Propane dehydrogenation device waste heat recovery power generation system and method

Abstract

The present application relates to a kind of propane dehydrogenation device waste heat recovery power generation method and system, the present application combines hot water system and organic rankine cycle system to form closed loop power generation system, recycle multiple low-temperature waste heat in propane dehydrogenation device and utilize it, while guaranteeing process design requirement, with the advantages of recycling steam condensate, reducing device exhaust emission, improving process energy recovery rate and utilization efficiency;Multiple low-temperature waste heat mainly includes reactor vacuum exhaust gas low-temperature section in propane dehydrogenation device, reactor regeneration air tail gas and multiple process gas between product gas compressor section, the present application is more effective, extensive to the recovery of energy, can significantly reduce the consumption of circulating water and reduce exhaust emission, energy saving and emission reduction, economic and environmental protection.

Description

Technical Field

[0001] This invention relates to a method and system for waste heat recovery and power generation from a propane dehydrogenation unit. Background Technology

[0002] Propylene is an important organic chemical raw material with wide applications and high market demand. In recent years, with the rapid development of various industries such as chemical and manufacturing, the demand for propylene has continued to rise. With the development of propylene production technology and the commissioning of production facilities, propylene production capacity has grown rapidly. Compared with traditional petrochemical and coal chemical propylene production technologies, propane dehydrogenation technology has advantages such as lower project investment, higher product yield, lower production cost, wider raw material sources, and environmental friendliness, and has become a popular propylene synthesis process.

[0003] Currently, propane dehydrogenation processes with a high market share suffer from low heat recovery efficiency and significant energy waste in many areas. For example, in existing propane dehydrogenation units, the exhaust gas from reactor vacuum pumping and the tail gas from reactor regeneration are directly sent to the exhaust gas system after passing through a waste heat boiler, without any low-temperature waste heat recovery or utilization. Furthermore, in the product gas compressor section, multiple streams of process gas are used, and only a portion of these streams are heat-recovered using a warm water system, without comprehensive recovery and effective utilization of low-temperature heat. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to provide a method and system for waste heat recovery and power generation of propane dehydrogenation unit that can effectively recover low-temperature waste heat and improve energy utilization, in light of the current state of the technology.

[0005] The technical solution adopted by the present invention to solve the above-mentioned technical problems is as follows:

[0006] A method for recovering waste heat from a propane dehydrogenation unit to generate electricity includes the following steps:

[0007] (1) A warm water system is used for the first step of waste heat recovery. Warm water is used as the medium, and at least two heat exchangers are used to exchange heat with multiple medium and low temperature waste heat in the propane dehydrogenation unit. The warm water is heated and the process medium in the unit is cooled at the same time.

[0008] (2) The heated water is sent to the warm water cooler through the warm water tank and pressurized by the warm water pump. After cooling, it returns to the heat exchanger to realize the closed-loop circulation of the entire warm water system.

[0009] (3) The warm water cooler also serves as the evaporator in the organic Rankine cycle system. The organic working fluid is vaporized and superheated in the device using warm water as a heat source, and then enters the expander for expansion and power generation. The depressurized organic working fluid exhaust gas is condensed by the condenser and sent to the separation tank. Then, the organic working fluid is pressurized by the circulation pump and enters the warm water cooler, realizing the closed-loop operation of the entire organic Rankine cycle system.

[0010] Preferably, the operating conditions of the warm water working medium in the warm water system are an operating temperature of 60℃~130℃ and an operating pressure of 0.1~2.0MPaG. The warm water system uses warm water as the process medium to stably recover the low-temperature waste heat in the propane dehydrogenation unit. The operating equipment in the warm water system includes a heat exchanger, a warm water tank, a warm water pump, and a warm water cooler.

[0011] Preferably, in the warm water system, the inlet operating temperature of the multiple low-temperature waste heat process media is 100-180°C, and the outlet operating temperature is 70-100°C.

[0012] Preferably, the organic Rankine cycle system uses organic matter as the process medium and includes a water cooler, an expander, a generator, a condenser, a separator, and a circulating pump that are interconnected to form a power generation system.

[0013] Preferably, the process medium used in the organic Rankine cycle system is one or more of R245fa, R134a, R600a, isopentane, and n-pentane.

