure (preferably left the critical point in the Ts diagram) is preferably cooled to condensation without affecting the vapor region.
    [15]
    15. The method according to claim 14, characterized in that the cooled in the heat exchanger gas is expanded via a throttle point in the tank.
    [16]
    16. The method according to any one of claims 11 to 15, characterized in that the regasification of the liquefied gas stored in the tank by means of a method according to one of claims 1 to 10 takes place.
    [17]
    17. A method for demand-dependent control and delivery of the electrical output power of a regenerative energy-powered energy converter, in particular electric generator, wherein a gas, for example air, is liquefied in a device coupled to the energy converter, the liquefied gas is preferably stored without pressure in a tank and the energy stored in the liquefied gas is converted into electrical energy as needed by a method according to any one of claims 11 to 16 and made available to electrical consumers.
    [18]
    18. The method according to claim 17, characterized in that at least a part of the electrical energy obtained by the conversion is supplied to the gas liquefying apparatus for the operation thereof as needed.
    [19]
    19. A device for carrying out a method according to one of claims 1 to 10, comprising a tank (1) for cryogenic liquefied gas, an evaporator (17) and arranged between the tank and the evaporator pressure lock, characterized in that the pressure lock two chambers (27,28), which are filled alternately with a subset of the cryogenic liquefied gas from the tank (1) and after the respective filling of the tank (1) separable and connectable to the evaporator (17), and that at least a displacement body (21, 22) is provided which is arranged to displace the gas contained in the chamber under evaporator pressure (27, 28) into the evaporator (17).
    [20]
    20. The apparatus according to claim 19, characterized in that the at least one displacement body (21,22) is designed as displaceable in a cylinder mounted displacement piston.
    [21]
    21. The device according to claim 19 or 20, characterized in that the two chambers (27,28) via shut-off valves (3,4,11,12; 13,14,18,19) each with the tank (1) and with the Evaporator (17) are connected so that they can be connected alternately with the tank (1) and with the evaporator (17).
    [22]
    22. Device according to claim 19, 20 or 21, characterized in that each chamber (27; 28) has its own displacement body (21; 22), the displacement bodies (21; 22) of both chambers (27; 28) being too synchronous Motion are coupled with each other.
    [23]
    23. Device according to claim 22, characterized in that the displacement pistons (21, 22) displaceably mounted in particular in a respective cylinder (6; 8) rotate synchronously with an actuating piston (40) displaceably mounted in an actuating cylinder (29) are coupled.
    [24]
    24. The device according to claim 23, characterized in that at least one line acted upon by gas pressure in the actuating cylinder (29) opens, so that the displacement of the or the displacement body (21,22) by unilaterally pressurizing the actuating piston) 40) takes place with gas pressure.
    [25]
    25. The apparatus of claim 23 or 24, characterized in that two on both sides of the actuating piston (40) in the actuating cylinder (29) opening, each be acted upon by the gas pressure lines are provided.
    [26]
    26. The device according to one of claims 19 to 25, characterized in that the one chamber (27; 28) and the evaporator (17) respectively connecting line (15) via a heat exchanger (16) leads.
    [27]
    27. Device according to one of claims 19 to 26, characterized in that the tank (1) and the chambers (27.28) of the pressure lock are thermally insulated.
    [28]
    28. Device according to one of claims 19 to 27, characterized in that the volume of the chambers (27.28) is smaller in each case than the volume of the evaporator (17) and possibly downstream of him containers.
    [29]
    29. An apparatus for utilizing energy stored in cryogenic liquefied gas, in particular for carrying out the method according to one of claims 11 to 16, comprising a tank for storing the liquefied gas, a regasification device connected to the tank for regasifying the liquefied gas, an energy converter for Converting the energy released by the regasification into electrical energy, wherein the electrical energy supplied by the energy converter is provided to electrical consumers, characterized in that the energy converter comprises a pressure-increasing device which is drivable with the pressure of the regasified gas, wherein the pressure-increasing device is arranged in order to compress a liquid medium, for example water, fed to the pressure-increasing device, that the energy converter further comprises an expansion machine, in particular a turbine, with which the pressure booster is connected to the expansion machine to supply the compressed liquid medium, and that the energy converter further comprises an electric generator which is drivable by the expansion machine.
    [30]
    30. The device according to claim 29, characterized in that the pressure-increasing device is designed as a piston machine.
    [31]
    31. The apparatus of claim 29 or 30, characterized in that the expansion machine is connected via a return line to the pressure increasing device to recycle the relaxed in the expansion machine liquid medium, such as water, the pressure-increasing device.
    [32]
    32. Apparatus according to claim 29, 30 or 31, characterized in that the drive side of the pressure-increasing device is connected to a heat exchanger to the one driving chambers of the pressure-increasing device leaving gas whose isobar in the liquid region ends without affecting the steam zone to pass through the heat exchanger ,
    [33]
    33. The apparatus of claim 32, characterized in that the heat exchanger is connected via a throttle point with the tank to supply the cooled in the heat exchanger gas to the tank.
    [34]
    34. Device according to one of claims 29 to 33, characterized in that the regasification device according to one of claims 19 to 28 is formed.
    [35]
    35. A device for demand-dependent control and output of the electrical output of a regenerative energy driven energy converter, in particular an electric generator, in particular for carrying out the method according to claim 17 or 18, comprising a coupled to the energy converter Gasverflüssigungsvorrichtung, a tank for storing the liquefied gas and a Device according to one of claims 29 to 34 for converting the energy stored in the cryogenic liquefied gas into electrical energy.
    [36]
    A device according to claim 35, characterized in that at least part of the electrical energy obtained by the conversion is supplied to the gas liquefying apparatus for its operation as required.
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    同族专利:
    公开号 | 公开日
    EP3208512B1|2019-11-20|
    AT518299B1|2018-03-15|
    EP3208512A1|2017-08-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP1306604A2|2001-10-29|2003-05-02|Chart Inc.|Cryogenic fluid delivery system|
    US5884488A|1997-11-07|1999-03-23|Westport Research Inc.|High pressure fuel supply system for natural gas vehicles|DE102018206073B3|2018-04-20|2019-10-24|Technische Universität Dresden|System and method for the compression and transfer of liquefied fuel to the gas phase|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    AT342016|2016-02-18|
    ATA8002/2017A|AT518299B1|2016-02-18|2016-02-18|Process for regasifying cryogenic liquefied gas|ATA8002/2017A| AT518299B1|2016-02-18|2016-02-18|Process for regasifying cryogenic liquefied gas|
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