A comprehensive energy station with ammonia working fluid coupled with fuel and operation method thereof

Abstract

The present invention provides an integrated energy station of ammonia working fluid coupled with fuel and an operation method thereof, wherein the integrated energy station comprises a storage unit, an evaporation unit, a separation unit, a power generation unit, a first heat exchange unit, an absorption unit, a second heat exchange unit, a third heat exchange unit and an ammonia energy center; wherein the evaporation unit, the separation unit, the power generation unit, the absorption unit, the second heat exchange unit and the third heat exchange unit are cyclically connected in sequence; the power generation unit and the third heat exchange unit are also independently connected to the ammonia energy center; the first heat exchange unit is independently connected to the storage unit, the evaporation unit, the separation unit, the absorption unit and the ammonia energy center; the storage unit is also independently connected to the evaporation unit and the second heat exchange unit; the integrated energy station utilizes the characteristics of ammonia being both an energy carrier and a working medium of a circulation system, fully couples the two, transforms disadvantages into advantages to form complementarity, and is conducive to industrial production and application.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical energy, and in particular relates to an integrated energy station of ammonia working fluid coupled with fuel and an operation method thereof. Background Art

[0002] The Kalina power cycle system is a power cycle power generation system with ammonia water mixture as the working fluid. Because of the variable temperature characteristics of ammonia water in the evaporation-condensation heat exchange process, it can be applied to the field of waste heat recovery, and is also applied to clean energy fields such as solar energy, geothermal energy, and biomass energy. At present, the cycle power generation system has the following shortcomings and problems: ① Constrained by the circulation system, the waste heat recovery and utilization efficiency is limited; ② The equipment selection requires accuracy, and there is a lack of other operation correction means after construction; ③ The system has limited means of matching and adjusting heat sources with large dynamic reciprocating and intermittent changes in temperature or flow; ④ The system relies on the normal operation of the cold source; ⑤ The subcooling degree of the conventional unit condensing end is low, and the ammonia water pump is prone to cavitation; ⑥ If the cold source end is used for heat, increasing the temperature parameters requires increasing the system back pressure, which affects the system output; ⑦ The heat source system below 60°C is not economical.

[0003] CN214577243U discloses a Kalina coupled power generation system based on solar amino thermochemical energy storage, including an amino thermochemical energy storage system and a Kalina circulation system, wherein the outlet of the separator is respectively connected to the hot end inlets of the sixth heat exchanger and the seventh heat exchanger, and the seventh heat exchanger and the eighth heat exchanger are connected to the feed water pump in sequence to form a loop; the sixth heat exchanger, the throttle valve, the fifth heat exchanger and the condensation pump are connected in sequence to form a loop; the inlet of the separator is connected to the sixth heat exchanger through the fourth heat exchanger; the inlet of the turbine and the cold end outlet of the seventh heat exchanger are respectively interconnected with the amino thermochemical energy storage system, and the outlet is connected to the hot end inlet of the fifth heat exchanger through the fourth heat exchanger, and the outlet pipeline of the throttle valve is interconnected with the fourth pipeline.

[0004] CN102337934A discloses a combined cycle power generation system for improving the efficiency of heat source utilization, including a steam boiler, which is sequentially connected in series to a steam turbine, a condenser and a feed pump, and the feed pump is connected back to the steam boiler to form a Rankine power cycle, and also includes an ammonia evaporator, which is once connected in series to an ammonia vapor-liquid separator, an ammonia absorber / condenser, an ammonia storage tank and an ammonia feed pump, and the ammonia feed pump is connected back to the ammonia evaporator to form a Kalina power cycle.

[0005] However, the above two coupling systems cannot completely solve the problems of Kalina's power cycle system. Since ammonia is one of the most basic chemical raw materials in the world, it has been widely used in the refrigeration industry and has mature industrial preparation technology and transportation system. At the same time, it is also a zero-carbon clean energy and is considered to be an excellent carrier of hydrogen energy. It is stable and safe in nature, inexpensive and easy to store and transport. The energy system centered on ammonia has broad prospects, but there are still the following shortcomings or problems: ① Ammonia stored in liquid form must be vaporized before use, releasing a large amount of cold energy. It is conventionally heated by a hot water boiler, which increases equipment; ② It consumes both cold energy and heat energy; ③ Low temperature affects subsequent combustion and other energy utilization processes.