[0014] Preferably, the condenser's hot-side condensation operating temperature is -5 to 50°C, and the cold-side operating medium includes cooling water, cold water, ammonia, and propylene.

[0015] The heat exchanger type is selected from plate heat exchangers and high-efficiency heat exchangers.

[0016] Preferably, there are five heat exchangers connected in parallel. The heat source for the first heat exchanger is the product gas from the first stage outlet of the product gas compressor; the heat source for the second heat exchanger is the product gas from the second stage outlet of the product gas compressor; and the heat source for the third heat exchanger is the product gas from the third stage outlet of the product gas compressor. The flow rate for each heat exchanger is 190–232 t / h, and the operating temperature is 100–130°C. The heat source for the fourth heat exchanger is the reactor regeneration air tail gas after heat recovery, with a flue gas flow rate of 800–1000 t / h and an operating temperature of 100–180°C. The heat source for the fifth heat exchanger is the low-temperature section of the reactor vacuum exhaust gas after high-temperature heat recovery, with a flow rate of 28–34 t / h and an operating temperature of 100–180°C.

[0017] A waste heat recovery power generation system for a propane dehydrogenation unit includes:

[0018] A generator, connected to an expander, is used for expansion-based power generation;

[0019] A condenser, connected downstream of the expander, is used to receive the exhaust gas after the expander and condense it.

[0020] A separator, connected downstream of the condenser, is used to separate the fluid and transport the separated liquid phase downstream;

[0021] A warm water tank, which stores water after heat recovery;

[0022] A heat exchanger, connected to the warm water tank, includes at least two sets of devices for recovering heat from different gases to heat the water in the tank; and

[0023] The warm water cooler is equipped with a first inlet connected to the outlet of the warm water tank, a first outlet connected to the inlet of the heat exchanger, a second inlet connected to the outlet of the separator, and a second outlet connected to the expander. It is used to utilize the heat from the hot water output from the warm water tank to vaporize the working fluid for power generation and to cool the water circulating into the heat exchanger.

[0024] Preferably, the heat exchanger includes a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, and a fifth heat exchanger connected in parallel, with the inlet of each heat exchanger connected to the first outlet of the hot water cooler.

[0025] The aforementioned hot water cooler includes multiple sets of coolers connected in parallel.

[0026] Preferably, a warm water pump for providing water delivery power is provided between the outlet of the warm water tank and the first inlet of the warm water cooler;

[0027] A circulating pump is installed between the outlet of the separator and the second inlet of the warm water cooler to provide power for transporting the working fluid.

[0028] Compared with existing technologies, the advantages of this invention are as follows: This invention combines a warm water system and an organic Rankine cycle system to form a closed-loop power generation system, recovering and utilizing multiple streams of low-temperature waste heat from the propane dehydrogenation unit. While ensuring process design requirements, it has advantages such as recovering steam condensate, reducing unit exhaust gas emissions, improving process energy recovery rate and utilization efficiency, high safety, and stable process operation. The multiple streams of low-temperature waste heat mainly include the low-temperature section of the reactor vacuum exhaust gas in the propane dehydrogenation unit, the reactor regeneration air tail gas, and multiple streams of process gas between the product gas compressor section. This invention has more effective and extensive energy recovery, which can significantly reduce the consumption of circulating water and the amount of tail gas emissions, achieving energy conservation, emission reduction, and economic and environmental protection. Attached Figure Description

[0029] Figure 1 This is a process flow diagram of an embodiment of the present invention;

[0030] Figure 2 This is a process flow diagram of Comparative Example 1 of the present invention;

[0031] Figure 3 This is a process flow diagram of Comparative Example 2 of the present invention. Detailed Implementation

[0032] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments.

[0033] Example:

[0034] like Figure 1 As shown, the waste heat recovery and power generation method of the propane dehydrogenation unit in this embodiment includes the following steps:

[0035] (1) A warm water system is used for the first step of waste heat recovery. Warm water is used as the medium, and at least two heat exchangers are used to exchange heat with multiple medium and low temperature waste heat in the propane dehydrogenation unit. The warm water is heated and the process medium in the unit is cooled at the same time.

[0036] (2) The heated water is sent to the warm water cooler E-106 through the warm water tank V-101 and pressurized by the warm water pump P-101. After cooling, it returns to the heat exchanger to realize the closed-loop circulation of the entire warm water system.

