Ammonia-phenol wastewater treatment device

Abstract

The utility model provides an ammonia-phenol wastewater treatment device which comprises a deacidification tower and a deamination tower which are sequentially connected, a deacidification tower reboiler and a deamination tower reboiler are arranged on the lower portion of the deacidification tower and the lower portion of the deamination tower respectively, the deamination tower is connected with multiple-effect evaporation devices, at least one effect evaporation device in the multiple-effect evaporation devices is connected with the deamination tower reboiler, and the deamination tower reboiler is connected with the deamination tower reboiler. The bottom of the last-effect evaporation device is connected with the reduction phase splitter; the multi-effect evaporation device is matched with the reduction phase splitter to replace a traditional extraction dephenolization process in a multi-effect evaporation concentration and phenol sodium salt reduction mode, the effluent index is better guaranteed, the dephenolization device technological process is shortened, operation is easy and easy to control, operation is more stable, the process does not need an extraction agent, the safety level is low, operation is safer, and the method is suitable for industrial production. And the low steam unit consumption can be guaranteed, and the energy-saving effect is achieved.

Description

Technical Field

[0001] This application relates to the technical field of chemical equipment, and particularly relates to an apparatus for treating phenol-ammonia wastewater. Background Art

[0002] Phenol-ammonia wastewater mainly comes from the wastewater generated in processes such as coal pyrolysis, coal-to-oil, and deep processing of coal tar. This type of wastewater contains a large amount of pollutants such as phenol, ammonia, sulfides, and cyanides. Among them, the phenol content is as high as 5000 - 15000 mg / L, and the COD is as high as 20000 - 50000 mg / L. The water quality is very complex and belongs to toxic and difficult-to-degrade industrial wastewater. This wastewater must first be pretreated with a phenol-ammonia recovery device to remove and recover phenol, ammonia, oil, and acidic gas in the wastewater before effectively reducing the biological toxicity of the wastewater, so as to meet the water intake conditions of the biochemical device.

[0003] Currently, the phenol-ammonia recovery device mainly adopts the methods of stripping purification and extraction to recover substances such as ammonia and phenol in the wastewater as valuable by-products. These by-products can be sold externally to reduce the operating cost of wastewater treatment and at the same time reduce the difficulty of biochemical treatment of wastewater. However, the extraction process has a long flow, complex operation, and requires controlling multiple operating parameters, such as solvent type, ratio, temperature, pressure, etc. The difficulty is relatively large, and improper operation is likely to cause a decrease in the effluent index. Since phenol substances have biological toxicity, there is a possibility of causing the entire subsequent biochemical device to break down, and this process generally has problems such as high energy consumption and large investment. The stripping purification process has high energy consumption. The stripping process requires a large amount of heat energy to achieve the separation and purification of wastewater, which will lead to an increase in operating costs. In large-scale industrial treatment, the energy consumption brought by continuous high-temperature steam supply cannot be ignored.

[0004] For example, in the patent application with the application number: CN201210145137.7, a method for recycling and treating high-concentration phenol-ammonia wastewater discloses a technical solution, which mainly includes the following steps: First, the high-concentration phenol-ammonia wastewater from which suspended matter and tar have been removed is saturatedly absorbed by acidic gas. After the pH value of the wastewater decreases, it enters the extraction tower for continuous countercurrent extraction. The raffinate phase after extraction is subjected to deacidification, deammoniation, and stripping solvent using a single-column pressurized stripping process. Alkali is added to the side line of the acid water stripping tower, and acidic gas phase and extraction agent are discharged from the top of the tower. Ammonia gas is obtained after three-stage partial condensation from the lower side line. The extraction phase after extraction enters the rectifying phenol tower to recover the extraction agent, and at the same time, by-product crude phenol is obtained. The acidic gas used in the present invention is generated during the wastewater treatment process, and the internal circulation of the acidic gas achieves the purpose of energy conservation and environmental protection. And during the single-column stripping process, deacidification, deammoniation, and stripping solvent are simultaneously realized, which can effectively treat high-concentration phenol-ammonia wastewater, recover crude phenol and ammonia at the same time, and the effluent can meet the requirements of subsequent conventional biochemical treatment, so that the final wastewater reaches the standard for discharge. This application can effectively treat high-concentration phenol-ammonia wastewater and recover crude phenol and ammonia at the same time. However, this application has the following disadvantages:

[0005] 1. High energy consumption, without utilizing the heat of the process;

[0006] 2. Complex process: The treatment method of this patent involves multiple steps and equipment, such as acid gas absorption tower, extraction tower, acid water stripping tower, etc., and the process flow is relatively complex.

[0007] In summary, in the current situation where energy prices remain high and environmental protection requirements are strict, the phenolic ammonia sewage treatment industry urgently needs energy-saving and efficient treatment methods. Therefore, a new technical solution is needed to solve the above technical problems. Utility Model Content

[0008] This application provides a phenolic ammonia wastewater treatment device, including a deacidification tower and a deammoniation tower connected in sequence. Reboilers of the deacidification tower and the deammoniation tower are respectively arranged at the lower parts of the deacidification tower and the deammoniation tower. The deammoniation tower is connected with a multi-effect evaporation device, and at least one effect evaporation device in the multi-effect evaporation device is connected with the reboiler of the deammoniation tower. The bottom of the last effect evaporation device is connected with a reduction phase separator.

[0009] As a preferred solution, each effect evaporation device includes a heating chamber and an evaporation chamber. The heating chamber includes a shell side and a tube side; wherein, the tube side inlet of the heating chamber of the first effect evaporation device is connected with the deammoniation tower, the tube side outlet of the heating chamber of the first effect evaporation device is connected with the evaporation chamber of the first effect evaporation device, and the bottom material side of the evaporation chamber of the first effect evaporation device is respectively connected with the tube side inlet of the heating chamber of the next effect and the tube side inlet of the heating chamber of the first effect; the top of the evaporation chamber of the first effect evaporation device is connected with the shell side inlet of the heating chamber of the next effect evaporation device; the bottom material side of the evaporation chamber of the last effect evaporation device is respectively connected with the reduction phase separator and the tube side inlet of the heating chamber of the last effect evaporation device; and the top of at least one evaporation chamber is connected with the reboiler of the deammoniation tower.

[0010] As a preferred solution, a feed pipeline is arranged on one side of the deacidification tower, and the feed pipeline is also connected with the upper part of the deacidification tower through a second feed pipeline. The second feed pipeline passes through a primary condenser and a raw material secondary preheater.

[0011] As a preferred solution, a raw material feed pump is arranged on the feed pipeline.

[0012] As a preferred solution, the bottom of the deacidification tower is connected with the deammoniation tower through a deacidification tower bottom product extraction pipeline, and the raw material secondary preheater is arranged on the deacidification tower bottom product extraction pipeline.

[0013] As a preferred solution, the top of the deammoniation tower is connected to a partial condenser through a deammoniation tower top product pipeline, and the first-stage condenser is arranged on the deammoniation tower top product pipeline. An ammonia water product pipeline is arranged at the top of the partial condenser, and a second-stage condenser is arranged on the ammonia water product pipeline. The bottom of the partial condenser is connected to the upper part of the deammoniation tower through a deammoniation tower reflux pipeline, and a reflux pump is arranged on the deammoniation tower reflux pipeline.

[0014] As a preferred solution, the bottom of the deammoniation tower is connected to the tube side inlet of the heating chamber of the first-effect evaporation device through a deammoniation tower bottom product pipeline, and a multi-effect first-stage preheater and a multi-effect second-stage preheater are sequentially arranged on the deammoniation tower bottom product pipeline.