[0006] In summary, how to utilize the characteristics of ammonia as both an energy carrier and a working medium of the circulation system, fully couple the two, and transform disadvantages into advantages to form complementarity has become a problem that needs to be solved urgently. Summary of the invention

[0007] In view of the problems existing in the prior art, the purpose of the present invention is to provide an integrated energy station with ammonia as the working medium coupled with fuel and an operation method thereof. The integrated energy station utilizes the characteristics of ammonia as both an energy carrier and a working medium of a circulation system, fully couples the two, transforms disadvantages into advantages to form complementarity, achieves the purpose of flexible design and performance improvement, and has a variety of adjustment means, which is conducive to industrial production and application.

[0008] To achieve this object, the present invention adopts the following technical solutions:

[0009] In a first aspect, the present invention provides an integrated energy station of ammonia working fluid coupled with fuel, the integrated energy station comprising a storage unit, an evaporation unit, a separation unit, a power generation unit, a first heat exchange unit, an absorption unit, a second heat exchange unit, a third heat exchange unit and an ammonia energy center;

[0010] The evaporation unit, the separation unit, the power generation unit, the absorption unit, the second heat exchange unit and the third heat exchange unit are connected in a circular manner in sequence; the power generation unit and the third heat exchange unit are also independently connected to the ammonia energy center;

[0011] The first heat exchange unit is independently connected to the storage unit, the evaporation unit, the separation unit, the absorption unit and the ammonia energy center;

[0012] The storage unit is also independently connected to the evaporation unit and the second heat exchange unit.

[0013] In the present invention, the integrated energy station couples and optimizes the Kalina cycle power generation system and the ammonia energy system. On the one hand, it can realize cogeneration of heat and power to meet general heat needs without affecting the power generation performance of the system; on the other hand, the concentration of the ammonia working fluid entering the Kalina cycle power generation system is controllable and adjustable, and the heat exchange process curve of the evaporation unit can be changed or the ammonia filling point can be changed by changing the working fluid concentration, breaking the heat exchange narrow point limitation of the general Kalina power cycle unit; on the third hand, the integrated energy station can effectively utilize the leakage loss of the ammonia turbine of the traditional Kalina power cycle unit; on the fourth hand, the integrated energy station cancels the heat recovery equipment and simplifies the overall composition; on the fifth hand, the integrated energy station can also deeply cool the lean ammonia liquid and optimize the absorption reaction process; on the sixth hand, the ammonia leaving the Kalina cycle power generation system can reduce the back pressure of the gas turbine generator set and improve the output of the cycle power generation system.

[0014] The following are preferred technical solutions of the present invention, but are not intended to be limitations of the technical solutions provided by the present invention. Through the following technical solutions, the technical objectives and beneficial effects of the present invention can be better achieved and realized.

[0015] As a preferred technical solution of the present invention, the storage unit includes at least one liquid ammonia tank, such as 1, 2, 3, 4 or 5, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0016] Preferably, the evaporation unit includes at least one evaporator, for example, 1, 2, 3, 4 or 5, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0017] Preferably, the separation unit includes at least one separator, such as 1, 2, 3, 4 or 5, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0018] Preferably, the power generation unit includes at least one ammonia turbine generator set, such as 1, 2, 3, 4 or 5 sets, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0019] Preferably, the first heat exchange unit includes at least one ammonia water cooler, such as 1, 2, 3, 4 or 5, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0020] Preferably, the absorption unit includes at least one absorber, such as 1, 2, 3, 4 or 5, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0021] Preferably, the second heat exchange unit includes at least one heat recovery device, such as 1, 2, 3, 4 or 5, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0022] Preferably, the third heat exchange unit includes at least one liquid ammonia vaporizer, such as 1, 2, 3, 4 or 5, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0023] Preferably, the ammonia energy center includes any one of an ammonia boiler, an ammonia fuel cell, an ammonia gas turbine, an ammonia blending boiler, an ammonia charging device or an ammonia direct-fired lithium bromide refrigeration unit, or a parallel combination of at least two of them, and also includes various combined heat, power and cooling systems and ammonia chemical processes.

