Steam-saving temperature and pressure reducing device

Abstract

The steam-saving type temperature and pressure reduction device comprises a steam jet device, a flash tank and a condensation pump, the steam jet device comprises a jet device body, a high-pressure inlet, a low-pressure outlet, a low-pressure inlet and an outlet bypass pipe, and the high-pressure inlet, the low-pressure outlet, the low-pressure inlet and the outlet bypass pipe are arranged on the jet device body; the flash tank comprises a flash tank body, and a flash tank inlet, a flash tank outlet and a condensed water outlet which are formed in the flash tank body; the condensation pump comprises a condensation pump body, a condensation pump inlet and a condensation pump outlet, wherein the condensation pump inlet and the condensation pump outlet are formed in the condensation pump body. According to the invention, the pressure energy from high pressure to low pressure is utilized to pump a large amount of flash steam generated by condensate water with the temperature of about 100 DEG C on site, the high-pressure steam and the flash steam are mixed and then form low-pressure steam to the downstream, and due to the addition of the flash steam, less high-pressure steam can be used under the condition that the demand quantity of downstream steam is certain, so that the energy consumption is reduced. And the same amount of low-pressure steam is formed, so that the aim of saving energy is fulfilled.

Description

Technical Field

[0001] The invention relates to the technical field of temperature reduction and pressure reduction equipment, and in particular discloses a steam-saving temperature reduction and pressure reduction device. Background Art

[0002] As the name suggests, the desuperheater / pressure reducer / device reduces high-temperature and high-pressure steam to low-pressure and low-temperature steam (which can be superheated steam) that can be used by customers.

[0003] In some factories, boilers or certain workstations produce high-pressure steam. However, most production processes require low-pressure steam, as high-pressure steam transfers heat less effectively than low-pressure steam. Using high-pressure steam on equipment that requires low pressure wastes significant energy and poses safety risks. Therefore, to protect equipment and conserve energy, steam pressure must be reduced to the required level.

[0004] For example, the steam generated by the boiler passes through the superheater outlet to the steam turbine to perform work. The turbine has a certain range of steam parameters. If the steam parameters at the superheater outlet exceed the upper limit required by the turbine, it will cause damage to the turbine. Therefore, a desuperheater / desuperheater / desuperheater device must be used to reduce the parameters to within the applicable range.

[0005] Currently, there are two solutions to this problem in the industry:

[0006] 1. Reduce steam temperature and pressure through general desuperheater and pressure reducer

[0007] like Figure 1 As shown, a typical attemperator and pressure reducer includes a pressure reducing valve 1. Essentially, a typical attemperator and pressure reducer reduces steam pressure by closing the pressure reducing valve. The steam temperature remains unchanged and may even increase due to heat loss from the valve. After pressure reduction, the steam becomes low-pressure, superheated steam. A small amount of water is then added after the valve, allowing this water to absorb the heat from the superheated steam and vaporize into saturated steam at that pressure. Simultaneously, the superheated steam, having absorbed the heat from the superheating, becomes low-pressure, saturated steam. While reducing steam pressure with an attemperator and pressure reducing valve is feasible, it also has numerous drawbacks. Reducing steam pressure with an attemperator and pressure reducing valve can degrade steam quality and reduce its ability to perform work.

[0008] 2. Energy recovery through back-pressure steam turbine generator sets

[0009] like Figure 2As shown, a back-pressure steam turbine generator set includes a steam turbine 2 and a generator 3. Steam drives steam turbine 2, which is directly connected to generator 3 to generate electricity. The generated electricity is then connected to the grid and fed into the nearest power distribution system within the plant for grid use. The high-pressure steam is converted to low-pressure steam after work in the turbine impeller and then used in the required process. Replacing the steam attemperator and pressure reducing valve with a steam turbine generator set, utilizing the pressure energy consumed by the steam turbine for power generation, is also feasible. However, this presents several challenges. a) The system is complex and costly. In addition to the steam turbine, a generator, grid-connected equipment, and even a dedicated distribution room are required, resulting in high costs. b) The more complex the system, the higher the failure rate. c) Grid-connected power generation requires approval and unified management by the power management department, and there are also administrative costs, which reduces the actual return on investment. d) For many companies, not only must capacity recovery be considered, but more importantly, plant-wide steam balance must be considered. Replacing conventional attemperator and pressure reducing valves with steam turbine generator sets will inevitably increase steam consumption, leading to an increase in the upstream high-pressure steam supply.

[0010] Therefore, the above-mentioned defects of the existing temperature reduction and pressure reduction devices are technical problems that need to be solved urgently. Summary of the Invention

[0011] The present invention provides a steam-saving temperature and pressure reduction device, which aims to solve the above-mentioned defects of the existing temperature and pressure reduction devices.