[0015] As a preferred solution, the multi-effect evaporation device adopts a triple-effect evaporation device. The triple-effect evaporation device includes a first-effect heating chamber. The tube side outlet at the top of the first-effect heating chamber is connected to the upper middle part of the first-effect evaporation chamber. The shell side inlet of the first-effect heating chamber is connected to a steam supply pipeline, and the shell side outlet of the first-effect heating chamber is connected to a steam condensate product pipeline. The top of the first-effect evaporation chamber is connected to the shell side inlet of the second-effect heating chamber. The material side at the bottom of the first-effect evaporation chamber is respectively connected to the tube side inlet of the first-effect heating chamber and the tube side inlet of the second-effect heating chamber. The tube side outlet at the top of the second-effect heating chamber is connected to the upper middle part of the second-effect evaporation chamber. The shell side outlet on one side of the second-effect heating chamber is connected to a wastewater product pipeline. The top of the second-effect evaporation chamber is connected to the shell side inlet of the third-effect heating chamber. The material side at the bottom of the second-effect evaporation chamber is respectively connected to the tube side inlet at the bottom of the second-effect heating chamber and the tube side inlet at the bottom of the third-effect heating chamber. The top of the third-effect heating chamber is connected to the upper middle part of the third-effect evaporation chamber. The shell side outlet on one side of the third-effect heating chamber is connected to a wastewater product pipeline. The top of the third-effect evaporation chamber is connected to a deammoniation tower reboiler, and the bottom of the third-effect evaporation chamber is respectively connected to the tube side inlet at the bottom of the third-effect heating chamber and a reduction phase separator.

[0016] As a preferred solution, a multiple-effect evaporation device is a four-effect evaporation device. The four-effect evaporation device includes a first-effect heating chamber. The tube-side outlet at the top of the first-effect heating chamber is connected to the upper middle part of the first-effect evaporation chamber. A steam supply pipeline is connected to the shell-side inlet of the first-effect heating chamber, and a steam condensate extraction pipeline is connected to the shell-side outlet of the first-effect heating chamber. The top of the first-effect evaporation chamber is connected to the shell-side inlet of the second-effect heating chamber. The material side at the bottom of the first-effect evaporation chamber is connected to the tube-side inlet at the bottom of the first-effect heating chamber and the tube-side inlet at the bottom of the second-effect heating chamber. The top of the second-effect heating chamber is connected to the upper middle part of the second-effect evaporation chamber. The shell-side outlet on one side of the second-effect heating chamber is connected to a wastewater extraction pipeline. The top of the second-effect evaporation chamber is connected to the shell-side inlet of the third-effect heating chamber. The material side at the bottom of the second-effect evaporation chamber is connected to the tube-side inlet at the bottom of the second-effect heating chamber and the tube-side inlet at the bottom of the third-effect heating chamber. The top of the third-effect heating chamber is connected to the upper middle part of the third-effect evaporation chamber. The shell-side outlet on one side of the third-effect heating chamber is connected to a wastewater extraction pipeline. The top of the third-effect evaporation chamber is connected to a reboiler of an ammonia stripping tower and is also connected to the shell-side inlet of the fourth-effect heating chamber. The material side at the bottom of the third-effect evaporation chamber is connected to the tube-side inlet at the bottom of the third-effect heating chamber and the tube-side inlet at the bottom of the fourth-effect heating chamber. The top of the fourth-effect heating chamber is connected to the fourth-effect evaporation chamber. The shell-side outlet on one side of the fourth-effect heating chamber is connected to a wastewater extraction pipeline. The top of the fourth-effect evaporation chamber is connected to a wastewater extraction pipeline. The material side at the bottom of the fourth-effect evaporation chamber is respectively connected to the tube-side inlet at the bottom of the fourth-effect heating chamber and a reduction phase separator.

[0017] As a preferred solution, the steam condensate extraction pipeline passes through a multiple-effect secondary preheater.

[0018] As a preferred solution, the wastewater extraction pipeline passes through a multiple-effect primary preheater.

[0019] As a preferred solution, the ammonia stripping tower adopts a plate column, and an alkali addition port is arranged below the feed inlet of the ammonia stripping tower.