[0024] In the present invention, various devices can be connected in series, in parallel or in a composite form, as long as they can achieve the required functions.

[0025] The absorber and the recycler can be combined into one device to reduce the floor space. For the multi-stage series connection of ammonia turbine generator sets, an intermediate ammonia extraction pipeline can be configured to supply gas to the ammonia energy center or to adjust the operating conditions of the ammonia turbine.

[0026] As a preferred technical solution of the present invention, the cold source outlet of the evaporator is connected to the separator, the gas phase outlet of the separator is connected to the first liquid phase inlet of the absorber through the ammonia turbine generator set, the liquid phase outlet of the absorber is connected to the heat source inlet of the heat energy recovery device, the heat source outlet of the heat energy recovery device is connected to the heat source inlet of the liquid ammonia gasifier, and the heat source outlet of the liquid ammonia gasifier is connected to the cold source inlet of the evaporator through an ammonia water pump.

[0027] In the present invention, a water inlet is connected between the heat source outlet of the liquid ammonia gasifier and the ammonia water pump, for mixing with liquid ammonia to form an ammonia water working medium.

[0028] In addition, a heat exchanger may be added to achieve direct heat exchange between the liquid ammonia in the liquid ammonia tank and the fluid at the heat source outlet of the evaporator to further reduce its temperature.

[0029] As a preferred technical solution of the present invention, the ammonia turbine generator set is also connected to the ammonia energy center.

[0030] In the present invention, ammonia leaking from the shaft end seal of the ammonia turbine can also enter the ammonia energy center through the pipeline.

[0031] Preferably, the cold source outlet of the liquid ammonia gasifier is connected to the ammonia energy center.

[0032] In the present invention, the pipeline connecting the ammonia turbine generator set to the ammonia energy center can be equipped with an air extraction pump, a pressure regulating valve, a pressure stabilizing valve, etc., or used to replace the control regulating valve. At the same time, the ammonia gas leaked from the shaft end seal of the ammonia turbine can be transported to the ammonia energy center through the pipeline;

[0033] As a preferred technical solution of the present invention, the cold source inlet of the ammonia water cooler is connected to the liquid ammonia tank, the cold source outlet of the ammonia water cooler is respectively connected to the cold source inlet of the evaporator and the ammonia energy center, the heat source inlet of the ammonia water cooler is connected to the liquid phase outlet of the separator, and the heat source outlet of the ammonia water cooler is connected to the second liquid phase inlet of the absorber.

[0034] As a preferred technical solution of the present invention, the liquid ammonia tank is independently connected to the cold source inlet of the evaporator and the cold source inlet of the liquid ammonia vaporizer.

[0035] In the present invention, when multiple evaporators are connected in series, the cold source outlet of the ammonia water cooler or the liquid ammonia tank needs to be connected to the cold source inlet of each evaporator respectively, so as to change the ammonia charging point of the evaporator.

[0036] As a preferred technical solution of the present invention, a heat exchanger is provided on the pipeline connecting the separator and the ammonia turbine generator set.

[0037] In the present invention, a heat exchanger may be arranged on the pipeline connecting the separator and the ammonia turbine generator set to further increase the temperature of ammonia entering the ammonia turbine generator set through other heat sources.

[0038] As a preferred technical solution of the present invention, turbine expansion devices are independently arranged on the pipelines connecting the ammonia energy center with the ammonia turbine generator set, the ammonia water cooler and the liquid ammonia gasifier for recovering excess pressure energy.

[0039] In the above-mentioned integrated energy station, each device can be provided with a bypass, each pipeline can be made of various materials and types, and a manual valve or a regulating valve can be provided, and no specific restrictions are made here.

[0040] In a second aspect, the present invention provides an operation method of the integrated energy station described in the first aspect, wherein the liquid ammonia from the storage unit is divided into three streams;

[0041] The first stream of liquid ammonia is evaporated in the evaporation unit and then enters the separation unit to obtain a gas phase and a liquid phase; the separated gas phase enters the power generation unit to generate electricity, and the gas phase after power generation enters the absorption unit to become a liquid phase, and then successively passes through the second heat exchange unit and the third heat exchange unit for heat exchange, and the liquid phase after heat exchange flows into the evaporation unit to form a cycle;

[0042] At the same time, the second stream of liquid ammonia enters the first heat exchange unit, and after heat exchange with the liquid phase from the separation unit, part of it flows into the evaporation unit, and the other part flows into the ammonia energy center; while the liquid phase from the separation unit flows into the absorption unit after heat exchange;

[0043] At the same time, the third stream of liquid ammonia enters the third heat exchange unit, exchanges heat with the liquid phase from the second heat exchange unit, and then flows into the ammonia energy center.

