System for recovering and refining desalted water from steam condensate

Abstract

The utility model relates to the technical field of waste liquid recovery and reutilization, in particular to a system for recovering steam condensate and refining desalted water, which sequentially comprises a pretreatment system, an ion exchange system and a regeneration system connected with the ion exchange system according to the flowing direction of the steam condensate, the pretreatment system sequentially comprises a condensate water tank, an oil and iron removal filter and an activated carbon filter in the flowing direction of steam condensate; the ion exchange system sequentially comprises a front cation bed, a refining mixed bed, a desalting water tank and a first flow direction control device according to the flow direction of steam condensate; the technical problems that in the prior art, steam condensate recycling treatment is complex in treatment process, corresponding technological parameters need to be specifically adjusted according to steam condensate, the equipment adaptation rate is low, and cost is high are solved.

Description

Technical Field

[0001] The utility model relates to the technical field of waste liquid recovery and reuse, in particular to a system for recovering refined desalted water from steam condensate. Background Art

[0002] With water scarcity and growing environmental awareness, steam condensate recovery has become a cost-effective, environmentally friendly, and sustainable way to utilize water resources. Steam condensate refers to the liquid water formed by the condensation of water vapor generated during industrial production, air conditioning, refrigeration, and boiler processes. This condensate contains impurities such as oil, grease, cations, and anions. Traditionally, steam condensate was treated as wastewater and discharged directly, resulting in significant water waste and pollution. In recent years, environmental protection and energy conservation have become inevitable, driven by national regulations and corporate requirements. Therefore, developing steam condensate recovery solutions is of great significance, particularly for large-scale manufacturers, as it can save significant energy and capital.

[0003] There are two existing methods for recovering steam condensate: pressure flash evaporation and atmospheric pressure flash evaporation. For example, CN108654127A discloses a steam condensate recovery system, which includes a steam flash tank connected to high- and medium-pressure steam condensate from users. The steam flash tank is equipped with a flash steam pipe 1, which connects the condensate to the steam condensate tank inlet through a connecting pipe at the bottom. The upper end of the steam condensate tank is connected to low-pressure steam condensate from users. The steam condensate tank is equipped with a flash steam pipe 2. The collected condensate is pumped to the system user for heat exchange via a steam condensate circulation pump. After heat exchange, it is sent to a hot water tank. The condensate collected in the hot water tank is divided into two paths after passing through a hot water transfer pump: one path is sent to a refrigeration station, and the other is used to flush the main pipeline. A weather jacket 1 is installed on the gas outlet pipe at the top of the hot water tank. The weather jacket 1 uses circulating cooling water to cool the water vapor discharged from the hot water tank, and then returns it to the hot water tank for collection.

[0004] Both pressure flash evaporation and atmospheric flash evaporation have disadvantages to some extent. The main disadvantages of pressure flash evaporation include: 1. High energy consumption: Pressure flash evaporation requires high pressure, so a large amount of energy is consumed to maintain the system pressure, which reduces energy efficiency and increases operating costs. 2. High equipment requirements: Because it is carried out under high pressure conditions, pressure flash evaporation has high requirements for equipment, requiring the use of special materials and designs that can withstand high pressure. This increases the investment cost and maintenance difficulty of the equipment. 3. High operational difficulty: The operation process of pressure flash evaporation is relatively complex and requires strict control of parameters such as pressure and temperature. Otherwise, the evaporation effect and product quality may be affected, requiring operators to possess high professional knowledge and skills. The main disadvantages of atmospheric flash evaporation include: 1. Slow evaporation rate: Compared with pressure flash evaporation, atmospheric flash evaporation has a slower evaporation rate because the boiling point of liquid at atmospheric pressure is higher, requiring more energy to evaporate the liquid into gas, which affects production efficiency and output. 2. Large footprint: Atmospheric flash evaporation equipment is generally large and occupies a correspondingly large area. This will increase land costs and construction difficulty; 3. High requirements for raw materials: Atmospheric pressure flash evaporation has high requirements for the purity and properties of raw materials. If the raw materials contain more impurities or components that are not conducive to evaporation, it may affect the evaporation effect and product quality.

[0005] Both methods have certain shortcomings, and the specific considerations depend on factors such as specific process conditions, equipment performance, and operational level. The need to adjust specific process parameters, such as flash evaporation conditions, based on the different impurities in the steam condensate can hinder the widespread adoption of these equipment and systems. Furthermore, these methods can result in high processing costs, placing a financial burden on some companies.