[0037] (3) The warm water cooler E-106 also serves as the evaporator in the organic Rankine cycle system. The organic working fluid is vaporized and superheated in this device using warm water as a heat source, and then enters the expander T-201 for expansion and power generation. The depressurized organic working fluid exhaust gas is condensed by the condenser E-201 and sent to the separator V-201. Then, the organic working fluid is pressurized by the circulation pump P-201 and enters the warm water cooler E-106, realizing the closed-loop operation of the entire organic Rankine cycle system.

[0038] The operating conditions of the warm water system are: operating temperature 60℃~130℃, operating pressure 0.1~2.0MPaG. The warm water system uses warm water as the process medium to stably recover low-temperature waste heat from the propane dehydrogenation unit. The operating equipment in the warm water system includes a heat exchanger, a warm water tank, a warm water pump, and a warm water cooler. The inlet operating temperature of the multiple low-temperature waste heat process media in the warm water system is 100~180℃, and the outlet operating temperature is 70~100℃.

[0039] The organic Rankine cycle system uses organic matter as the process medium and includes interconnected components forming a power generation system: a warm water cooler E-106, an expander T-201, a generator X-201, a condenser E-201, a separator V-201, and a circulating pump P-201. The process medium used in the organic Rankine cycle system is one or more of R245fa, R134a, R600a, isopentane, and n-pentane.

[0040] The E-201 condenser operates at a hot-side condensing temperature of -5 to 50°C, and the cold-side operating media include cooling water, cold water, ammonia, propylene, etc. The heat exchanger type is selected from plate heat exchangers and high-efficiency heat exchangers.

[0041] In this embodiment, five heat exchangers are connected in parallel. The heat source for the first heat exchanger is the product gas from the first stage outlet of the product gas compressor; the heat source for the second heat exchanger is the product gas from the second stage outlet of the product gas compressor; and the heat source for the third heat exchanger is the product gas from the third stage outlet of the product gas compressor. The flow rate for each heat exchanger is 190–232 t / h, and the operating temperature is 100–130°C. The heat source for the fourth heat exchanger is the reactor regeneration air tail gas after heat recovery, with a flue gas flow rate of 800–1000 t / h and an operating temperature of 100–180°C. The heat source for the fifth heat exchanger is the low-temperature section of the reactor vacuum exhaust gas after high-temperature heat recovery, with a flow rate of 28–34 t / h and an operating temperature of 100–180°C.

[0042] The waste heat recovery power generation system of the propane dehydrogenation unit used in the above method includes:

[0043] Generator X-201, connected to expander T-201, is used for expansion power generation;

[0044] Condenser E-201, connected downstream of the expander, is used to receive the exhaust gas after the expander and condense it.

[0045] Separator V-201 is connected downstream of condenser E-201 and is used to separate the fluid and transport the separated liquid phase downstream.

[0046] The V-101 warm water tank stores water after heat recovery.

[0047] A heat exchanger, connected to a warm water tank V-101, includes at least two sets of heat recovery devices for heating water in the warm water tank V-101, which recover heat from different gases respectively.

[0048] The warm water cooler E-106 is equipped with a first inlet connected to the outlet of the warm water tank V-101, a first outlet connected to the inlet of the heat exchanger, a second inlet connected to the outlet of the separator V-201, and a second outlet connected to the expander T-201. It is used to utilize the heat from the hot water output from the warm water tank V-101 to vaporize the working fluid for power generation and to cool the water circulating into the heat exchanger.

[0049] The heat exchanger in this embodiment includes a first heat exchanger E-101, a second heat exchanger E-102, a third heat exchanger E-103, a fourth heat exchanger E-104, and a fifth heat exchanger E-105 connected in parallel. The inlet of each heat exchanger is connected to the first outlet of a hot water cooler E-106. The hot water cooler E-106 includes multiple sets of coolers connected in parallel.

[0050] A warm water pump P-101 is installed between the outlet of the warm water tank V-101 and the first inlet of the warm water cooler E-106 to provide power for water delivery; a circulating pump P-201 is installed between the outlet of the separator V-201 and the second inlet of the warm water cooler E-106 to provide power for transporting the working fluid.