[0044] In the present invention, the evaporation unit is used to evaporate the liquid ammonia. The heat source medium is not limited to water, heat transfer oil, molten salt or flue gas, etc. The source can be outside the system or from the energy center within the system.

[0045] The cold source pipeline of the second heat exchange unit is a heat energy user or an external cooling circuit.

[0046] As a preferred technical solution of the present invention, the cold source inlet temperature of the evaporation unit is controlled to be -20 to 80°C, for example, -20°C, -10°C, 0°C, 10°C, 20°C, 40°C, 60°C or 80°C; the cold source outlet temperature is 80 to 160°C, for example, 80°C, 100°C, 120°C, 140°C or 160°C. The selection of the above numerical values ​​is not limited to the listed numerical values, and other unlisted numerical values ​​within their respective numerical ranges are equally applicable.

[0047] Preferably, the temperature of the gas phase outlet of the separation unit is controlled to be 80-160°C, for example, 80°C, 100°C, 120°C, 140°C or 160°C; the temperature of the liquid phase outlet is controlled to be 80-160°C, for example, 80°C, 100°C, 120°C, 140°C or 160°C. The selection of the above numerical values ​​is not limited to the listed values, and other unlisted values ​​within their respective numerical ranges are also applicable.

[0048] Preferably, the outlet temperature of the power generation unit is controlled to be 50-100°C, such as 50°C, 60°C, 70°C, 80°C, 90°C or 100°C, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0049] Preferably, the heat source inlet temperature of the first heat exchange unit is controlled to be 80-160°C, for example, 80°C, 100°C, 120°C, 140°C or 160°C; the heat source outlet temperature is 10-50°C, for example, 10°C, 20°C, 30°C, 40°C or 50°C; the cold source outlet temperature is -20-50°C, for example, -20°C, -10°C, 0°C, 10°C, 20°C, 30°C, 40°C or 50°C. The selection of the above numerical values ​​is not limited to the listed values, and other unlisted values ​​within their respective numerical ranges are equally applicable.

[0050] Preferably, the heat source inlet temperature of the second heat exchange unit is controlled to be 30-50°C, such as 30°C, 40°C or 50°C; the heat source outlet temperature is 20-40°C, such as 20°C, 30°C or 40°C. The selection of the above numerical values ​​is not limited to the listed values, and other unlisted values ​​within their respective numerical ranges are also applicable.

[0051] Preferably, the heat source inlet temperature of the third heat exchange unit is controlled to be 20-40°C, such as 20°C, 30°C or 40°C; the heat source outlet temperature is 10-30°C, such as 10°C, 20°C or 30°C; the cold source outlet temperature is 0-10°C, such as 0°C, 4°C, 6°C, 8°C or 10°C. The selection of the above numerical values ​​is not limited to the listed values, and other unlisted values ​​within their respective numerical ranges are equally applicable.

[0052] Based on the integrated energy station described in the first aspect, the present invention designs a suitable temperature control system to further improve the use effect of the entire system.

[0053] Compared with the prior art, the present invention has the following beneficial effects:

[0054] (1) The integrated energy station of the present invention couples and optimizes the Kalina cycle power generation system with the ammonia energy system, thereby expanding the scope of heat source recovery, recovering low-temperature heat sources, achieving deep recovery of waste heat, and improving the thermoelectric conversion efficiency;

[0055] (2) In the integrated energy station of the present invention, the mechanical seal part of the ammonia turbine is greatly simplified, thereby extending the maintenance cycle;

[0056] (3) The integrated energy station of the present invention is more flexible in design and provides diversified configurations to meet various customized requirements;

[0057] (4) The integrated energy station of the present invention has strong adaptability and can make corresponding operating mode adjustments in response to design deviations or long-term deviations of the unit from the original operating conditions;

[0058] (5) The integrated energy station of the present invention can improve the working conditions of the key power equipment ammonia pump and enhance reliability;

[0059] (6) The integrated energy station described in the present invention uses liquid ammonia as a cold source for heat exchange, thereby increasing the temperature of ammonia entering the ammonia energy center, optimizing the ammonia energy utilization process, and improving the utilization rate of ammonia resources. BRIEF DESCRIPTION OF THE DRAWINGS

[0060] Figure 1 It is a structural schematic diagram of an integrated energy station with ammonia working fluid coupled with fuel provided in Example 1 of the present invention.

