• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:

    公开号:AT510279A4
    申请号:T0024011
    申请日:2011-02-22
    公开日:2012-03-15
    发明作者:Klaus Dipl Ing Engelhart；Thomas Dr Trixner
    申请人:Klaus Dipl Ing Engelhart；Thomas Dr Trixner；
    IPC主号:
    专利说明:

    15357
    The invention relates to a method for converting energy, in which in a primary circuit, a heat transfer medium is heated and vaporized by an external energy source, the heat transfer medium is then expanded to obtain mechanical work, then condensed in a condenser and by a feedwater pump back to the external energy source is performed, wherein the heat transfer medium in a condenser emits heat to a cooling medium, which is cooled in a wet cooling tower in a cooling circuit, and wherein the cooling medium is continuously supplemented by fresh water, which is supplied via a fresh water supply line.
    The production of electrical energy from solar energy can be done in a known manner by photovoltaic solar systems. The cost of such equipment is relatively high, so that broad-based implementation is not economically viable at the moment.
    Alternatively, solar heat can be used to heat a heat transfer medium, which is used in a cyclic process to generate mechanical work.
    The present method is essentially based on a conventional steam power process in which a liquid-gas or liquid-phase change takes place in each cycle, as is the case with the Clausius-Rankine process. Essential in any such cycle is in addition to the temperature on the hot side, the temperature on the capacitor side, which should be as low as possible to achieve high efficiency.
    The inventive method is intended to be used in particular in the subtropical and tropical areas, in which usually the removal of heat is only possible via cooling towers. Cooling towers can on the one hand be designed as dry cooling towers and, on the other hand, as wet cooling towers. Dry cooling towers have the advantage that virtually no consumption of coolant occurs. However, a disadvantage is the significantly poorer efficiency of the cycle due to the increased temperature in the condenser and the energy consumption for a fan. When cooling in a wet cooling tower comparatively low temperatures in the condenser can be achieved, however, it is necessary that cooling medium continuously supplemented by fresh water, as systematically permanent losses occur by evaporation.
    On the other hand, plants for the desalination of seawater are known, which produce distilled water by stepwise evaporation and recondensation. It is known to use for this purpose the so-called MSF process, in which several stages follow one another, in which, with gradually decreasing 4 * I * * * 4 4 4 * I * * * 4 4 2- • · * ·
    Pressure liquid phase and vapor phase are present at gradually lower temperatures. Energy maintenance is required to maintain the MSF process, which is costly.
    The object of the present invention is to further develop a method of converting energy of the type described above so that a higher efficiency is achieved. In addition, it should be possible, as needed, to achieve a partial desalination of the supplied fresh water with low energy consumption.
    According to the invention, the fresh water first gives off heat in a heat exchanger to the condensed heat transfer medium before it is fed to the cooling circuit in the wet cooling tower.
    An essential feature of the method according to the invention is that the fresh water is supplied at a relatively high temperature and the amount of heat transported in order to preheat the heat transfer medium is used. In this way, for example, when using solar energy with a smaller collector area Auslangen be found. Based on the collector surface thus the efficiency is increased.
    It is also important that not all the cooling water must be transported over an optionally very long line, but only the proportion that is consumed on the one hand by evaporation in the cooling tower and on the other hand by deduction of concentrated brine.
    It is particularly preferred if the fresh water is heated in a supply line from a fresh water source to the heat exchanger by solar radiation, wherein preferably a temperature of more than 80 ° C and particularly preferably a temperature of more than 110 ° C is reached. Already by minor structural measures, the already required supply line for fresh water can be designed so that this reaches the actual system with the above-mentioned high temperature. In this way, the efficiency-degree advantage can be realized with virtually no additional effort.
    Preferably, the inventive method is operated so that the fresh water is then supplied when sufficient solar radiation is available to heat it in the supply line. In order to cover the permanently occurring need for fresh water, appropriate buffer storage must be provided.
    For longer supply lines, however, the duration of the flow through the fresh water supply lines may be several days, if one tries to avoid too high flow velocities in order to minimize the losses.
    t · I * 9 4 9 * ring. In this case, the heat capacity of the sand bed in which the pipes are laid, sufficient to allow continuous operation of the fresh water supply.