[0012] The present invention relates to a steam-saving temperature and pressure reduction device, comprising:

[0013] The steam ejector includes an ejector body, a high-pressure inlet, a low-pressure outlet, a low-pressure inlet, and an outlet bypass pipe provided on the ejector body. The high-pressure inlet is used to connect to the high-pressure steam inlet, and the low-pressure outlet is used to connect to the flash steam; the outlet bypass pipe is used to connect to the desuperheated water; the low-pressure outlet is used to output the low-pressure steam after the ejection in the steam ejector is completed;

[0014] The flash tank includes a flash tank body, a flash tank inlet, a flash tank outlet, and a condensed water outlet provided on the flash tank body; the flash tank outlet is connected to the low-pressure outlet for outputting the flash steam after the flash evaporation in the flash tank is completed; the flash tank inlet is used to receive high-temperature condensed water on site, and the condensed water outlet is used to output the condensed water after the flash evaporation in the flash tank is completed;

[0015] The condensate pump includes a condensate pump body, and a condensate pump inlet and a condensate pump outlet arranged on the condensate pump body. The condensate pump inlet is connected to the condensate outlet, and the condensate pump outlet is used to output the condensate after condensation in the condensate pump is completed.

[0016] Furthermore, the steam-saving type cooling and pressure reducing device also includes a control system, which includes a first pressure collection module arranged at the inlet of the high-pressure inlet for collecting the high-pressure steam pressure of the cooling and pressure reducing inlet, a first temperature collection module for collecting the temperature of the high-pressure steam at the cooling and pressure reducing inlet, and a first mass collection module for collecting the quality of the high-pressure steam at the cooling and pressure reducing inlet; the control system also includes a second pressure collection module arranged at the outlet of the low-pressure outlet for collecting the low-pressure steam pressure of the cooling and pressure reducing outlet, a second temperature collection module for collecting the temperature of the low-pressure steam at the cooling and pressure reducing outlet, and a second mass collection module for collecting the quality of the low-pressure steam at the cooling and pressure reducing outlet; the control system also includes a third pressure collection module arranged at the inlet of the outlet bypass pipe for collecting the cooling water inlet pressure, a third temperature collection module for collecting the cooling water inlet temperature, and a third mass collection module for collecting the cooling water inlet quality; the control system also includes a fourth pressure collection module arranged at the inlet of the low-pressure inlet for collecting the flash steam pressure of the flash steam inlet, a fourth temperature collection module for collecting the flash steam temperature of the flash steam inlet, and a fourth mass collection module for collecting the flash steam quality of the flash steam inlet.

[0017] Furthermore, the control system also includes a controller, which is connected to the first pressure acquisition module, the first temperature acquisition module, the first mass acquisition module, the second pressure acquisition module, the second temperature acquisition module, the second mass acquisition module, the third pressure acquisition module, the third temperature acquisition module, the third mass acquisition module, the fourth pressure acquisition module, the fourth temperature acquisition module and the fourth mass acquisition module respectively, and is used to collect the high-pressure steam temperature of the cooling and decompression inlet collected by the first pressure acquisition module, the high-pressure steam temperature of the cooling and decompression inlet collected by the first temperature acquisition module, the mass of the high-pressure steam of the cooling and decompression inlet collected by the first mass acquisition module, and the high-pressure steam temperature of the cooling and decompression inlet collected by the second pressure acquisition module. The high-pressure steam flow rate at the ejector inlet is calculated based on the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0018] Furthermore, the high-pressure steam flow rate at the steam ejector inlet is calculated using the mass balance formula:

[0019] m2=m L +m w +m1

[0020] Among them, m2 is the mass flow rate of low-pressure steam at the outlet of the steam ejector, m L is the evaporation capacity of the flash tank, m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet, m w The amount of water added to reduce the temperature.

[0021] Furthermore, the controller is also used to calculate the amount of condensed water flowing out of the flash tank based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0022] Furthermore, the amount of condensed water flowing out of the flash tank is calculated using the following formula:

[0023] m s ′=m s -m L

[0024] Among them, m s ′ is the amount of condensed water flowing out of the flash tank, m s is the amount of high-temperature condensed water flowing into the flash tank; m L is the evaporation capacity of the flash tank.

[0025] Furthermore, the controller is also used to calculate the flash steam volume of the flash evaporator based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0026] Furthermore, the amount of condensed water flowing out of the flash tank is calculated using the following formula:

[0027]

[0028] Among them, m L is the evaporation capacity of the flash tank, m s is the amount of high-temperature condensed water flowing into the flash tank, h s is the specific enthalpy of the high-temperature condensed water flowing into the flash tank, h L is the specific enthalpy of the high-temperature condensed water flowing into the flash tank, h s ′ is the specific enthalpy of the condensed water flowing out of the flash tank.

[0029] Furthermore, the controller is also used to calculate the entropy increase and recovered energy of the isolated system using the entropy increase equation of the isolated system based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0030] Furthermore, the entropy increase of an isolated system is calculated by the following formula:

[0031] ΔS′=-(m1-m L )(s2-s1)+m w (s2-s w )+m L (s2-s L )

[0032] =-m1(s2-s1)+m L (s2-s1)+m w (s2-s w )+m L (s2-s L )

[0033] Where ΔS′ represents the entropy increase of the isolated system when the condensed water flash steam is extracted by the jet device, m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet, m L is the evaporation capacity of the flash tank, s2 is the specific entropy of the high-pressure steam entering the desuperheater, s1 is the specific entropy of the high-pressure steam entering the desuperheater, mw is the amount of cooling water added; s w is the specific entropy of the desuperheating water entering the desuperheating and pressure reducing device, s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer;

[0034] The recovered energy is calculated using the following formula:

[0035] ΔI=m L (2s2-s1-s L )*T0

[0036] Where ΔI represents the loss of the ability to pump condensed water and flash steam using the jet device, m L is the evaporation capacity of the flash tank, s1 is the specific entropy of the high-pressure steam entering the desuperheater, s2 is the specific entropy of the low-pressure steam leaving the desuperheater, s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer, and T0 is the ambient thermodynamic temperature.