[0061] Figure 2It is a structural schematic diagram of a comprehensive energy station with ammonia working fluid coupled with fuel provided in Comparative Example 1 of the present invention.

[0062] Figure 3 It is a structural schematic diagram of a comprehensive energy station with ammonia working fluid coupled with fuel provided in Comparative Example 2 of the present invention.

[0063] Among them, A-evaporation unit, B-first heat exchange unit, C-second heat exchange unit, D-third heat exchange unit, E-separation unit, F-power generation unit, G-ammonia pump, H-absorption unit, I-ammonia energy center, J-storage unit.

[0064] The direction of the arrow indicates the flow direction of the working fluid. DETAILED DESCRIPTION

[0065] In order to better illustrate the present invention and facilitate understanding of the technical solution of the present invention, the present invention is further described in detail below. However, the following embodiments are only simple examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims.

[0066] The following are typical but non-limiting embodiments of the present invention:

[0067] Embodiment 1:

[0068] This embodiment provides an integrated energy station with ammonia working fluid coupled with fuel and an operation method thereof. The structural schematic diagram of the integrated energy station is shown in FIG. Figure 1 As shown, the integrated energy station includes a storage unit J, an evaporation unit A, a separation unit E, a power generation unit F, a first heat exchange unit B, an absorption unit H, a second heat exchange unit C, a third heat exchange unit D and an ammonia energy center I.

[0069] The storage unit J includes a liquid ammonia tank, the evaporation unit A includes an evaporator; the separation unit E includes a separator; the power generation unit F includes an ammonia turbine generator set; the first heat exchange unit B includes an ammonia water cooler; the absorption unit H includes an absorber; the second heat exchange unit C includes a heat energy recovery device; the third heat exchange unit D includes a liquid ammonia gasifier; and the ammonia energy center I includes an ammonia boiler.

[0070] The cold source outlet of the evaporator is connected to the separator, the gas phase outlet of the separator is connected to the first liquid phase inlet of the absorber through the ammonia turbine generator set, the liquid phase outlet of the absorber is connected to the heat source inlet of the heat energy recovery device, the heat source outlet of the heat energy recovery device is connected to the heat source inlet of the liquid ammonia gasifier, and the heat source outlet of the liquid ammonia gasifier is connected to the cold source inlet of the evaporator through an ammonia water pump G.

[0071] The ammonia turbine generator set is also connected to the ammonia energy center I; the cold source outlet of the liquid ammonia gasifier is connected to the ammonia energy center I.

[0072] The cold source inlet of the ammonia water cooler is connected to the liquid ammonia tank, the cold source outlet of the ammonia water cooler is respectively connected to the cold source inlet of the evaporator and the ammonia energy center I, the heat source inlet of the ammonia water cooler is connected to the liquid phase outlet of the separator, and the heat source outlet of the ammonia water cooler is connected to the second liquid phase inlet of the absorber.

[0073] The liquid ammonia tank is independently connected to the cold source inlet of the evaporator and the cold source inlet of the liquid ammonia vaporizer.

[0074] The operation method of the above-mentioned integrated energy station includes:

[0075] Divide the liquid ammonia from the liquid ammonia tank into three streams;

[0076] The first stream of liquid ammonia is evaporated in the evaporator and then enters the separator to obtain a gas phase and a liquid phase; the separated gas phase enters the ammonia turbine generator set to generate electricity, and the gas phase after power generation enters the absorber to become a liquid phase, and then passes through the heat energy recovery device and the liquid ammonia gasifier in turn for heat exchange, and the liquid phase after heat exchange flows into the evaporator through the ammonia water pump G to form a cycle;

[0077] At the same time, the second stream of liquid ammonia enters the ammonia water cooler, and after heat exchange with the liquid phase from the separator, part of it flows into the evaporator, and the other part flows into the ammonia energy center I; while the liquid phase from the separator flows into the absorber after heat exchange;

[0078] At the same time, the third stream of liquid ammonia enters the liquid ammonia gasifier, exchanges heat with the liquid phase from the heat energy recovery device, and then flows into the ammonia energy center I.