    A particularly advantageous embodiment of the method according to the invention is characterized in that the fresh water in the heat exchanger is successively passed through a plurality of chambers which are partially filled with liquid fresh water and partly with fresh steam water and in which a different pressure is set, which decreases in the flow direction of the fresh water , The heat exchanger is thus structurally modeled on an MSF system. As a result, the energy of the fresh water can be delivered in a particularly efficient manner to the heat transfer medium. In particular, it is possible that preheaters are provided in the gas chambers of the individual chambers, where fresh water condenses, since the preheaters are flowed through by the relatively cool heat transfer medium. In this way it is possible to carry out a desalination of the fresh water. Depending on the design of the system, about 10% of distilled water is then recovered from the fresh water, while the main part of the fresh water is led to the wet-cooling tower with a slightly elevated salt content of, for example, 4%.
    Particularly preferred are the pressure differences in the individual chambers maintained by steam jet pumps, which are provided above each chamber. The suppression of the last chamber is established and maintained via a vacuum pump connected to another condenser and to a separator. In contrast to known systems in which a common steam jet pump maintains the negative pressure of each chamber, a considerable energy saving is achieved here. In particular, it is not necessary to divert live steam for the operation of the individual steam jet pumps, only the vacuum pump for generating the negative pressure in the very last chamber must be driven by external power supply and may for example be designed as a steam jet pump, which is operated with live steam. However, the amount of live steam needed here is much smaller than in the case in which all chambers are evacuated with live steam, which increases the overall efficiency of the system accordingly. The interconnection is carried out in particular so that gas (non-condensable gases which are dissolved in the fresh water and vaporous fresh water) is sucked out of the chamber assigned to it via each steam jet pump. The individual steam jet pumps are connected in series, i. the input and output ports of successively arranged pumps are connected respectively.
    Furthermore, the present invention also relates to a device for converting energy, with an external energy source for heating a heat transfer medium, a working machine for obtaining mechanical work by
    Relaxation of the heat transfer medium, a condenser for condensation of the heat transfer medium and a feed water pump for conveying the heat transfer medium to the external energy source, and with a wet cooling tower for cooling a cooling medium, which is heated in the condenser, and with a supply line for fresh water to supplement the vaporized in the cooling tower cooling medium.
    In order to simplify the illustration of the invention, a simple steam cycle is described below. In reality, a circuit with multiple reheats will be used as needed and circumstances. The process of the invention is used in the low-pressure stage.
    According to the invention, a heat exchanger is provided which on the one hand flows through the fresh water in order to cool it and on the other hand flows through the condensed heat transfer medium in order to heat it.
    Due to the system according to the invention, the efficiency of cycle processes following solar co-octors or the like can be significantly increased. In particular, it is possible to provide the amount of distilled water in the plant itself required for cleaning the levels of the collectors and for the steam cycle, without causing significant additional expense. However, the method according to the invention and the device for carrying out the method can also be combined with other forms of primary energy. For example, natural gas can be used.
    In the following, the invention will be explained in more detail with reference to the embodiments illustrated in FIGS.
    1 shows a schematic circuit diagram of a system for carrying out the method according to the invention; Fig. 2 shows schematically the basic structure of a steam jet pump and Fig. 3 shows a fresh water supply line in section.
    In the circuit diagram of Fig. 1, a primary circuit is initially designated 1. In this case, a heat transfer medium is heated by an external energy source 2, which is formed in the present case by an array of solar panels 3. In order to achieve higher temperatures, the solar collectors 3 are provided with concentrators 3a, for example in the form of mirrors. The heated and at least partially vaporized heat transfer medium is expanded in a turbine 4, which is connected to a generator 5 in order to feed electricity into a schematically indicated power network 6. The expanded heat transfer medium is passed via a first line 7 in a condenser 8, in which it is cooled and condensed. A first feedwater pump 9 conveys the heat transfer medium into a heat exchanger 10, in... *. 1 * * * "4 · the preheating of the heat transfer medium takes place. Another feedwater pump 11 conveys the heat transfer medium via a further line 12 back to the external energy source 2 to close the primary circuit 1.