[0037] The beneficial effects achieved by the present invention are:

[0038] The present invention provides a steam-saving temperature-reducing and pressure-reducing device, which utilizes a steam ejector, a flash tank, and a condensate pump. The steam ejector comprises an ejector body, a high-pressure inlet, a low-pressure outlet, and a low-pressure inlet and outlet bypass pipe provided on the ejector body; the flash tank comprises a flash tank body, a flash tank inlet, a flash tank outlet, and a condensate outlet provided on the flash tank body; and the condensate pump comprises a condensate pump body, a condensate pump inlet, and a condensate pump outlet provided on the condensate pump body. The steam-saving temperature-reducing and pressure-reducing device provided by the present invention utilizes the pressure energy of reducing high pressure to low pressure to pump flash steam generated by a large amount of condensate at about 100°C on-site. The high-pressure steam and flash steam are mixed and then flow downstream to form low-pressure steam. Due to the addition of flash steam, under the condition of a certain downstream steam demand, less high-pressure steam can be used to form the same amount of low-pressure steam, thereby achieving the purpose of energy saving. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 It is a structural diagram of an existing general temperature and pressure reducing device;

[0040] Figure 2 It is a structural diagram of an existing back-pressure steam turbine generator set;

[0041] Figure 3 Schematic diagram of the structure of the steam-saving temperature and pressure reduction device of the present invention;

[0042] Figure 4 It is a schematic diagram of the isolated system of the ejector in the steam-saving temperature and pressure reduction device of the present invention.

[0043] Description of Figure Numbers:

[0044] 10. Steam ejector; 20. Flash tank; 30. Condensate pump; 11. Ejector body; 12. High-pressure inlet; 13. Low-pressure outlet; 14. Low-pressure inlet; 15. Outlet bypass pipe; 21. Flash tank body; 22. Flash tank inlet; 23. Flash tank outlet; 24. Condensate outlet; 31. Condensate pump body; 32. Condensate pump inlet; 33. Condensate pump outlet. DETAILED DESCRIPTION

[0045] In order to better understand the above technical solution, the above technical solution will be described in detail below with reference to the accompanying drawings and specific implementation methods.

[0046] like Figure 3 and Figure 4 As shown, the present invention proposes a steam-saving type temperature and pressure reduction device, including a steam ejector 10, a flash tank 20 and a condensate pump 30, wherein the steam ejector 10 includes an ejector body 11, and a high-pressure inlet 12, a low-pressure outlet 13, a low-pressure inlet 14 and an outlet bypass pipe 15 provided on the ejector body 11, the high-pressure inlet 12 is used to connect the high-pressure steam, the low-pressure outlet 13 is used to connect the flash steam; the outlet bypass pipe 15 is used to connect the temperature-reducing water; the low-pressure outlet 14 is used to output the low-pressure steam after the ejection in the steam ejector 10 is completed; the flash tank 20 includes a flash tank body 21, and a flash tank body 22 provided on the flash tank body 23. The flash tank inlet 22, flash tank outlet 23 and condensed water outlet 24 on the evaporator body 21; the flash tank outlet 23 is connected to the low-pressure outlet 13 for outputting the flash steam after the flash evaporation in the flash tank 20 is completed; the flash tank inlet 22 is used to access the high-temperature condensed water on site, and the condensed water outlet 24 is used to output the condensed water after the flash evaporation in the flash tank 20 is completed; the condensate pump 30 includes a condensate pump body 31, and a condensate pump inlet 32 ​​and a condensate pump outlet 33 provided on the condensate pump body 31, the condensate pump inlet 32 ​​is connected to the condensed water outlet 24, and the condensate pump outlet 33 is used to output the condensed water after the condensation in the condensate pump 30 is completed.

[0047] The steam-saving, temperature-reducing and pressure-reducing device proposed in this embodiment directs the high-pressure steam originally connected to the temperature-reducing and pressure-reducing gas inlet to the high-pressure inlet 12 of the steam ejector 10, and the low-pressure steam originally connected to the temperature-reducing and pressure-reducing outlet to the low-pressure outlet 13 of the steam ejector 10. High-temperature condensate from the site is connected to the flash tank inlet 22 of the flash evaporator flash tank 20, and the flash tank outlet of the flash tank 20 is connected to the low-pressure inlet 13 of the steam ejector 10. The flashed condensate outlet 24 of the flash tank 20 is connected to the condensate pump inlet 32 ​​of the condensate pump 30, which then pumps the condensate to the storage tank or pipeline specified by the process. The temperature-reducing water originally connected to the temperature-reducing and pressure-reducing valve is now connected to the outlet bypass pipe 15 of the steam ejector 10.