[0079] The cold source inlet temperature of the evaporator is controlled to be 70°C, and the cold source outlet temperature is controlled to be 110°C;

[0080] Controlling the temperature of the gas phase outlet of the separator to be 100-110°C and the temperature of the liquid phase outlet to be 100-110°C;

[0081] Controlling the outlet temperature of the ammonia turbine generator set to 50-60° C.;

[0082] The heat source inlet temperature of the ammonia water cooler is controlled to be 100°C, the heat source outlet temperature is controlled to be 40°C, and the cold source outlet temperature is controlled to be 20°C;

[0083] Control the heat source inlet temperature of the heat energy recovery device to be 40-50°C and the heat source outlet temperature to be 30-40°C;

[0084] The heat source inlet temperature of the liquid ammonia gasifier is controlled to be 30-40°C, the heat source outlet temperature is controlled to be 20-30°C, and the cold source outlet temperature is controlled to be 0-10°C.

[0085] Comparative Example 1:

[0086] This comparative example provides an integrated energy station for coupling ammonia working fluid with fuel and an operation method thereof. The integrated energy station refers to the integrated energy station in Example 1, except that: the first heat exchange unit B is not included, that is, the liquid phase outlet of the separator is directly connected to the second liquid phase inlet of the absorber. The structural schematic diagram is shown in FIG. Figure 2 shown.

[0087] The operation method of the above-mentioned integrated energy station includes:

[0088] Divide the liquid ammonia from the liquid ammonia tank into two streams;

[0089] The first stream of liquid ammonia is evaporated in the evaporator and then enters the separator to obtain gas phase and liquid phase; the separated gas phase enters the ammonia turbine generator set to generate electricity, and the gas phase after power generation enters the absorber to become liquid phase, and then passes through the heat energy recovery device and the liquid ammonia gasifier in turn for heat exchange, and the liquid phase after heat exchange flows into the evaporator through the ammonia water pump G to form a cycle; the separated liquid phase enters the absorber;

[0090] At the same time, the second stream of liquid ammonia enters the liquid ammonia gasifier, exchanges heat with the liquid phase from the heat energy recovery device, and then flows into the ammonia energy center I.

[0091] The cold source inlet temperature of the evaporator is controlled to be 70°C, and the cold source outlet temperature is controlled to be 110°C;

[0092] Controlling the temperature of the gas phase outlet of the separator to be 100-110°C and the temperature of the liquid phase outlet to be 100-110°C;

[0093] Controlling the outlet temperature of the ammonia turbine generator set to 60-70° C.;

[0094] Control the heat source inlet temperature of the heat energy recovery device to be 50-60°C and the heat source outlet temperature to be 40-50°C;

[0095] The heat source inlet temperature of the liquid ammonia gasifier is controlled to be 40-50°C, the heat source outlet temperature is controlled to be 30-40°C, and the cold source outlet temperature is controlled to be 0-10°C.

[0096] In the integrated energy station in this comparative example, the ammonia content entering the evaporator is reduced because there is no ammonia water cooler, which reduces the absorption of heat on the hot side of the evaporator, reduces the amount of ammonia overflowing from the gas phase of the separator, and accordingly, the power generation of the ammonia turbine generator set is reduced. In addition, the temperature of the liquid phase loop solution of the separator increases, resulting in a weakening of the subsequent absorption process effect, which ultimately leads to an increase in the back pressure of the ammonia turbine generator set and reduces the output of the unit by 30% to 40%. The working condition of the ammonia water pump deteriorates and cavitation is prone to occur. The energy required to heat the liquid ammonia entering the ammonia energy center and evaporate it into ammonia requires additional consumption.

[0097] Comparative Example 2:

[0098] This comparative example provides an integrated energy station with ammonia working fluid coupled to fuel and an operation method thereof. The integrated energy station refers to the integrated energy station in Example 1, except that: the third heat exchange unit D is not included, that is, the heat source outlet of the heat energy recovery device is directly connected to the cold source inlet of the evaporator through the ammonia pump G. The structural schematic diagram is shown in FIG. Figure 3 shown.