[0051] Taking a 600,000-ton / year propane dehydrogenation unit as an example, the low-temperature waste heat sources in the unit mainly include the low-temperature section of the reactor vacuum exhaust gas, the reactor regeneration air tail gas, and multiple streams of process gas between the product gas compressor sections. Among them, the first, second, and third streams are the product gas outlets of the first, second, and third stages of the product gas compressor, respectively, with flow rates of approximately 190 t / h to 232 t / h and operating temperatures of 100℃ to 130℃. The fourth stream is the reactor vacuum exhaust gas, which has a relatively high outlet temperature. To improve energy utilization efficiency, it can be used to preheat fresh regenerated air or by-product low-pressure steam. Therefore, in this embodiment, the low-temperature section of the reactor vacuum exhaust gas after high-temperature heat recovery is used as the heat source, with a flow rate of 28-34 t / h and an operating temperature of 100-180°C. The fifth stream is the reactor regenerated air tail gas, which, after heat recovery, has a flue gas flow rate of 800-1000 t / h and an operating temperature of 100-180°C. Using the above five streams as heat sources, a warm water system and an organic Rankine cycle system are used to recover waste heat for power generation, and the process streams are cooled to 70-100°C.

[0052] The entire system employs a waste heat recovery power generation system combining a warm water system and an organic Rankine cycle system. The first step utilizes the warm water system, using warm water as the operating medium. The warm water first undergoes heat recovery through heat exchangers E-101 to E-105, with the operating temperature heated from 60-80℃ to 80-100℃. The heated water then passes through a warm water tank V-101, is pressurized by a warm water pump, and cooled to 60-80℃ by a warm water cooler E-106, thus completing the warm water system circulation. The operating pressure of the entire warm water system is between 0.1 and 2.0 MPaG. The warm water cooler E-106 can be operated in parallel, with 1 to 5 units depending on the heat exchange efficiency. Simultaneously, the warm water cooler E-106 also serves as the vaporizer for the organic medium in the organic Rankine cycle; in this embodiment, R134A is used as the operating medium for the organic Rankine cycle system. After gasification, the high-temperature and high-pressure organic working fluid operates under the following conditions: operating pressure 2.0–2.4 MPaG, operating temperature 75–80℃. It then enters an expander for expansion and power generation, with an expander efficiency of 85%. The exhaust gas from the expander operates at a temperature of 35–45℃ and a pressure of 0.8–1.1 MPaG. Cooling water at 25–45℃ or chilled water is condensed into a liquid phase in condenser E-201 and then pressurized to 2.0–2.4 MPaG by circulating pump P-201, thus achieving a closed-loop circulation of the entire organic Rankine cycle system.

[0053] Calculations show that when a 600,000-ton / year propane dehydrogenation unit adopts a waste heat recovery power generation system combining a warm water system and an organic Rankine cycle system, the heat recovered by the warm water system after the product gas from the first stage of the product gas compressor is cooled in the first heat exchanger E-101 is 4.3–5.2 MW; the heat recovered by the warm water system after the product gas from the second stage of the product gas compressor is cooled in the second heat exchanger E-102 is 4.0–4.9 MW; and the heat recovered by the warm water system after the product gas from the third stage of the product gas compressor is cooled in the third heat exchanger E-102 is 4.0–4.9 MW. After cooling, the heat recovered by the warm water system is 4.2–5.1 MW; after the reactor regeneration air exhaust gas is cooled in the fourth heat exchanger E-104, the heat recovered by the warm water system is 11.8–14.5 MW; after the reactor vacuum exhaust gas is cooled in the fifth heat exchanger E-105, the heat recovered by the warm water system is 18.7–22.8 MW. Therefore, after recovery by the warm water system, the energy recovered by the gasification of the organic medium in the warm water cooler E-106 is 43.0–52.6 MW. Taking the turbine expansion power generation efficiency as 85%, the waste heat recovery system can generate 3.5 MW–4.3 MW of electricity, with an energy conversion efficiency of 7.4%–9.1%. When the system heat exchange is adopted, 26.6–32.5 t / h of steam condensate from the reactor vacuum exhaust gas can be recovered, while reducing circulating water consumption by 3750–4550 t / h.