[0048] In the above structure, see Figure 3 and Figure 4 The steam-saving type temperature reduction and pressure reduction device provided in this embodiment further includes a control system, which includes a first pressure acquisition module provided at the inlet of the high-pressure inlet 12 for collecting the pressure of the high-pressure steam at the temperature reduction and pressure reduction inlet, a first temperature acquisition module for collecting the temperature of the high-pressure steam at the temperature reduction and pressure reduction inlet, and a first quality acquisition module for collecting the quality of the high-pressure steam at the temperature reduction and pressure reduction inlet; the control system also includes a second pressure acquisition module provided at the outlet of the low-pressure outlet 13 for collecting the pressure of the low-pressure steam at the temperature reduction and pressure reduction outlet, a second temperature acquisition module for collecting the temperature of the low-pressure steam at the temperature reduction and pressure reduction outlet, and The control system further includes a second mass acquisition module for acquiring the quality of the low-pressure steam at the outlet of the desuperheating and pressure reduction device. The control system also includes a third pressure acquisition module, located at the inlet of the outlet bypass pipe 15, for acquiring the desuperheating water inlet pressure, a third temperature acquisition module, for acquiring the desuperheating water inlet temperature, and a third mass acquisition module, for acquiring the desuperheating water inlet quality. The control system also includes a fourth pressure acquisition module, located at the inlet of the low-pressure inlet 14, for acquiring the flash steam pressure at the flash steam inlet, a fourth temperature acquisition module, for acquiring the flash steam temperature at the flash steam inlet, and a fourth mass acquisition module, for acquiring the flash steam quality at the flash steam inlet. The steam-saving desuperheating and pressure reduction device provided in this embodiment uses corresponding pressure acquisition modules, temperature acquisition modules, and quality acquisition modules to acquire pressure data, temperature data, and quality data, and has a high degree of automation.

[0049] Further, see Figure 3 and Figure 4 The steam-saving type temperature and pressure reduction device provided in this embodiment further comprises a control system, which is connected to the first pressure acquisition module, the first temperature acquisition module, the first mass acquisition module, the second pressure acquisition module, the second temperature acquisition module, the second mass acquisition module, the third pressure acquisition module, the third temperature acquisition module, the third mass acquisition module, the fourth pressure acquisition module, the fourth temperature acquisition module and the fourth mass acquisition module respectively, and is used to collect the temperature of the high-pressure steam at the temperature reduction and pressure reduction inlet collected by the first pressure acquisition module, the temperature of the high-pressure steam at the temperature reduction and pressure reduction inlet collected by the first temperature acquisition module, and the temperature of the high-pressure steam at the temperature reduction and pressure reduction inlet collected by the first mass acquisition module. The high-pressure steam flow rate at the ejector inlet is calculated based on the following parameters: mass, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure acquisition module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature acquisition module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass acquisition module, the cooling water inlet pressure collected by the third pressure acquisition module, the cooling water inlet temperature collected by the third temperature acquisition module, the cooling water inlet mass collected by the third mass acquisition module, the flash steam pressure at the flash steam inlet collected by the fourth pressure acquisition module, the flash steam temperature at the flash steam inlet collected by the fourth temperature acquisition module and the flash steam mass at the flash steam inlet collected by the fourth mass acquisition module.

[0050] Specifically, the steam-saving temperature and pressure reduction device provided in this embodiment has a control system that specifies the following operating parameters:

[0051] 1) The higher the on-site condensate temperature, the better. If necessary, the pipes leading to the condensate should be well insulated. Generally, it should be greater than 100°C.

[0052] 2) The flash temperature in the flash tank 20 is maintained at 70-90°C (corresponding to a saturated pressure of 0.0312MPa-0.0701MPa). If the temperature is too high, the amount of flash steam is small, and if the temperature is too low, the jet device cannot be driven. The pressure in the flash tank 20 is the saturated pressure corresponding to the temperature.

[0053] 3) The parameters of the high-pressure steam at the high-pressure inlet 12 of the steam ejector 10 should be consistent with those of the original desuperheater and pressure reducer, and the flow rate should conform to the following mass balance formula. The high-pressure steam flow rate at the steam ejector inlet is calculated using the mass balance formula:

[0054] m2=m L +m w +m1 (1)

[0055] In formula (1), m2 is the mass flow rate of low-pressure steam at the steam ejector outlet, in kg / h; m L is the flash tank evaporation capacity (obtained in the flash tank calculation), in kg / h; m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet (provided by the ejector manufacturer), in kg / h; m w It is the amount of cooling water added, which is equal to the amount of cooling water added by the original cooling and pressure reducing device, and the unit is kg / h.

[0056] Preferably, see Figure 3 and Figure 4 The steam-saving cooling and pressure reduction device provided in this embodiment has a controller that is further used to calculate the amount of condensed water flowing out of the flash tank based on the high-pressure steam temperature at the cooling and pressure reduction inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and pressure reduction inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and pressure reduction inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and pressure reduction outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and pressure reduction outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and pressure reduction outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0057] Specifically, see Figure 3 and Figure 4 In the steam-saving temperature and pressure reduction device provided in this embodiment, the amount of condensed water flowing out of the flash tank is equal to the flow rate of the condensate pump. The amount of condensed water flowing out of the flash tank is calculated by the following formula:

[0058] m s ′=m s -m L (2)

[0059] In formula (2), m s ' is the amount of condensed water flowing out of the flash tank (the flow rate of the condensate pump), in kg / h; m s is the amount of high-temperature condensed water flowing into the flash tank, in kg / h; m L It is the evaporation capacity of the flash tank, obtained in the flash evaporator calculation, and the unit is kg / h.

