System for rapidly adjusting indexes of coking wastewater

Abstract

The utility model discloses a system for quickly adjusting indexes of coking wastewater. Comprising an ammonia distillation tower, a desulfurization removal pipeline, a reboiler, a low-pressure steam pipeline, a steam condensate pipeline, an ammonia distillation wastewater pump, an ammonia water heat exchanger, an ammonia water heat exchange pipeline, an ammonia distillation wastewater traffic pipe, a first electromagnetic valve, a residual ammonia water pipeline, a wastewater first-section cooler, a wastewater second-section cooler and an ammonia distillation wastewater pipeline, the output end of the ammonia water heat exchanger is communicated and connected with an ammonia distillation wastewater traffic pipe, the ammonia distillation wastewater traffic pipe is fixedly connected with a first electromagnetic valve, and the output end of the ammonia water heat exchanger is fixedly connected with a second temperature controller; the ammonia distillation wastewater traffic pipe for a tar removal ammonia water separation process is additionally arranged behind the ammonia water heat exchanger, ammonia distillation wastewater does not exchange heat with the wastewater first-section cooler and the wastewater second-section cooler any more, and returns to a residual ammonia water system at a high temperature, so that the operations of stopping a residual ammonia water pump, an ammonia distillation wastewater pump and the like are avoided, and the adjustment time is greatly shortened.

Description

Technical Field

[0001] This utility model relates to the field of coking wastewater treatment technology, and in particular to a system for rapidly adjusting the indicators of coking wastewater. Background Technology

[0002] Coking coal, in the absence of air, undergoes dry distillation to produce coke, coke oven gas, and chemical products. Coking wastewater originates from the high-temperature dry distillation of coal, gas purification, and chemical product refining processes. It has a complex composition, high pollutant concentrations, and high toxicity, classifying it as recalcitrant industrial wastewater. Characterized by total NH3-N content, coking wastewater is primarily concentrated in the residual ammonia water (approximately 95% of the total NH3-N). Therefore, before mixing the residual ammonia water with other wastewater (such as gas seal water) for biological treatment, a significant reduction in NH3-N must be achieved to meet the influent NH3-N requirements of the biological treatment process. Many methods exist for removing NH3-N from residual ammonia water, such as distillation, stripping, adsorption, and precipitation. The latter two methods are only suitable for small-scale treatment. Each method has its own advantages and disadvantages. Advantages and disadvantages: In the coking industry, distillation is generally used as a pretreatment method for residual ammonia water before biochemical treatment. The conventional process flow in the coking industry is as follows: the residual ammonia water from the tar ammonia water separation process enters the ammonia water heat exchanger to exchange heat with the ammonia stripping wastewater discharged from the bottom of the ammonia stripping tower; the alkali solution enters the static pipeline mixer through the metering pump and mixes with the residual ammonia water, and then enters the upper part of the ammonia stripping tower to decompose the fixed ammonium in the residual ammonia water; the ammonia stripping wastewater at the bottom of the tower is indirectly heated by the reboiler, and the generated steam is returned to the bottom of the tower as the heat source for ammonia stripping; the ammonia gas at the top of the ammonia stripping tower is condensed by the top separator and sent to the desulfurization or ammonium sulfate unit; the ammonia stripping wastewater from the bottom of the tower is pumped out by the ammonia stripping wastewater pump, exchanges heat with the residual ammonia water in the ammonia water heat exchanger, and is then cooled by the first and second stage wastewater coolers before being sent to the wastewater treatment unit.

[0003] In existing coking wastewater index adjustment systems, ammonia stripping wastewater typically exchanges heat with the primary and secondary wastewater coolers, resulting in a decrease in wastewater temperature. To adjust wastewater indexes, it is necessary to shut down equipment such as the residual ammonia pump and the ammonia stripping wastewater pump. This not only increases operational complexity but may also affect the stability and reliability of the system. Furthermore, the index adjustment process is relatively lengthy because it requires multiple steps and monitoring of multiple parameters. Utility Model Content

[0004] The purpose of this invention is to provide a system for rapidly adjusting the parameters of coking wastewater, in order to solve the problems mentioned in the background art.