[0099] The operation method of the above-mentioned integrated energy station includes:

[0100] Divide the liquid ammonia from the liquid ammonia tank into two streams;

[0101] The first stream of liquid ammonia is evaporated in the evaporator and then enters the separator to obtain gas phase and liquid phase; the separated gas phase enters the ammonia turbine generator set to generate electricity, and the gas phase after power generation enters the absorber to become liquid phase, and then enters the heat energy recovery device for heat exchange, and the liquid phase after heat exchange flows into the evaporator through the ammonia water pump G to form a cycle;

[0102] At the same time, the second stream of liquid ammonia enters the ammonia water cooler, and after heat exchange with the liquid phase from the separator, part of it flows into the evaporator, and the other part flows into the ammonia energy center I; while the liquid phase from the separator flows into the absorber after heat exchange;

[0103] The cold source inlet temperature of the evaporator is controlled to be 70°C, and the cold source outlet temperature is controlled to be 110°C;

[0104] Controlling the temperature of the gas phase outlet of the separator to be 100-110°C and the temperature of the liquid phase outlet to be 100-110°C;

[0105] Controlling the outlet temperature of the ammonia turbine generator set to 60-70° C.;

[0106] The heat source inlet temperature of the ammonia water cooler is controlled to be 100°C, the heat source outlet temperature is controlled to be 40°C, and the cold source outlet temperature is controlled to be 20°C;

[0107] The heat source inlet temperature of the heat energy recovery device is controlled to be 40-50°C, and the heat source outlet temperature is controlled to be 30-40°C.

[0108] The integrated energy station in this comparative example is limited by the ability of the heat recovery device to cool the ammonia working fluid. The back pressure of the ammonia turbine generator set increases, and the power generation output of the unit decreases by 20% to 30%. The working condition of the ammonia pump deteriorates, and cavitation is prone to occur. The energy required to heat and evaporate the liquid ammonia entering the ammonia energy center into ammonia gas requires additional consumption.

[0109] From the above embodiments and comparative examples, it can be seen that the integrated energy station of the present invention couples and optimizes the Kalina cycle power generation system with the ammonia energy system, thereby expanding the heat source recovery range, recovering low-temperature heat sources, realizing deep recovery of waste heat, and improving the thermoelectric conversion efficiency; the mechanical seal part of the ammonia turbine is greatly simplified, extending the maintenance cycle; the design is more flexible, providing diversified configurations to meet various customized needs; and the corresponding operating mode adjustment can be made for design deviations or long-term deviations of the unit from the original operating conditions; the working conditions of the ammonia pump of the key power equipment are improved, and the reliability is improved; liquid ammonia is used as a cold source for heat exchange, which increases the temperature of ammonia entering the ammonia energy center, optimizes the ammonia energy utilization process, and improves the utilization rate of ammonia resources.

[0110] The present invention illustrates the system and detailed method of the present invention through the above-mentioned embodiments, but the present invention is not limited to the above-mentioned system and detailed method, that is, it does not mean that the present invention must rely on the above-mentioned system and detailed method to be implemented. Those skilled in the art should understand that any improvement of the present invention, equivalent replacement of the operation of the present invention, addition of auxiliary operations, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

Claims

1. An integrated energy station with ammonia working fluid coupled with fuel, characterized in that: The integrated energy station includes a storage unit, an evaporation unit, a separation unit, a power generation unit, a first heat exchange unit, an absorption unit, a second heat exchange unit, a third heat exchange unit and an ammonia energy center; The evaporation unit, the separation unit, the power generation unit, the absorption unit, the second heat exchange unit and the third heat exchange unit are connected in a circular manner in sequence; the power generation unit and the third heat exchange unit are also independently connected to the ammonia energy center; The first heat exchange unit is independently connected to the storage unit, the evaporation unit, the separation unit, the absorption unit and the ammonia energy center; The storage unit is also independently connected to the evaporation unit and the second heat exchange unit.