    The cooling of the heat transfer medium in the condenser 8 via a cooling circuit in which a cooling medium is passed through the condenser 8, thereby heated by the heat transfer medium and is guided into a wet cooling tower 13 in which it distributes a plurality of spray nozzles 14 to a spray becomes. Due to the heat of evaporation of the partially evaporating cooling medium heat is removed from the remaining cooling medium and the thus cooled cooling medium is collected in a collecting trough 15 of the wet cooling tower 13 and fed via a coolant pump 16 in turn the capacitor 8.
    The cooling medium evaporated in the wet cooling tower 13 is continuously supplemented by fresh water, which is supplied via a connecting line 17, in which a fresh water pump 18 is provided. In order not to increase the salt content of the cooling medium beyond an allowable limit, moreover, cooling medium is continuously withdrawn from the collecting trough 15 of the wet cooling tower 13 and disposed of via a disposal pump 19. The disposal may, for example, consist in that in corresponding basin 20 a salt extraction is carried out analogously to the sea salt extraction. Upstream of the fresh water pump 18, the fresh water passes through the heat exchanger 10 by being cooled. The supply of fresh water takes place from a fresh water source, such as the sea, which is indicated here schematically with 21. Via a corresponding fresh water supply line 22, which is equipped with supply pumps 23, the fresh water is supplied to the heat exchanger 10. Depending on the position of the device, the length of the fresh water supply line 22 may be between several tens of kilometers and several hundred kilometers. Since the plant is primarily intended for subtropical or tropical areas, the fresh water in the fresh water supply line 22 is heated by solar radiation (schematically indicated by arrows 24) and reaches the heat exchanger 10 with temperatures that can be 90 ° C or more.
    In the following, the structure of the heat exchanger 10 and the associated system parts will be described in more detail. The heat exchanger 10 is divided into a plurality of chambers 25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j. The chambers 25a to 25j are arranged substantially vertically and have a height of several meters. They are separated by partitions 26 against each other, but are provided in the lower part by flow openings 27 through which the fresh water can flow through the heat exchanger 10. In operation, the chambers 25a to 25j in the lower area with liquid
    Fresh water and filled in the upper part with vaporous fresh water, which is due to the given pressure differences, a different liquid level 28 sets, which will be explained in more detail below. The internal pressure in the chambers 25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j drops from the ambient pressure in the first chamber 25a in the flow direction, for example by 0.1 bar.
    In the upper region of the individual chambers 25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j each preheater 29 are provided, which are flowed through by the heat transfer medium of the primary circuit 1 against the flow direction of the fresh water, wherein the heat transfer medium from the Capacitor 8 is supplied. In any case, the individual preheaters 29 are arranged so high that in the section filled with fresh vaporous water, i. located above the liquid level 28. Below the individual preheater 29, a collecting trough 30 for condensed fresh water is formed in each case in order to collect the fresh water condensed on the preheaters 29. In this condensed fresh water from the drip pans 30 is a distillate, which is salt-free accordingly and can be used as distilled water. This distilled water is fed to a separator 31, which is partially filled with liquid distilled water and partly with condensable gases. About a discharge line 32, the distilled water is withdrawn. A vacuum pump 35, for example in the form of a steam jet pump driven by live steam, provides for a corresponding suppression in the separator 31 by discharging the non-condensable gases.
    At the upper portion of the individual chambers 25b to 25j (except for the first chamber 25a), steam jet pumps 33b to 33j are connected, respectively. The wiring is exemplified for the steam jet pump 33c above the chamber 25c. It must be said in advance that in principle the pressure in the interior of the chambers 25a to 25j gradually decreases in the direction of flow of the fresh water, that is to say in FIG. 1, from left to right. Accordingly, the liquid level 28 increases from left to right. The steam jet pump 33c above the chamber 25c sucks from this gas and is thereby driven by the flow directed from the upstream steam jet pump 33b to the downstream steam jet pump 33d.
    Essential to this wiring is that the pressure differences between adjacent chambers 25a to 25j are relatively small, so that the efficiency of the individual steam jet pumps 33b to 33j is very large.
    The steam jet pump 33j of the most downstream chamber 25j is connected to the gas space of the separator 31 via another condenser 34. The extracted in the steam jet pump 33j steam is cooled in this further capacitor 34 by a partial flow of the cooling medium from the sump 15 of the wet cooling tower 13 and largely condensed, which partial flow is driven by a feed pump 36. Downstream of the further capacitor 34, the partial flow is reunited with the exiting from the condenser 8 main flow of the cooling medium.