[0060] Preferably, see Figure 3 and Figure 4 The steam-saving type cooling and decompression device provided in this embodiment has a controller that is further used to calculate the flash steam volume of the flash evaporator based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0061] Specifically, see Figure 3 and Figure 4 In the steam-saving temperature and pressure reduction device provided in this embodiment, the amount of condensed water flowing out of the flash tank is calculated using the following formula:

[0062]

[0063] In formula (3), m L is the evaporation capacity of the flash tank, in kg / h; m s is the amount of high-temperature condensed water flowing into the flash tank, which is the amount of all available high-temperature condensed water on site obtained through on-site investigation, in kg / h; h sis the specific enthalpy of the high-temperature condensed water flowing into the flash tank, which is obtained from the "Water Vapor Thermodynamic Properties Chart" based on the on-site investigation of the temperature and pressure of the high-temperature condensed water flowing into the flash tank. The unit is kJ / kg; h L The specific enthalpy of the high-temperature condensed water flowing into the flash tank is obtained from the "Water Vapor Thermodynamic Properties Chart" according to its temperature and pressure. It has been stipulated that its temperature is 70-90℃. Generally, it is 80℃. After determining its temperature, the pressure is the saturation pressure corresponding to the temperature, and the unit is kJ / kg; h s ′ is the specific enthalpy of the condensed water flowing out of the flash tank. Its temperature and pressure are consistent with the temperature and pressure of the evaporating steam in the flash evaporator, but the specific enthalpy is found according to the condensed water in the "Water Vapor Thermodynamic Properties Diagram" and the unit is kJ / kg.

[0064] Further, see Figure 3 and Figure 4 The steam-saving cooling and pressure reduction device provided in this embodiment is further configured to use the isolated system entropy increase equation to calculate the entropy increase and recovered energy of the isolated system based on the high-pressure steam temperature at the cooling and pressure reduction inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and pressure reduction inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and pressure reduction inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and pressure reduction outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and pressure reduction outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and pressure reduction outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

[0065] Specifically, see Figure 3 and Figure 4 The steam-saving temperature and pressure reduction device provided in this embodiment is based on production requirements and the principle that the downstream (low-pressure steam) quality remains unchanged. The entropy increase of the isolated system is calculated using the entropy increase equation of the isolated system:

[0066] ΔS′=-(m1-m L )(s2-s1)+m w (s2-s w )+m L (s2-s L )

[0067] =-m1(s2-s1)+m L (s2-s1)+m w (s2-s w )+m L (s2-sL ) (4)

[0068] In formula (4), ΔS′ represents the entropy increase of the isolated system when the flash steam of condensed water is extracted by the ejector device, and the symbol “′” represents the difference between the entropy increase of the isolated system and the conventional desuperheating and pressure reduction device, and the unit is kg / h; m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet (provided by the ejector manufacturer), and the unit is kg / h; m L is the evaporation capacity of the flash tank (obtained in the flash evaporator calculation), the unit is kg / h; s2 is the specific entropy of the high-pressure steam entering the desuperheater, which is obtained from P2 and T2 in the "Water Vapor Thermodynamic Properties Chart", the unit is kJ / (kg.K); s1 is the specific entropy of the high-pressure steam entering the desuperheater, which is obtained from P1 and T1 in the "Water Vapor Thermodynamic Properties Chart", the unit is kJ / (kg.K), m w The amount of cooling water added is equal to the amount of cooling water added by the original cooling and pressure reducing device, and the unit is kg / h; s w is the specific entropy of the desuperheating water entering the desuperheater and pressure reducer, which can be found from pw and Tw in the "Thermodynamic Properties of Water Vapor" chart, and the unit is kJ / (kg.K); s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer, and is given by P L 、T L It can be found in the "Thermodynamic Properties Diagram of Water Vapor" that it is kJ / (kg.K).

[0069] In the "Water Steam Thermodynamic Properties Diagram", S1 can be found through P1 and T1, S2 can be found through P2 and T2; S W , and then calculate the entropy increment:

[0070] ΔS=-m1(s2-s1)+m w (s2-s w ) (5)

[0071] In formula (5), ΔS is the entropy increase of the desuperheater as an isolated system, with the unit of kJ / K; m1 is the mass of steam entering the desuperheater, which is determined by the production process and the unit is kg; s1 is the specific entropy of steam entering the desuperheater, which is obtained from P1 and T1 in the "Water Steam Thermodynamic Properties Chart" and the unit is kJ / (kg.K); s2 is the specific entropy of steam leaving the desuperheater, which is obtained from P2 and T2 in the "Water Steam Thermodynamic Properties Chart" and the unit is kJ / (kg.K); m w The mass of the cooling water for cooling and reducing pressure is determined by the upstream and downstream processes, and the unit is kg; s w It is the specific entropy of the cooling water entering the cooling and pressure reducing device, which can be found from pw and Tw in the "Water Vapor Thermodynamic Properties Diagram" and the unit is kJ / (kg.K).

[0072] So the equation can be written as:

[0073] ΔS′=ΔS+m L (2s2-s1-s L ) (6)

[0074] In formula (6), ΔS′ represents the entropy increase of the isolated system when the condensate flash steam is extracted by the jet device; ΔS represents the entropy increase of the desuperheater as an isolated system, m L is the evaporation capacity of the flash tank, s1 is the specific entropy of the steam entering the desuperheater, which is obtained from P1 and T1 in the "Water Vapor Thermodynamic Properties Chart", and the unit is kJ / (kg.K); s2 is the specific entropy of the steam leaving the desuperheater, which is obtained from P2 and T2 in the "Water Vapor Thermodynamic Properties Chart", and the unit is kJ / (kg.K); s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer.