[0005] To solve the above-mentioned technical problems, this utility model provides the following technical solution: a system for rapidly adjusting the indicators of coking wastewater, comprising an ammonia stripping tower, an ammonia water heat exchange pipe connected to the ammonia stripping tower, an ammonia water heat exchanger connected to the other end of the ammonia water heat exchange pipe, an ammonia water heat exchanger connected to the input end of the ammonia water heat exchanger connected to an ammonia stripping wastewater pump and a residual ammonia water pipe, the ammonia stripping wastewater pump being connected to the ammonia stripping tower, an ammonia water heat exchanger connected to the output end of the ammonia water heat exchanger connected to an ammonia stripping wastewater transport pipe, a first solenoid valve fixedly connected to the ammonia water heat exchanger, and a second temperature controller fixedly connected to the output end of the ammonia water heat exchanger.

[0006] As a further technical solution of this utility model, a shrinkage unit is fixedly connected to the ammonia stripping tower, and the shrinkage unit is conductively connected to a desulfurization pipeline, a first return water pipeline, a first supply water pipeline, and a sodium hydroxide alkali solution pipeline.

[0007] As a further technical solution of this utility model, a reboiler is connected to the ammonia stripping tower, and a low-pressure steam pipe and a steam condensate pipe are connected to the reboiler. A first temperature controller is fixedly connected to the low-pressure steam pipe.

[0008] As a further technical solution of this utility model, the ammonia water heat exchanger is connected to a wastewater primary cooler, and the wastewater primary cooler is connected to a second water supply pipe and a second water return pipe.

[0009] As a further technical solution of this utility model, a second solenoid valve is fixedly connected to the input end of the wastewater primary cooler, and a third temperature controller is fixedly connected to the output end of the wastewater primary cooler.

[0010] As a further technical solution of this utility model, the output end of the first stage wastewater cooler is connected to a second stage wastewater cooler, and the second stage wastewater cooler is connected to a low-temperature water supply pipe and a low-temperature water return pipe.

[0011] As a further technical solution of this utility model, the output end of the wastewater two-stage cooler is connected to an ammonia-eating wastewater pipe, and a fourth temperature controller is fixedly connected to the ammonia-eating wastewater pipe.

[0012] Compared with the prior art, the beneficial effects achieved by this utility model are as follows: This utility model adds a tar-removing ammonia water separation process flow pipe after the ammonia water heat exchanger. The ammonia water no longer exchanges heat with the first-stage and second-stage wastewater coolers, and returns to the residual ammonia water system at a higher temperature. This avoids the need to shut down the residual ammonia water pump and the ammonia water separation pump, greatly shortening the adjustment time. Compared with the conventional adjustment process, the simplified operation of the ammonia separation unit shortens the operation time. Simply changing the destination of the ammonia water separation wastewater can prevent the excessive wastewater from impacting the biochemical system, greatly improving start-up and shutdown time and enhancing the management level of the enterprise. Attached Figure Description

[0013] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0014] Figure 1 This is a schematic diagram of the system structure of this utility model.

[0015] In the diagram: 1. Ammonia stripping tower; 2. Desulfurization pipeline; 3. First return water pipeline; 4. First supply water pipeline; 5. Sodium hydroxide alkali solution pipeline; 6. Reboiler; 7. Low-pressure steam pipeline; 8. Steam condensate pipeline; 9. First temperature controller; 10. Ammonia stripping wastewater pump; 11. Ammonia water heat exchanger; 12. Ammonia water heat exchange pipeline; 13. Second temperature controller; 14. Ammonia stripping wastewater access pipeline; 15. First solenoid valve; 16. Residual ammonia water pipeline; 17. Wastewater primary cooler; 18. Second supply water pipeline; 19. Second return water pipeline; 20. Third temperature controller; 21. Wastewater secondary cooler; 22. Low-temperature water supply pipeline; 23. Low-temperature water return pipeline; 24. Fourth temperature controller; 25. Ammonia stripping wastewater pipeline; 26. Divider; 27. Second solenoid valve. Detailed Implementation

[0016] To make the objectives, technical solutions, and advantages of the embodiments of this utility model clearer, the technical solutions of the embodiments of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this utility model, not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this utility model.