[0006] Based on the above-mentioned existing technology, there are technical problems in the existing technology that need to be solved urgently, such as the steam condensate recovery process is complicated, the corresponding process parameters need to be adjusted according to the specific steam condensate, the equipment adaptability is not high, and the cost is high. Utility Model Content

[0007] In order to solve the above technical problems, the utility model provides a system for recovering refined desalted water from steam condensate, wherein the system comprises, in order according to the flow direction of the steam condensate: a pretreatment system, an ion exchange system, and a regeneration system connected to the ion exchange system;

[0008] The pretreatment system includes a condensate water tank, an oil and iron removal filter, and an activated carbon filter in the direction of flow of steam condensate;

[0009] The ion exchange system includes, in order of the flow direction of the steam condensate, a pre-cation bed, a refined mixed bed, a desalted water tank, and a first flow direction control device; the first flow direction control device is provided with a first desalted water outlet and a second desalted water outlet, the first desalted water outlet is connected to a water unit for production reuse, and the second desalted water outlet is connected to the regeneration system;

[0010] The regeneration system includes a second flow direction control device, an acid regeneration system, and an alkali regeneration system; the acid regeneration system is connected to the pre-cation bed and the refined mixed bed respectively; the alkali regeneration system is connected to the refined mixed bed;

[0011] The second flow direction control device is provided with a material inlet, a first material outlet and a second material outlet; the material inlet is connected to the second desalted water outlet, the first material outlet is connected to the acid regeneration system, and the second material outlet is connected to the alkali regeneration system.

[0012] Furthermore, the first flow direction control device is one of a reversing valve, a diverter valve, and a bypass with a switch valve, which is used to transport the desalted water in the desalted water tank to the water unit and / or the regeneration system.

[0013] Furthermore, the second flow direction control device is one of a reversing valve, a diverter valve, and a bypass with a switch valve, which is used to deliver the desalted water delivered from the first flow direction control device to the acid regeneration system and / or the alkali regeneration system respectively.

[0014] Furthermore, the pretreatment system further comprises a steam-condensate heat exchanger for reducing the temperature of the steam condensate entering the steam-condensate heat exchanger, and the condensate outlet of the steam-condensate heat exchanger is connected to the condensate inlet of the condensate water tank.

[0015] Furthermore, a first water pump is provided between the condensate water tank and the oil removal and iron removal filter, and the first water pump is used to pump the steam condensate passing through the condensate water tank into the oil removal and iron removal filter.

[0016] Furthermore, the oil and iron removal filter is provided with a filter element filter layer for adsorbing and intercepting grease and solid impurities in the steam condensate.

[0017] Furthermore, the solid impurities include iron-containing solid impurities.

[0018] Furthermore, an activated carbon adsorption layer is provided in the activated carbon filter for adsorbing residual grease in the material sent out from the oil and iron removal filter.

[0019] Furthermore, an intermediate water tank and a second water pump are provided between the pretreatment system and the ion exchange system; the outlet of the activated carbon filter is connected to the inlet of the intermediate water tank, the outlet of the intermediate water tank is connected to the inlet of the second water pump, and the outlet of the second water pump is connected to the material inlet of the pre-cation bed;

[0020] The intermediate water tank is used to store the material filtered from the activated carbon filter;

[0021] The second water pump is used to deliver the material in the intermediate water tank to the front catenary bed.

[0022] Furthermore, a first cation exchange resin layer is provided in the pre-cation bed for absorbing cations in the material sent from the pretreatment system to the pre-cation bed.

[0023] Furthermore, a second cation exchange resin layer and an anion exchange resin layer are provided in the refined mixed bed for absorbing anions and remaining cations in the material sent from the pre-cation bed to the refined mixed bed.

[0024] Furthermore, a terminal filter is provided between the refined mixed bed and the desalted water tank to further refine the material sent out from the refined mixed bed to meet higher water demand.

[0025] Furthermore, a third water pump is provided between the desalted water tank and the first flow direction control device for delivering the desalted water in the desalted water tank to the first flow direction control device for reversing or diverting delivery.