[0075] Due to the first law of thermodynamics, s1+s L >2s2, so m L (2s2-s1-s L ) must be a negative number. Therefore, this technology has an entropy increase of one m less than that of the temperature and pressure reduction device. L (2s2-s1-s L ).

[0076] The calculation formula for the decrease in work capacity caused by the increase in entropy of an isolated system is:

[0077] I=ΔS*T0 (7)

[0078] In formula (7), I is the loss of exergy, in kJ; ΔS is the entropy increase of the desuperheater as an isolated system, obtained through the previous calculation, in kJ / (kg.K); T0 is the ambient thermodynamic temperature, in K.

[0079] P1, T1, P2, T2, P L 、T L They are respectively the high-pressure steam pressure at the inlet of cooling and decompression (in MPa(A)), the high-pressure steam temperature at the inlet of cooling and decompression (in °C), the low-pressure steam pressure at the outlet of cooling and decompression (in MPa(A)), the low-pressure steam temperature at the outlet of cooling and decompression (in °C), the flash evaporation steam pressure (in MPa(A)) and the flash evaporation steam temperature (in °C), all of which are known data measured on site or parameters calculated previously.

[0080] Simply put, it is to make use of the originally wasted steam power, extract more steam from the condensate, reduce the supply of high-pressure steam, and achieve the real purpose of energy saving.

[0081] The steam-saving temperature and pressure reduction device provided in this embodiment utilizes the pressure energy of reducing high pressure to low pressure to pump flash steam from on-site condensate water, which is mixed and then sent downstream to form low-pressure steam. Due to the addition of flash steam, under the condition of a certain downstream steam demand, less high-pressure steam can be used to form the same amount of low-pressure steam, thereby achieving the purpose of energy saving.

[0082] By comparing with the existing technology, the following technical effects are achieved:

[0083] 1. Comparison of conventional temperature and pressure reduction devices with this embodiment

[0084] Reducing steam pressure through a conventional desuperheating and pressure reducing valve degrades steam quality and reduces exergy. Compared to conventional desuperheating and pressure reducing devices, this embodiment reduces exergy loss and recovers this lost energy as power for low-temperature flash evaporation of condensed water. The recovered energy is calculated using the following formula:

[0085] ΔI=m L (2s2-s1-s L )*T0 (8)

[0086] In formula (8), ΔI represents the loss of work capacity when using the jet device to extract condensed water and flash steam, m L is the evaporation capacity of the flash tank, s1 is the specific entropy of the high-pressure steam entering the desuperheater, s2 is the specific entropy of the low-pressure steam leaving the desuperheater, s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer, and T0 is the ambient thermodynamic temperature.

[0087] 2. Comparison of this embodiment with the steam turbine generator set replacing the temperature and pressure reduction device

[0088] Using steam turbine generators to replace desuperheating and pressure reducing devices is only suitable for plants with excess steam. When a plant does not have excess steam, using steam turbines to replace desuperheating and pressure reducing devices will result in insufficient steam supply to downstream equipment. In order to ensure the steam flow required by downstream processes, the upstream high-pressure steam supply must be increased. This increased high-pressure steam supply will be exactly equal to the desuperheating water volume of the desuperheating and pressure reducing device, and the desuperheating water volume is calculated using the following formula:

[0089] m w =m1(h1-h2) / (h2-h m ) (9)

[0090] In formula (9), m wis the mass of the desuperheating water entering the desuperheater, which is determined by the upstream and downstream processes and is expressed in kg; m1 is the mass of the high-pressure steam entering the desuperheater, which is determined by the production process and is expressed in kg; h1 is the specific enthalpy of the high-pressure steam entering the desuperheater, which is obtained from P1 and T1 in the "Water Vapor Thermodynamic Properties Chart" and is expressed in kJ / kg; h2 is the specific enthalpy of the low-pressure steam leaving the desuperheater, which is obtained from P2 and T2 in the "Water Vapor Thermodynamic Properties Chart" and is expressed in kJ / kg; h m is the specific enthalpy of the desuperheating water entering the desuperheater and pressure reducer, and P w 、T w It can be found in the "Thermodynamic Properties of Water Vapor" chart, and the unit is kJ / kg.

[0091] 3. The steam turbine power generation and grid connection system is complex and costly. This is because, in addition to the steam turbine, it also requires a generator, grid connection equipment, and even a dedicated distribution room. This results in high costs. However, the technical solution of this embodiment, with its simple main structure consisting of only a steam ejector, a flash tank, and a condensate pump, is extremely cost-effective. Besides the condensate pump, all other equipment is static, resulting in an extremely low failure rate.

[0092] 4. The value generated by the technical solution of this embodiment is to directly reduce the upstream steam supply, that is, to directly reduce the load of the boiler, reduce production costs, and have a huge advantage in investment return ratio.

[0093] 5. The steam turbine power generation and grid connection system involves a lengthy process: steam is generated by a boiler, converted to mechanical energy by a turbine, converted to electrical energy by a generator, transmitted to the grid, and then converted to other energy sources by power-consuming equipment. However, the technical solution of this embodiment directly reduces steam consumption.