[0017] Please see the appendix Figure 1This utility model provides an embodiment of a system for rapidly adjusting the parameters of coking wastewater, comprising an ammonia stripping tower 1, an ammonia water heat exchange pipe 12 connected to the ammonia stripping tower 1, an ammonia water heat exchanger 11 connected to the other end of the ammonia water heat exchange pipe 12, an ammonia water wastewater pump 10 and a residual ammonia water pipe 16 connected to the input end of the ammonia water heat exchanger 11, and the ammonia water wastewater pump 10 connected to the ammonia stripping tower 1; an ammonia water wastewater passage pipe 14 connected to the output end of the ammonia water heat exchanger 11, a first solenoid valve 15 fixedly connected to the ammonia water wastewater passage pipe 14, and a second temperature controller 13 fixedly connected to the output end of the ammonia water heat exchanger 11; a distributor 26 fixedly connected to the ammonia stripping tower 1, and a distributor 26 connected to... The system is connected to a desulfurization pipeline 2, a first return water pipeline 3, a first supply water pipeline 4, and a sodium hydroxide alkali solution pipeline 5. The sodium hydroxide alkali solution pipeline 5 is used to add sodium hydroxide alkali solution to the ammonia stripping tower 1, reacting it with the fixed ammonium salts in the ammonia stripping wastewater to convert them into volatile ammonia and the corresponding sodium salts. This conversion process helps to transform the fixed ammonia in the wastewater into more easily treated volatile ammonia. A reboiler 6 is connected to the ammonia stripping tower 1, and a low-pressure steam pipeline 7 and a steam condensate pipeline 8 are connected to the reboiler 6. A first temperature controller 9 is fixedly connected to the low-pressure steam pipeline 7, which is used to transport low-pressure steam to the reboiler 6 as a heat source for heating and vaporizing the liquid. The low-pressure steam can improve... To provide a more uniform heat distribution, allowing the liquid to reach its boiling point more quickly, the steam condensate pipe 8 is used to recover the steam condensate generated in the reboiler 6 and transport it to the corresponding treatment equipment; the ammonia water heat exchanger 11 is connected to a wastewater primary cooler 17, which is connected to a second water supply pipe 18 and a second water return pipe 19; the input end of the wastewater primary cooler 17 is fixedly connected to a second solenoid valve 27, and the output end of the wastewater primary cooler 17 is fixedly connected to a third temperature controller 20; the output end of the wastewater primary cooler 17 is connected to a wastewater secondary cooler 21, which is connected to a low-temperature water supply pipe 22 and a low-temperature water return pipe 21. Pipeline 23, the first water supply pipeline 4, the second water supply pipeline 18, and the low-temperature water supply pipeline 22 are used to transport circulating water to the heat exchange areas of the distributor 26, the first wastewater cooler 17, and the second wastewater cooler 21, respectively. The first return water pipeline 3, the second return water pipeline 19, and the low-temperature water return water pipeline 23 are used for the return of the cooling medium. The output end of the second wastewater cooler 21 is connected to an ammonia-eating wastewater pipeline 25. A fourth temperature controller 24 is fixedly connected to the ammonia-eating wastewater pipeline 25. The first temperature controller 9, the second temperature controller 13, the third temperature controller 20, and the fourth temperature controller 24 are used to monitor and control the temperature of the fluid to ensure that the temperature during the wastewater treatment process is within a predetermined range.

[0018] Working principle: When using this utility model, the ammonia stripping wastewater at the bottom of the ammonia stripping tower 1 is first indirectly heated by the reboiler 6, and the generated steam returns to the bottom of the tower as the heat source for ammonia stripping. The ammonia gas at the top of the ammonia stripping tower 1 is condensed by the fractionator 26 and then transported to the desulfurization or deammonium removal unit through the desulfurization pipeline 2. The ammonia stripping wastewater from the bottom of the ammonia stripping tower 1 is extracted by the ammonia stripping wastewater pump 10, and after exchanging heat with the residual ammonia water transported in the residual ammonia water pipeline 16 through the ammonia water heat exchanger 11, the residual ammonia water is sent back to the ammonia stripping tower 1 through the ammonia water heat exchanger 12. The ammonia stripping wastewater then passes through the wastewater first-stage cooler. After being cooled by the primary wastewater cooler 17 and the secondary wastewater cooler 21, the wastewater is discharged through the ammonia-containing wastewater pipeline 25 and sent to the wastewater treatment device. When any indicators exceed the standard, the system controls the second solenoid valve 27 to close and the first solenoid valve 15 to open. The ammonia-containing wastewater, after heat exchange in the ammonia water heat exchanger 11, no longer needs to be cooled by the primary wastewater cooler 17 and the secondary wastewater cooler 21. Instead, it returns to the remaining ammonia water system through the ammonia-containing wastewater transport pipe 14, avoiding the need to shut down the remaining ammonia water pump and the ammonia-containing wastewater pump 10, greatly shortening the adjustment time, and changing the destination of the ammonia-containing wastewater to prevent the excessive wastewater from affecting the biological treatment device. The system performs an impact test. The first water supply pipe 4, the second water supply pipe 18, and the low-temperature water supply pipe 22 are used to transport circulating water to the heat exchange areas of the distributor 26, the first wastewater cooler 17, and the second wastewater cooler 21, respectively. The first return water pipe 3, the second return water pipe 19, and the low-temperature water return water pipe 23 are used for the return of the cooling medium. The low-pressure steam pipe 7 is used to transport low-pressure steam to the reboiler 6 as a heat source for heating and vaporizing the liquid. Low-pressure steam can provide a more uniform heat distribution, allowing the liquid to reach its boiling point more quickly. The steam condensate pipe 8 is used to... The steam condensate generated in reboiler 6 is recovered and transported to the corresponding treatment equipment. Sodium hydroxide alkali pipeline 5 is used to add sodium hydroxide alkali to ammonia stripping tower 1, which reacts with the fixed ammonium salt in the ammonia stripping wastewater to convert it into volatile ammonia and the corresponding sodium salt. This conversion process helps to convert the fixed ammonia in the wastewater into more easily treated volatile ammonia. The first temperature controller 9, the second temperature controller 13, the third temperature controller 20 and the fourth temperature controller 24 are used to monitor and control the temperature of the fluid to ensure that the temperature in the wastewater treatment process is within the predetermined range.