[0026] Furthermore, the acid regeneration system includes an acid metering tank, an acid injector, and a mixed acid flow control device;

[0027] The acid ejector is provided with an acid inlet, a first desalted water inlet, and a mixed acid outlet for mixing the desalted water and the acid;

[0028] The acid inlet is connected to the outlet of the acid metering box, and the first desalted water inlet is connected to the first material outlet, so as to mix the acid liquid in the acid metering box and the desalted water sent from the first material outlet to obtain a mixed acid liquid. The mixed acid outlet is connected to the mixed acid flow direction control device, and the mixed acid flow direction control device is connected to the pre-cation bed on one path to send the mixed acid liquid to the pre-cation bed to regenerate the resin in the first cation exchange resin layer in the pre-cation bed; and is connected to the refining mixed bed on the other path to send the mixed acid to the refining mixed bed to regenerate the resin in the second cation exchange resin layer in the refining mixed bed.

[0029] Furthermore, the mixed acid flow control device is one of a reversing valve, a diverter valve, and a bypass with an on-off valve, which is used to deliver the mixed acid liquid sent out from the acid injector to the pre-cation bed and / or the refined mixed bed.

[0030] Furthermore, the alkali regeneration system includes an alkali metering box and an alkali injector;

[0031] The alkali ejector is provided with an alkali inlet, a second desalted water inlet, and a mixed alkali outlet for mixing the desalted water and the alkali;

[0032] The alkali inlet is connected to the outlet of the alkali metering tank, and the second desalted water inlet is connected to the second material outlet, so as to mix the alkali solution in the alkali metering tank and the desalted water sent from the second material outlet to obtain a mixed alkali solution. The mixed alkali outlet is connected to the refining mixed bed to send the mixed alkali solution into the refining mixed bed to regenerate the resin in the anion exchange resin layer in the refining mixed bed.

[0033] Furthermore, the acid regeneration system also includes an acid mist absorber for absorbing acid mist generated when the acid is mixed with desalted water to prevent it from diffusing into the air and polluting the environment.

[0034] Furthermore, the alkali regeneration system also includes a carbon dioxide absorber. While the alkali in the alkali metering box is delivered to the alkali injector, air is introduced into the alkali metering box to ensure pressure stability. The carbon dioxide absorber is used to absorb carbon dioxide in the introduced air to prevent the carbon dioxide in the air from reacting with the alkali, causing the alkali to fail and reducing the production efficiency of the entire system.

[0035] Furthermore, the system also includes a wastewater pool, which is connected to the pre-cation bed and the refined mixed bed to collect waste liquid generated when the regeneration system regenerates the ion exchange system.

[0036] The beneficial effects of the present invention are:

[0037] 1. The utility model provides a system for recovering and refining desalted water from steam condensate. The system comprises, in order according to the flow direction of the steam condensate, a pretreatment system, an ion exchange system, and a regeneration system connected to the ion exchange system; the pretreatment system comprises, in order according to the flow direction of the steam condensate, a condensate water tank, an oil and iron removal filter, and an activated carbon filter; the ion exchange system comprises, in order according to the flow direction of the steam condensate, a pre-cation bed, a refined mixed bed, a desalted water tank, and a first flow direction control device; and finally, desalted water with an electrical conductivity of less than 20 μs / cm at 25° C. is obtained and directly sent to a water unit or regeneration system requiring water in the plant area, or used to dilute acid and alkali solutions in an acid regeneration system and an alkali regeneration system. This solves the technical problems of the prior art in steam condensate recovery and treatment, such as a complex treatment process, the need to adjust corresponding process parameters according to the specific steam condensate, low equipment adaptability, and high cost.

[0038] 2. The regeneration system of the present invention includes a second flow direction control device, an acid regeneration system, and an alkali regeneration system; the acid regeneration system is respectively connected to the pre-cation bed and the refined mixed bed; the alkali regeneration system is connected to the refined mixed bed; since the ion exchange system will accumulate impurities during long-term use, resulting in reduced production efficiency, the structural design of the regeneration system of the present invention can remove the above impurities and restore the adsorption capacity of the ion exchange system, thereby extending its service life, improving the production safety index, and meeting the requirements of environmental protection and sustainable development. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 This is a schematic structural diagram of a system for recovering refined desalted water from steam condensate in an embodiment of the present utility model;

[0040] The names of the labels in the figure are:

[0041] 1. Condensate water tank; 2. Oil and iron removal filter; 3. Activated carbon filter; 4. Pre-cationic bed; 5. Refining mixed bed; 6. Desalted water tank; 7. First flow control device; 8. Second flow control device; 9. Steam condensate heat exchanger; 10. First water pump; 11. Intermediate water tank; 12. Second water pump; 13. Terminal filter; 14. Third water pump; 15. Acid metering tank; 16. Acid injector; 17. Mixed acid flow control device; 18. Alkali metering tank; 19. Alkali injector. DETAILED DESCRIPTION

[0042] Example 1

[0043] like Figure 1 As shown, this embodiment provides a system for recovering refined desalted water from steam condensate, the system comprising, in order according to the flow direction of the steam condensate: a pretreatment system, an ion exchange system, and a regeneration system connected to the ion exchange system;

[0044] The pretreatment system includes, in order according to the flow direction of the steam condensate, a condensate water tank 1, an oil and iron removal filter 2, and an activated carbon filter 3;

[0045] The ion exchange system includes a pre-cation bed 4, a refined mixed bed 5, a desalted water tank 6, and a first flow direction control device 7 in sequence according to the flow direction of the steam condensate; the first flow direction control device 7 is provided with a first desalted water outlet and a second desalted water outlet, the first desalted water outlet is connected to the water unit for production reuse, and the second desalted water outlet is connected to the regeneration system. In this embodiment, the first flow direction control device 7 is a reversing valve. In some embodiments, the first flow direction control device 7 is a diverter valve or a bypass with a switch valve, which is used to realize the transportation of the desalted water in the desalted water tank 6 to the water unit and / or the regeneration system.

[0046] The regeneration system includes a second flow direction control device 8, an acid regeneration system, and an alkali regeneration system; the acid regeneration system is respectively connected to the pre-cation bed 4 and the refined mixed bed 5; the alkali regeneration system is connected to the refined mixed bed 5. In this embodiment, the second flow direction control device 8 is a diverter valve. In some embodiments, the second flow direction control device 8 is a reversing valve or a bypass with a switch valve, which is used to realize the desalted water transported from the first flow direction control device 7 to the acid regeneration system and / or the alkali regeneration system respectively.

[0047] The second flow direction control device 8 is provided with a material inlet, a first material outlet and a second material outlet; the material inlet is connected to the second desalted water outlet, the first material outlet is connected to the acid regeneration system, and the second material outlet is connected to the alkali regeneration system.

[0048] The pretreatment system further includes a steam-condensate heat exchanger 9 to reduce the temperature of the steam condensate entering the steam-condensate heat exchanger 9 . The condensate outlet of the steam-condensate heat exchanger 9 is connected to the condensate inlet of the condensate water tank 1 .

[0049] A first water pump 10 is further provided between the condensate water tank 1 and the oil and iron removal filter 2 . The first water pump 10 is used to pump the steam condensate passing through the condensate water tank 1 into the oil and iron removal filter 2 .

[0050] The oil and iron removal filter 2 is provided with a filter element filter layer for adsorbing and intercepting grease and solid impurities in the steam condensate. In this embodiment, the solid impurities include iron-containing solid impurities.

[0051] The activated carbon filter 3 is provided with an activated carbon adsorption layer for adsorbing the remaining grease in the material sent out from the oil and iron removal filter 2 .

[0052] An intermediate water tank 11 and a second water pump 12 are further provided between the pretreatment system and the ion exchange system; the outlet of the activated carbon filter 3 is connected to the inlet of the intermediate water tank 11, the outlet of the intermediate water tank 11 is connected to the inlet of the second water pump 12, and the outlet of the second water pump 12 is connected to the material inlet of the pre-cation bed 4;

[0053] The intermediate water tank 11 is used to store the material filtered from the activated carbon filter 3;

[0054] The second water pump 12 is used to deliver the material in the intermediate water tank 11 to the front positive bed 4.

[0055] The pre-cation bed 4 is provided with a first cation exchange resin layer for absorbing cations in the material sent from the pretreatment system to the pre-cation bed 4 .

[0056] The refining mixed bed 5 is provided with a second cation exchange resin layer and an anion exchange resin layer for absorbing anions and remaining cations in the material sent from the pre-cation bed 4 to the refining mixed bed 5 .

[0057] A terminal filter 13 is further provided between the refined mixed bed 5 and the desalted water tank 6 for re-refining the material sent out from the refined mixed bed 5 to meet higher water demand.