[0054] Meanwhile, for a 600,000-ton / year propane dehydrogenation unit, adopting a waste heat recovery system increases equipment investment by approximately RMB 15 million to 20 million, but it generates 28,000 MW to 34,400 MW of electricity annually, while recovering 213,000 to 260,000 tons of steam condensate per year and reducing circulating water consumption by 30 million to 36.4 million tons per year, resulting in economic benefits of approximately RMB 14.6 million to 17.9 million per year. Therefore, the waste heat recovery power generation system combining a warm water system and an organic Rankine cycle system in this embodiment not only has advantages such as stable process operation and low circulating water consumption, but also possesses the technical characteristics of waste heat recovery power generation, energy conservation, and emission reduction.

[0055] Comparative Example 1:

[0056] like Figure 2 As shown, this comparative example also employs a waste heat recovery power generation technology for a propane dehydrogenation unit combining a warm water system and an organic Rankine cycle system. First, a warm water system, using warm water as the medium, recovers waste heat from multiple streams of process gas between the product gas compressor sections in the propane dehydrogenation unit using heat exchangers 1-3 (E-101-E-103), heating the warm water. The heated water then passes through a warm water tank (V-101) and is pressurized by a warm water pump (P-101) before being sent to a warm water cooler (E-106) for cooling, thus achieving a closed-loop circulation of the entire warm water system. The organic Rankine cycle system employs a multi-stage expansion power generation scheme based on different heat sources and evaporation temperatures. The organic working fluid, after being pressurized by a circulation pump (P-201), is divided into three streams that go to the warm water cooler (E-106), heat exchanger (E-202), and heat exchanger (E-203) respectively for vaporization and evaporation. Because heat exchangers E-202 and E-203 use regenerated air exhaust gas and reactor vacuum exhaust gas for direct heat exchange, respectively, the organic working fluid has a high vaporization temperature and evaporation pressure. After vaporization, it first enters the first stage of expander T-201-1, and after expansion, it mixes with the working fluid at the outlet of warm water cooler E-106 in the second stage of expander T-201-2. The exhaust gas after expansion and power generation is condensed by condenser E-201 and sent to separator V-201. Subsequently, the organic working fluid is circulated by a circulation pump to realize the closed-loop system of the entire organic Rankine cycle system.

[0057] In this comparative example, steam condensate can also be recovered, realizing the recovery of low-temperature waste heat in the device. However, compared with the above embodiments, there may be slightly worse energy recovery and power generation efficiency, and slightly lower stability of the propane dehydrogenation device. Therefore, it is necessary to consider the utilization of the two heat sources, regenerated air tail gas and reactor vacuum exhaust gas, and to add a compressor and consider the heat exchange problem between compressor sections.

[0058] Comparative Example 2:

[0059] like Figure 3As shown, this comparative example directly employs an organic Rankine cycle system for waste heat recovery and power generation technology in a propane dehydrogenation unit. Using organic matter as the medium, heat exchangers 1 to 5 (E-101 to E-105) are used to exchange heat at multiple locations in the propane dehydrogenation unit at medium and low temperatures. While cooling the process medium in the unit, the organic matter is also vaporized. The vaporized organic matter is then expanded and used for power generation via expander T-201. The depressurized organic working fluid exhaust gas is condensed by condenser E-201 and sent to separator V-201. Subsequently, the organic working fluid is pressurized by circulating pump P-201 and returned to the vaporization process, thus realizing a closed-loop system for the entire organic Rankine cycle.

[0060] In this comparative example, steam condensate can also be recovered, realizing the recovery of low-temperature waste heat in the unit. However, directly using organic Rankine cycle technology requires high stability of the power generation system, and it is also necessary to minimize the impact of the instability of the organic Rankine cycle system on the operation of the propane dehydrogenation unit.