2. The integrated energy station according to claim 1, characterized in that: The storage unit includes at least one liquid ammonia tank; The evaporation unit comprises at least one evaporator; The separation unit comprises at least one separator; The power generation unit includes at least one ammonia turbine generator set; The first heat exchange unit includes at least one ammonia water cooler; The absorption unit includes at least one absorber; The second heat exchange unit includes at least one heat energy recovery device; The third heat exchange unit includes at least one liquid ammonia vaporizer; The ammonia energy center includes any one of an ammonia boiler, an ammonia fuel cell, an ammonia gas turbine, an ammonia blending boiler, an ammonia charging device or an ammonia direct-fired lithium bromide refrigeration unit, or a parallel combination of at least two of them.

3. The integrated energy station according to claim 2, characterized in that: The cold source outlet of the evaporator is connected to the separator, the gas phase outlet of the separator is connected to the first liquid phase inlet of the absorber through the ammonia turbine generator set, the liquid phase outlet of the absorber is connected to the heat source inlet of the heat energy recovery device, the heat source outlet of the heat energy recovery device is connected to the heat source inlet of the liquid ammonia gasifier, and the heat source outlet of the liquid ammonia gasifier is connected to the cold source inlet of the evaporator through an ammonia water pump.

4. The integrated energy station according to claim 3, characterized in that: The ammonia turbine generator set is also connected to the ammonia energy center; The cold source outlet of the liquid ammonia gasifier is connected to the ammonia energy center.

5. The integrated energy station according to claim 3 or 4, characterized in that: The cold source inlet of the ammonia water cooler is connected to the liquid ammonia tank, the cold source outlet of the ammonia water cooler is respectively connected to the cold source inlet of the evaporator and the ammonia energy center, the heat source inlet of the ammonia water cooler is connected to the liquid phase outlet of the separator, and the heat source outlet of the ammonia water cooler is connected to the second liquid phase inlet of the absorber.

6. The integrated energy station according to claim 5, characterized in that: The liquid ammonia tank is independently connected to the cold source inlet of the evaporator and the cold source inlet of the liquid ammonia vaporizer.

7. The integrated energy station according to claim 3, characterized in that: A heat exchanger is arranged on the pipeline connecting the separator and the ammonia turbine generator set.

8. The integrated energy station according to claim 5, characterized in that: The pipelines connecting the ammonia energy center with the ammonia turbine generator set, the ammonia water cooler and the liquid ammonia gasifier are independently provided with turbine expansion devices.

9. An operating method of a comprehensive energy station according to any one of claims 1 to 8, characterized in that: The operation method comprises: Divide the liquid ammonia from the storage unit into three streams; The first stream of liquid ammonia is evaporated in the evaporation unit and then enters the separation unit to obtain a gas phase and a liquid phase; the separated gas phase enters the power generation unit to generate electricity, and the gas phase after power generation enters the absorption unit to become a liquid phase, and then successively passes through the second heat exchange unit and the third heat exchange unit for heat exchange, and the liquid phase after heat exchange flows into the evaporation unit to form a cycle; At the same time, the second stream of liquid ammonia enters the first heat exchange unit, and after heat exchange with the liquid phase from the separation unit, part of it flows into the evaporation unit, and the other part flows into the ammonia energy center; while the liquid phase from the separation unit flows into the absorption unit after heat exchange; At the same time, the third stream of liquid ammonia enters the third heat exchange unit, exchanges heat with the liquid phase from the second heat exchange unit, and then flows into the ammonia energy center.

10. The operating method according to claim 9, characterized in that: Control the cold source inlet temperature of the evaporation unit to be -20 to 80°C, and the cold source outlet temperature to be 80 to 160°C; Controlling the temperature of the gas phase outlet of the separation unit to be 80-160°C and the temperature of the liquid phase outlet to be 80-160°C; Controlling the outlet temperature of the power generation unit to be 50-100°C; Control the heat source inlet temperature of the first heat exchange unit to be 80-160°C, the heat source outlet temperature to be 10-50°C, and the cold source outlet temperature to be -20-50°C; Control the heat source inlet temperature of the second heat exchange unit to be 30-50°C and the heat source outlet temperature to be 20-40°C; The heat source inlet temperature of the third heat exchange unit is controlled to be 20-40°C, the heat source outlet temperature is controlled to be 10-30°C, and the cold source outlet temperature is controlled to be 0-10°C.

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