[0094] As a basic energy-saving concept, it is better to use less energy directly rather than repeatedly converting it, unless the site produces a lot of by-product steam and there is a surplus after using it in the entire production system.

[0095] The steam-saving type temperature and pressure reduction device provided by the present invention is described below with reference to specific embodiments:

[0096] The following is a comparison table of three technical methods in a unit in Guizhou, while ensuring the same downstream steam volume:

[0097] a. Various energy prices and operation schedules

[0098] High-pressure steam electricity prices Tap water prices Desalted water Annual operating time Yuan / t Yuan / kW.h Yuan / t Yuan / t h / a 120 0.6 1.75 10 7200

[0099] b. Import and export parameter table

[0100]

[0101] c. Benefit Analysis Comparison Table

[0102]

[0103] The above data show that the technology of this embodiment is affected by electricity and steam prices compared with steam turbine replacement for desuperheating and pressure reduction, but the actual benefits are basically the same, and the investment is much lower than that of the steam turbine system.

[0104] More importantly, the unit itself does not have enough steam. The difference in upstream steam demand between the two methods, one positive and one negative, is more than 7 tons. Therefore, it is inevitable to choose the technology of this embodiment.

[0105] Compared to the prior art, the steam-saving temperature-reducing and pressure-reducing device provided in this embodiment utilizes a steam ejector, a flash tank, and a condensate pump. The steam ejector comprises an ejector body, a high-pressure inlet, a low-pressure outlet, and a low-pressure inlet and outlet bypass pipe provided on the ejector body; the flash tank comprises a flash tank body, a flash tank inlet, a flash tank outlet, and a condensate outlet provided on the flash tank body; and the condensate pump comprises a condensate pump body, a condensate pump inlet, and a condensate pump outlet provided on the condensate pump body. The steam-saving temperature-reducing and pressure-reducing device provided in this embodiment utilizes the pressure energy of reducing high pressure to low pressure to pump flash steam generated by a large amount of condensate at approximately 100°C on-site. The high-pressure steam and flash steam mix and then flow downstream to form low-pressure steam. Due to the addition of flash steam, less high-pressure steam can be used to generate the same amount of low-pressure steam under certain downstream steam demand conditions, thereby achieving energy conservation.

[0106] Although preferred embodiments of the present invention have been described, those skilled in the art may make additional changes and modifications to these embodiments once they are aware of the basic inventive concepts. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments and all changes and modifications that fall within the scope of the invention. Obviously, those skilled in the art may make various changes and modifications to the present invention without departing from the spirit and scope of the invention. Thus, the present invention is intended to include such changes and modifications as fall within the scope of the claims and their equivalents.

Claims

1. A steam-saving temperature and pressure reduction device, characterized in that: include: A steam ejector (10), comprising an ejector body (11), and a high-pressure inlet (12), a low-pressure outlet (13), a low-pressure inlet (14), and an outlet bypass pipe (15) provided on the ejector body (11), wherein the high-pressure inlet (12) is used to receive a high-pressure steam inlet (12), and the low-pressure outlet (13) is used to receive flash steam; the outlet bypass pipe (15) is used to receive desuperheated water; and the low-pressure outlet (14) is used to output low-pressure steam after the ejection in the steam ejector (10) is completed. A flash tank (20), the flash tank (20) comprising a flash tank body (21), and a flash tank inlet (22), a flash tank outlet (23) and a condensed water outlet (24) provided on the flash tank body (21); the flash tank outlet (23) being connected to the low-pressure outlet (13) for outputting flash steam after flash evaporation in the flash tank (20); the flash tank inlet (22) being used to access high-temperature condensed water on site, and the condensed water outlet (24) being used to output condensed water after flash evaporation in the flash tank (20); A condensate pump (30), the condensate pump (30) includes a condensate pump body (31), and a condensate pump inlet (32) and a condensate pump outlet (33) provided on the condensate pump body (31), the condensate pump inlet (32) is connected to the condensate outlet (24), and the condensate pump outlet (33) is used to output the condensate after condensation in the condensate pump (30).

2. The steam-saving type temperature and pressure reduction device according to claim 1, characterized in that: The steam-saving type temperature-reducing and pressure-reducing device further comprises a control system, wherein the control system comprises a first pressure acquisition module arranged at the inlet of the high-pressure inlet (12) for collecting the pressure of the high-pressure steam at the temperature-reducing and pressure-reducing inlet, a first temperature acquisition module for collecting the temperature of the high-pressure steam at the temperature-reducing and pressure-reducing inlet, and a first quality acquisition module for collecting the quality of the high-pressure steam at the temperature-reducing and pressure-reducing inlet; the control system further comprises a second pressure acquisition module arranged at the outlet of the low-pressure outlet (13) for collecting the pressure of the low-pressure steam at the temperature-reducing and pressure-reducing outlet, a second temperature acquisition module for collecting the temperature of the low-pressure steam at the temperature-reducing and pressure-reducing outlet, and a first quality acquisition module for collecting the quality of the high-pressure steam at the temperature-reducing and pressure-reducing outlet. A second quality acquisition module for low-pressure steam quality; the control system also includes a third pressure acquisition module located at the inlet of the outlet bypass pipe (15) for acquiring the inlet pressure of the cooling water, a third temperature acquisition module located at the inlet temperature of the cooling water, and a third quality acquisition module located at the inlet quality of the cooling water; the control system also includes a fourth pressure acquisition module located at the inlet of the low-pressure inlet (14) for acquiring the flash steam pressure of the flash steam inlet, a fourth temperature acquisition module located at the inlet temperature of the flash steam inlet, and a fourth quality acquisition module located at the inlet quality of the flash steam inlet.