Claims

1. A method for recovering waste heat from a propane dehydrogenation unit to generate electricity, characterized in that... Includes the following steps: (1) A warm water system is used for the first step of waste heat recovery. With warm water as the medium, five heat exchangers are used to exchange heat on multiple medium and low temperature waste heat in the propane dehydrogenation unit, heating the warm water and cooling the process medium in the unit at the same time. (2) The heated water is sent to the warm water cooler (E-106) by the warm water tank (V-101) and the warm water pump (P-101) after being pressurized. After being cooled, it returns to the heat exchanger to realize the closed-loop circulation of the entire warm water system. (3) The warm water cooler (E-106) also serves as the evaporator in the organic Rankine cycle system. The organic working fluid is vaporized and superheated in the warm water cooler with warm water as the heat source, and then enters the expander (T-201) for expansion and power generation. The depressurized organic working fluid exhaust gas is condensed by the condenser (E-201) and sent to the separator (V-201). Then, the organic working fluid is pressurized by the circulation pump (P-201) and enters the warm water cooler (E-106), thus realizing the closed-loop operation of the entire organic Rankine cycle system. The heat exchangers consist of five units connected in parallel. The heat source for the first heat exchanger is the product gas from the first stage outlet of the product gas compressor; the heat source for the second heat exchanger is the product gas from the second stage outlet of the product gas compressor; and the heat source for the third heat exchanger is the product gas from the third stage outlet of the product gas compressor. The flow rate for each heat exchanger is 190~232 t / h, and the operating temperature is 100~130℃. The heat source for the fourth heat exchanger is the reactor regeneration air tail gas after heat recovery, with a flue gas flow rate of 800~1000 t / h and an operating temperature of 100~180℃. The heat source for the fifth heat exchanger is the low-temperature section of the reactor vacuum exhaust gas after high-temperature heat recovery, with a flow rate of 28~34 t / h and an operating temperature of 100~180℃.

2. The method for waste heat recovery and power generation from a propane dehydrogenation unit according to claim 1, characterized in that: The operating conditions of the warm water working medium in the aforementioned warm water system are: operating temperature 60℃~130℃, operating pressure 0.1~2.0MPaG.

3. The method for waste heat recovery and power generation from a propane dehydrogenation unit according to claim 2, characterized in that: In the aforementioned warm water system, the inlet operating temperature of the multiple low-temperature waste heat process media is 100~180℃, and the outlet operating temperature is 70~100℃.

4. The method for waste heat recovery and power generation from a propane dehydrogenation unit according to claim 1, characterized in that: The organic Rankine cycle system uses organic matter as the process medium and includes a water cooler (E-106), an expander (T-201), a generator (X-201), a condenser (E-201), a separator (V-201), and a circulation pump (P-201) that are interconnected to form a power generation system.

5. The method for waste heat recovery and power generation from a propane dehydrogenation unit according to claim 4, characterized in that: The organic Rankine cycle system uses one or more of the following as process media: R245fa, R134a, R600a, isopentane, and n-pentane.

6. The method for waste heat recovery and power generation from a propane dehydrogenation unit according to claim 1, characterized in that: The condenser (E-201) described above has a hot-side condensation operation temperature of -5 to 50°C, and the cold-side operating medium includes cooling water, cold water, ammonia, propylene, etc. The heat exchanger type is selected from plate heat exchangers and high-efficiency heat exchangers.

7. A waste heat recovery power generation system for a propane dehydrogenation unit, characterized in that, The method for waste heat recovery and power generation from a propane dehydrogenation unit according to any one of claims 1 to 6 comprises: The generator (X-201) is connected to the expander (T-201) for expansion power generation; A condenser (E-201), connected downstream of the expander (T-201), is used to receive the exhaust gas after passing through the expander (T-201) and condense it. The separator (V-201), connected downstream of the condenser (E-201), is used to separate the fluid and transport the separated liquid phase downstream; The warm water tank (V-101) stores water after heat recovery; A heat exchanger, connected to the warm water tank (V-101), includes at least two sets of heat exchangers that recover heat from different gases to heat the water in the warm water tank (V-101); and The warm water cooler (E-106) is equipped with a first inlet connected to the outlet of the warm water tank (V-101), a first outlet connected to the inlet of the heat exchanger, a second inlet connected to the outlet of the separator (V-201), and a second outlet connected to the expander (T-201). It is used to use the heat from the hot water output from the warm water tank (V-101) to vaporize the working fluid for power generation and to cool the water circulating into the heat exchanger. The heat exchangers include a first heat exchanger (E-101), a second heat exchanger (E-102), a third heat exchanger (E-103), a fourth heat exchanger (E-104), and a fifth heat exchanger (E-105) connected in parallel. The inlet of each heat exchanger is connected to the first outlet of the hot water cooler (E-106). The aforementioned hot water cooler (E-106) includes multiple sets of coolers connected in parallel. A warm water pump (P-101) for providing water delivery power is provided between the outlet of the warm water tank (V-101) and the first inlet of the warm water cooler; A circulating pump (P-201) for providing power for transporting the working fluid is provided between the outlet of the separator (V-201) and the second inlet of the warm water cooler (E-106).

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