[0019] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0020] The device embodiments described above are merely illustrative. The units described as separate components may or may not be physically separate. The components shown as units may or may not be physical units; that is, they may be located in one place or distributed across multiple network units. Some or all of the modules can be selected to achieve the purpose of this embodiment according to actual needs. Those skilled in the art can understand and implement this without any creative effort.

[0021] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and not to limit it. Although this utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this utility model.

Claims

1. A system for rapidly adjusting the parameters of coking wastewater, comprising an ammonia stripping tower (1), characterized in that: The ammonia stripping tower (1) is connected to an ammonia water heat exchange pipe (12), and the other end of the ammonia water heat exchange pipe (12) is connected to an ammonia water heat exchanger (11). The input end of the ammonia water heat exchanger (11) is connected to an ammonia stripping wastewater pump (10) and a remaining ammonia water pipe (16), and the ammonia stripping wastewater pump (10) is connected to the ammonia stripping tower (1). The output end of the ammonia water heat exchanger (11) is connected to an ammonia stripping wastewater transport pipe (14), and a first solenoid valve (15) is fixedly connected to the ammonia stripping wastewater transport pipe (14). The output end of the ammonia water heat exchanger (11) is fixedly connected to a second temperature controller (13).

2. The system for rapidly adjusting the parameters of coking wastewater according to claim 1, characterized in that: A shrinkage unit (26) is fixedly connected to the ammonia stripping tower (1), and the shrinkage unit (26) is connected to a desulfurization pipeline (2), a first return water pipeline (3), a first water supply pipeline (4), and a sodium hydroxide alkali solution pipeline (5).

3. The system for rapidly adjusting the parameters of coking wastewater according to claim 1, characterized in that: The ammonia stripping tower (1) is connected to a reboiler (6), and the reboiler (6) is connected to a low-pressure steam pipe (7) and a steam condensate pipe (8). The low-pressure steam pipe (7) is fixedly connected to a first temperature controller (9).

4. The system for rapidly adjusting the parameters of coking wastewater according to claim 1, characterized in that: The ammonia heat exchanger (11) is connected to a wastewater first-stage cooler (17), and the wastewater first-stage cooler (17) is connected to a second water supply pipe (18) and a second water return pipe (19).

5. The system for rapidly adjusting the parameters of coking wastewater according to claim 4, characterized in that: The input end of the wastewater primary cooler (17) is fixedly connected to a second solenoid valve (27), and the output end of the wastewater primary cooler (17) is fixedly connected to a third temperature controller (20).

6. The system for rapidly adjusting the parameters of coking wastewater according to claim 4, characterized in that: The output end of the wastewater primary cooler (17) is connected to the wastewater secondary cooler (21), and the wastewater secondary cooler (21) is connected to the low-temperature water supply pipe (22) and the low-temperature water return pipe (23).

7. The system for rapidly adjusting the parameters of coking wastewater according to claim 6, characterized in that: The output end of the wastewater two-stage cooler (21) is connected to an ammonia-steaming wastewater pipe (25), and a fourth temperature controller (24) is fixedly connected to the ammonia-steaming wastewater pipe (25).

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