    FIG. 2 shows one of the steam jet pumps 33b to 33j, which is designated here by way of example as 33. The input port 37 is connected to an output port 38 via a nozzle assembly 40, and as described above, the input port 37 of the single steam jet pumps 33c to 33j is connected to the output port 38 of the upstream steam jet pump 33b to 33i, respectively. The inlet port 37 of the first steam jet pump 33b is connected directly to the first chamber 25a. In the nozzle assembly 40, a negative pressure is caused by the flow, which causes gas to be sucked in at the suction port 39, which is connected to the respective associated chamber 25b to 25j.
    Fig. 3 shows a fresh water supply line 22 in section, with a plurality of tubes 41a, 41b and 41c, which are arranged parallel to each other in an insulating trough 42 in a sand bed 43. A cover 44 enhances heat absorption by reducing convection losses at higher temperatures. A return pipe 45 transports concentrated brine back if recovery is not possible at the site of the plant.
    The present invention makes it possible to use solar energy or other alternative energies with high efficiency and at the same time to produce drinking water or distilled water for industrial applications.
    权利要求:
    Claims (20)
    [1]
    • > • * «14» PATENT CLAIMS 1. A process for the conversion of energy, in which in a primary circuit (1) a heat transfer medium is heated and evaporated by an external energy source (2), the heat transfer medium is then expanded to obtain mechanical work, then in a condenser (8) is condensed and by at least one feedwater pump (9, 11) back to the external energy source (2) is guided, wherein the heat transfer medium in a condenser (8) gives off heat to a cooling medium in a wet cooling tower (13) in a cooling circuit is cooled, and wherein the cooling medium is continuously supplemented by fresh water, which is supplied via a fresh water supply line (22), characterized in that the fresh water first in a heat exchanger (10) gives off heat to the condensed heat transfer medium before it the cooling circuit in the wet cooling tower ( 13) is supplied.
    [2]
    2. The method according to claim 1, characterized in that the fresh water in the fresh water supply line (22) from a fresh water source (21) to the heat exchanger (10) is heated by sunlight, wherein the fresh water is preferably a temperature of more than 80 ° C and more preferably reaches a temperature of more than 110 ° C.
    [3]
    3. The method according to any one of claims 1 or 2, characterized in that the fresh water in the heat exchanger (10) successively through a plurality of chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) is performed, which are partially filled with liquid fresh water and partially filled with fresh steam water and in which a different pressure is set, which decreases in the flow direction of the fresh water.
    [4]
    4. The method according to claim 3, characterized in that the heat transfer medium after the condenser (8) by a plurality of preheater (29) is guided, each in the chambers (25a, 25b, 25c, 25h, 25e, 25f, 25g, 25h, 25i, 25j) of the heat exchanger (10) are arranged.
    [5]
    5. The method according to claim 4, characterized in that the preheaters (29) are arranged in a section filled with vaporous fresh water portion of the chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) and that in a collecting trough (30) for condensed fresh water under the preheaters (29) condensed fresh water is collected.
    [6]
    6. The method according to any one of claims 3 to 6, characterized in that in the chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) of the heat exchanger (10) via an arrangement of steam jet pumps - (33b, 33c, 33d, 33e, 33f, 33g, 33h, 33i, 33j) and via a vacuum pump (35) connected to a separator (31) and / or to another condenser (34). a predetermined negative pressure is established and maintained.
    [7]
    7. The method according to claim 6, characterized in that via each steam jet pump (33b, 33c, 33d, 33e, 33f, 33g, 33h, 33i, 33j) gas from its associated chamber (25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j), wherein preferably an input port (37) of the steam jet pump (33c, 33d, 33e, 33f, 33g, 33h, 33i, 33j) to the output port (38) of the upstream chamber (25b , 25c, 25d, 25e, 25f, 25g, 25h, 25i) associated with the steam jet pump (33b, 33c, 33d, 33e, 33f, 33g, 33h, 33i).
    [8]
    8. The method according to any one of claims 6 and 7, characterized in that in a collecting trough (30) obtained condensed fresh water to the separator (31) is passed.