3. The steam-saving temperature and pressure reduction device according to claim 2, characterized in that: The control system further includes a controller, which is connected to the first pressure acquisition module, the first temperature acquisition module, the first mass acquisition module, the second pressure acquisition module, the second temperature acquisition module, the second mass acquisition module, the third pressure acquisition module, the third temperature acquisition module, the third mass acquisition module, the fourth pressure acquisition module, the fourth temperature acquisition module and the fourth mass acquisition module respectively, and is used to acquire the temperature of the high-pressure steam at the cooling and pressure reduction inlet collected by the first pressure acquisition module, the temperature of the high-pressure steam at the cooling and pressure reduction inlet collected by the first temperature acquisition module, and the mass of the high-pressure steam at the cooling and pressure reduction inlet collected by the first mass acquisition module. The high-pressure steam flow rate at the ejector inlet is calculated by: the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

4. The steam-saving temperature and pressure reduction device according to claim 3, characterized in that: The high-pressure steam flow rate at the steam ejector inlet is calculated using the mass balance formula: m2=m L +m w +m1 Among them, m2 is the mass flow rate of low-pressure steam at the outlet of the steam ejector, m L is the evaporation capacity of the flash tank, m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet, m w The amount of water added to reduce the temperature.

5. The steam-saving temperature and pressure reduction device according to claim 3, characterized in that: The controller is further used to calculate the amount of condensed water flowing out of the flash tank based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

6. The steam-saving temperature and pressure reduction device according to claim 5, characterized in that: The amount of condensed water flowing out of the flash tank is calculated using the following formula: m s ′=m s -m L Among them, m s ′ is the amount of condensed water flowing out of the flash tank, m s is the amount of high-temperature condensed water flowing into the flash tank; m L is the evaporation capacity of the flash tank.

7. The steam-saving temperature and pressure reduction device according to claim 3, characterized in that: The controller is further configured to calculate the flash steam quantity of the flash evaporator based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

8. The steam-saving temperature and pressure reduction device according to claim 7, characterized in that: The amount of condensed water flowing out of the flash tank is calculated using the following formula: Among them, m L is the evaporation capacity of the flash tank, m s is the amount of high-temperature condensed water flowing into the flash tank, h s is the specific enthalpy of the high-temperature condensed water flowing into the flash tank, h L is the specific enthalpy of the high-temperature condensed water flowing into the flash tank, h s ′ is the specific enthalpy of the condensed water flowing out of the flash tank.

9. The steam-saving temperature and pressure reduction device according to claim 3, characterized in that: The controller is further used to calculate the entropy increase and recovered energy flux of the isolated system using the entropy increase equation of the isolated system based on the high-pressure steam temperature at the cooling and decompression inlet collected by the first pressure collection module, the high-pressure steam temperature at the cooling and decompression inlet collected by the first temperature collection module, the high-pressure steam mass at the cooling and decompression inlet collected by the first mass collection module, the low-pressure steam pressure at the cooling and decompression outlet collected by the second pressure collection module, the low-pressure steam temperature at the cooling and decompression outlet collected by the second temperature collection module, the low-pressure steam mass at the cooling and decompression outlet collected by the second mass collection module, the cooling water inlet pressure collected by the third pressure collection module, the cooling water inlet temperature collected by the third temperature collection module, the cooling water inlet mass collected by the third mass collection module, the flash steam pressure at the flash steam inlet collected by the fourth pressure collection module, the flash steam temperature at the flash steam inlet collected by the fourth temperature collection module, and the flash steam mass at the flash steam inlet collected by the fourth mass collection module.

10. The steam-saving temperature and pressure reduction device according to claim 9, characterized in that: The entropy increase of the isolated system is calculated by the following formula: ΔS′=-(m1-m L )(s2-s1)+m w (s2-s w )+m L (s2-s L ) =-m1(s2-s1)+m L (s2-s1)+m w (s2-s w )+m L (s2-s L )in, ΔS′ represents the entropy increase of the isolated system when the condensed water flash steam is extracted by the jet device, m1 is the mass flow rate of the high-pressure steam at the desuperheating and pressure reduction inlet, m L is the evaporation capacity of the flash tank, s2 is the specific entropy of the high-pressure steam entering the desuperheater, s1 is the specific entropy of the high-pressure steam entering the desuperheater, m w is the amount of cooling water added; s w is the specific entropy of the desuperheating water entering the desuperheating and pressure reducing device, s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer; The recovered energy is calculated by the following formula: ΔI=m L (2s2-s1-s L )*T0 Where ΔI represents the loss of the ability to pump condensed water and flash steam using the jet device, m L is the evaporation capacity of the flash tank, s1 is the specific entropy of the high-pressure steam entering the desuperheater, s2 is the specific entropy of the low-pressure steam leaving the desuperheater, s L is the specific entropy of the flash steam entering the desuperheater and pressure reducer, and T0 is the ambient thermodynamic temperature.

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