[0058] A third water pump 14 is further provided between the desalted water tank 6 and the first flow direction control device 7 for delivering the desalted water in the desalted water tank 6 to the first flow direction control device 7 for reversing or diverting delivery.

[0059] The acid regeneration system includes an acid metering tank 15, an acid injector 16, and a mixed acid flow control device 17;

[0060] The acid injector 16 is provided with an acid inlet, a first desalted water inlet, and a mixed acid outlet for mixing the desalted water and the acid;

[0061] The acid inlet is connected to the outlet of the acid metering tank 15, and the first desalted water inlet is connected to the first material outlet, so as to mix the acid solution in the acid metering tank 15 and the desalted water sent from the first material outlet to obtain a mixed acid solution. The mixed acid outlet is connected to the mixed acid flow direction control device 17. The mixed acid flow direction control device 17 is connected to the pre-cation bed 4 on one side to send the mixed acid solution to the pre-cation bed 4 to regenerate the resin in the first cation exchange resin layer in the pre-cation bed 4; and is connected to the refining mixed bed 5 on the other side to send the mixed acid to the refining mixed bed 5 to regenerate the resin in the second cation exchange resin layer in the refining mixed bed 5. In this embodiment, the mixed acid flow direction control device 17 is a bypass with a switch valve. In some embodiments, the mixed acid flow direction control device 17 is a reversing valve or a diverter valve to realize that the mixed acid solution sent from the acid injector 16 is sent to the pre-cation bed 4 and / or the refining mixed bed 5.

[0062] The alkali regeneration system includes an alkali metering box 18 and an alkali injector 19;

[0063] The alkali injector 19 is provided with an alkali inlet, a second desalted water inlet, and a mixed alkali outlet for mixing the desalted water and the alkali;

[0064] The alkali inlet is connected to the outlet of the alkali metering tank 18, and the second desalted water inlet is connected to the second material outlet, so as to mix the alkali solution in the alkali metering tank 18 and the desalted water sent from the second material outlet to obtain a mixed alkali solution. The mixed alkali outlet is connected to the refining mixed bed 5 to send the mixed alkali solution into the refining mixed bed 5 to regenerate the resin in the anion exchange resin layer in the refining mixed bed 5.

[0065] The acid regeneration system also includes an acid mist absorber for absorbing acid mist generated when the acid is mixed with desalted water to prevent it from diffusing into the air and polluting the environment.

[0066] The alkali regeneration system also includes a carbon dioxide absorber. While the alkali in the alkali metering box 18 is being delivered to the alkali injector 19, air is introduced into the alkali metering box 18 to ensure pressure stability. The carbon dioxide absorber is used to absorb carbon dioxide in the introduced air to prevent the carbon dioxide in the air from reacting with the alkali, causing the alkali to become ineffective and reducing the production efficiency of the entire system.

[0067] The system further comprises a wastewater tank, which is connected to the pre-cation bed 4 and the refined mixed bed 5 to collect waste liquid generated when the regeneration system regenerates the ion exchange system.

[0068] In the system for recovering refined desalted water from steam condensate provided in this embodiment, steam condensate was used to verify the system. The steam condensate had a pH value of 7-9 at 25°C, a conductivity of <20μs / cm, an iron ion content of <300μg / L, a fat content of <50μg / L, a hardness of ≤0.06mmol / L, and a feed temperature of ≤100°C.

[0069] Among them, when verifying the system, the oil removal and iron removal filter 2 is provided with a filter element filter layer using a material that can adsorb and retain grease and solid impurities in the prior art. The indicators of the activated carbon adsorption layer in the activated carbon filter 3 are shown in Table 1, the resin indicators used in the first cation exchange resin layer in the pre-cation bed 4 are shown in Table 2, the resin indicators used in the second cation exchange resin layer in the refined mixed bed 5 are shown in Table 3, and the resin indicators used in the anion exchange resin layer are shown in Table 4. The acid metering box 15 is filled with hydrochloric acid solution, and the indicators of the hydrochloric acid solution are shown in Table 5. The alkali metering box 18 is filled with sodium hydroxide solution, and the indicators of the sodium hydroxide solution are shown in Table 6:

[0070] Table 1 Activated carbon indicators in the activated carbon adsorption layer

[0071]

[0072] Table 2 Resin specifications used in the first cation exchange resin layer

[0073]

[0074] Table 3 Resin indexes used in the second cation exchange resin layer

[0075]

[0076] Table 4 Resin specifications used in the anion exchange resin layer

[0077]

[0078] Table 5 Hydrochloric acid solution indicators

[0079]

[0080] Table 6 Sodium hydroxide solution indicators

[0081]

[0082] It should be noted that the indicators of the above materials are only for verifying the system for recovering refined desalted water from steam condensate provided in this embodiment, and are not intended to limit the system.