    [9]
    9. The method according to any one of claims 1 to 8, characterized in that the heat transfer medium is heated by solar radiation as an external energy source (2), wherein the sunlight is preferably concentrated.
    [10]
    10. Apparatus for converting energy, with an external energy source for heating a heat transfer medium, a working machine (4) for obtaining mechanical work by relaxation of the heat transfer medium, a condenser (8) for condensing the heat transfer medium and a feedwater pump (9, 11) for the promotion the heat transfer medium to the external energy source (2), and with a wet cooling tower (13) for cooling a cooling medium, which is heated in the condenser (8), and with a fresh water supply line (22) to supplement the cooling medium evaporated in the cooling tower (13), characterized in that a heat exchanger (10) is provided which on the one hand flows through the fresh water in order to cool it and on the other hand flows through the condensed heat transfer medium in order to heat it.
    [11]
    11. The device according to claim 10, characterized in that the supply line for heating the fresh water (22) is formed by Soiarenergie.
    [12]
    12. The device according to claim 11, characterized in that the supply line (22) comprises a plurality of tubes, which are laid side by side in a «» 4 * - 10 - sand bed and optionally covered by a transparent cover upwards.
    [13]
    13. The apparatus according to claim 12, characterized in that in addition to the tubes of the supply line (22) is provided at least one return pipe for the return of saline cooling medium.
    [14]
    14. Device according to one of claims 10 to 13, characterized in that the heat exchanger (10) comprises a plurality of chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) which are interconnected, wherein a first chamber (25a) is connected to the fresh water supply line (22) and a last chamber (25j) is connected to a connecting line (17) leading to the wet cooling tower (13).
    [15]
    15. The apparatus according to claim 14, characterized in that each adjacent chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) with steam jet pumps (33b, 33c, 33d, 33e, 33f, 33g, 33h, 331, 33j) adapted to maintain a predetermined depression in the individual chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j).
    [16]
    16. Device according to one of claims 14 or 15, characterized in that in the chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) each have a pre-heater (29) is provided by the Heat transfer medium can be flowed through.
    [17]
    17. Device according to one of claims 10 to 16, characterized in that with a separator (31) and / or capacitor (34) connected to the vacuum pump (35) is provided to produce the intended negative pressure in the heat exchanger (10).
    [18]
    18. Device according to one of claims 10 to 16, characterized in that in the chambers (25a, 25b, 25c, 25d, 25e, 25f, 25g, 25h, 25i, 25j) is provided in each case a collecting trough (30) for condensed fresh water ,
    [19]
    19. Device according to one of claims 17 and 18, characterized in that the collecting trough (30) for condensed fresh water with the separator (31) is in communication. DipWr.g.wtag. 7iichae! Sabeluk A-USO Vienna, MSF öh! Ti * r Siiitj! 39 / Ϊ7 Tel ·: M3 V fc-i; s «3 4 for *!)« «O 8¾ 333 tan far
    [20]
    20. Device according to one of claims 10 to 19, characterized in that solar collectors (3) with concentrators (3¾ are provided for heating of the heat transfer medium.) 2011 02 22; Ba / St
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    同族专利:
    公开号 | 公开日
    AT510279B1|2012-03-15|
    引用文献:
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    JPWO2004108860A1|2003-06-09|2006-07-20|株式会社日立製作所|New fuel production plant and seawater desalination equipment used therefor|
    JP2005214139A|2004-01-30|2005-08-11|Xenesys Inc|Solar heat power generation and desalination system|
    KR100774546B1|2006-11-13|2007-11-08|두산중공업 주식회사|Seawater desalinating apparatus using blowdown of heat recovery steam generator|US10794228B2|2018-03-29|2020-10-06|XYZ Energy Group, LLC|System and method for the generation of heat and power using multiple loops comprising a primary heat transfer loop, a power cycle loop and an intermediate heat transfer loop|
    法律状态:
    2016-10-15| MM01| Lapse because of not paying annual fees|Effective date: 20160222 |
    优先权:
    申请号 | 申请日 | 专利标题
    AT0024011A|AT510279B1|2011-02-22|2011-02-22|METHOD FOR CONVERTING ENERGY|AT0024011A| AT510279B1|2011-02-22|2011-02-22|METHOD FOR CONVERTING ENERGY|
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