[0083] Through the above verification, the system for recovering refined desalted water using the steam condensate provided in this embodiment can ultimately achieve a pH value of 6.5-7.5 at 25°C, a conductivity of <0.2μs / cm, a silicon dioxide content ≤20μg / L, an iron ion content <300μg / L, a fat content of 0, and a hardness of 0. The desalted water at room temperature is directly sent to the water unit or regeneration system in the factory area that needs water, and is used to dilute the acid and alkali solutions in the acid regeneration system and the alkali regeneration system. This solves the technical problems of the steam condensate recovery process in the prior art, such as the complex treatment process, the need to adjust the corresponding process parameters according to the specific steam condensate, the low equipment adaptability, and the high cost.

[0084] At the same time, since the ion exchange system will accumulate impurities during long-term use, resulting in reduced production efficiency, the structural design of the regeneration system in this embodiment can remove the above impurities and restore the adsorption capacity of the ion exchange system, thereby extending its service life, improving the production safety index, and meeting the requirements of environmental protection and sustainable development.

[0085] It should be understood that the present invention is not limited to the contents described above and shown in the accompanying drawings, and various modifications and changes can be made without departing from the scope thereof. The scope of the present invention is limited only by the appended claims.

Claims

1. A system for recovering refined desalted water from steam condensate, characterized in that: The system includes, in order according to the flow direction of the steam condensate: a pretreatment system, an ion exchange system, and a regeneration system connected to the ion exchange system; The pretreatment system comprises, in order according to the flow direction of the steam condensate, a condensate water tank (1), an oil and iron removal filter (2), and an activated carbon filter (3); The ion exchange system comprises, in order according to the flow direction of the steam condensate, a pre-cation bed (4), a refined mixed bed (5), a desalted water tank (6), and a first flow direction control device (7); the first flow direction control device (7) is provided with a first desalted water outlet and a second desalted water outlet, the first desalted water outlet is connected to the water use unit, and the second desalted water outlet is connected to the regeneration system; The regeneration system comprises a second flow direction control device (8), an acid regeneration system, and an alkali regeneration system; the acid regeneration system is connected to the front cation bed (4) and the refining mixed bed (5), respectively; the alkali regeneration system is connected to the refining mixed bed (5); The second flow direction control device (8) is provided with a material inlet, a first material outlet and a second material outlet; the material inlet is connected to the second desalted water outlet, the first material outlet is connected to the acid regeneration system, and the second material outlet is connected to the alkali regeneration system.

2. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: The pretreatment system further comprises a steam-condensate heat exchanger (9), wherein a condensate outlet of the steam-condensate heat exchanger (9) is connected to a condensate inlet of the condensate water tank (1).

3. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: A first water pump (10) is also provided between the condensate water tank (1) and the oil and iron removal filter (2).

4. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: An intermediate water tank (11) and a second water pump (12) are also provided between the pretreatment system and the ion exchange system.

5. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: A third water pump (14) is also provided between the desalted water tank (6) and the first flow direction control device (7).

6. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: The acid regeneration system comprises an acid metering box (15), an acid injector (16), and a mixed acid second flow direction control device (17); The acid injector (16) is provided with an acid inlet, a first desalted water inlet, and a mixed acid outlet.

7. The system for recovering refined desalted water from steam condensate according to claim 1, characterized in that: The alkali regeneration system comprises an alkali metering box (18) and an alkali injector (19); The alkali injector (19) is provided with an alkali inlet, a second desalted water inlet, and a mixed alkali outlet.

8. The system for recovering refined desalted water from steam condensate according to claim 6, characterized in that: The acid regeneration system also includes an acid mist absorber.

9. The system for recovering refined desalted water from steam condensate according to claim 7, characterized in that: The alkali regeneration system also includes a carbon dioxide absorber.

10. The system for recovering refined desalted water from steam condensate according to any one of claims 1 to 9, characterized in that: The system further comprises a wastewater tank, which is connected to the front cation bed (4) and the refined mixed bed (5).

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