[0020] This application has the following advantages:

[0021] 1. By using a multiple-effect evaporation device and cooperating with a reduction phase separator, the method of multiple-effect evaporation concentration and phenolate reduction is adopted to replace the traditional extraction phenol removal process. The effluent index is more guaranteed, the process flow of the phenol removal device is shortened, the operation is simpler and easier to control, the operation is more stable, and this process does not require an extractant, has a low safety level, and is safer to operate;

[0022] 2. When the ammonia stripping tower operates under negative pressure, the ammonia stripping efficiency is higher, the ammonia nitrogen index of the effluent from the device is reduced, and the subsequent biochemical treatment pressure is relieved; however, the ammonia stripping tower can also operate under positive pressure;

[0023] 3. Ensure low steam consumption and achieve energy saving: Use the secondary steam from one effect of the multi-effect evaporation as a heat source to heat the deamination tower reboiler, realize thermal coupling between the deamination and dephenolization processes, and reduce the steam consumption of wastewater treatment;

[0024] 4. The process is simple, and the treatment equipment is less than that of steam stripping treatment of acetaminophen wastewater, which simplifies the steps of acetaminophen wastewater treatment. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is a structural schematic diagram of the first embodiment of the present application;

[0026] Figure 2 It is a structural diagram of Embodiment 2 of the present application;

[0027] 1. Deacidification tower; 2. Deamination tower; 3. Feed pipeline; 4. Feed pump; 5. Feed pipeline II; 6. Primary condenser; 7. Secondary raw material preheater; 8. Deacidification tower kettle extraction pipeline; 9. Deamination tower top extraction pipeline; 10. Partial condenser; 11. Ammonia extraction pipeline; 12. Secondary condenser; 13. Deamination tower reflux pipeline; 14. Reflux pump; 15. Deamination tower kettle extraction pipeline; 16. Multi-effect primary preheater; 17, multi-effect two-stage preheater; 18, deacidification tower reboiler; 19, deamination tower reboiler; 20, reduction phase separator; 21, reducing agent feed pipeline; 22, phenol oil extraction pipeline; 23, non-condenser extraction pipeline; 24, reduction phase separator tower kettle extraction pipeline; 25, first-effect heating chamber; 26, first-effect evaporation chamber; 27, steam condensate extraction pipeline; 28, first-effect evaporation chamber top extraction pipeline; 29, second 1. 1-effect heating chamber; 2. 1-effect evaporation chamber bottom extraction pipeline; 3. 2-effect evaporation chamber; 3. 2-effect steam pipeline; 3. 3-effect wastewater pipeline; 3. 3-effect wastewater extraction pipeline; 3. 3-effect heating chamber; 3. 2-effect evaporation chamber bottom extraction pipeline; 3. 3-effect evaporation chamber; 3. 3-effect steam pipeline; 4 ... 2. The production pipeline at the bottom of the three-effect evaporation chamber; 43. The pipeline at the bottom of the three-effect evaporation chamber; 44. The production pipeline 1 at the top of the three-effect evaporation chamber; 45. The four-effect heating chamber; 46. The four-effect evaporation chamber; 47. The four-effect steam pipeline; 48. The production pipeline at the top of the four-effect evaporation chamber; 49. The last-effect condenser; 50. The production pipeline at the bottom of the four-effect evaporation chamber; 51. The pipeline at the bottom of the four-effect evaporation chamber; 52. The steam heating pipeline; 53. The alkali addition port. DETAILED DESCRIPTION

[0028] The following is combined with Figure 1 , Figure 2 The specific implementation of the utility model is described in detail. It should be noted that the specific implementation described here is only used to illustrate and explain the utility model, and is not used to limit the utility model.

[0029] Example 1:

[0030] This embodiment provides an acetaminophen wastewater treatment device, which includes a deacidification tower 1 and a deammoniation tower 2 connected in sequence. A feed pipeline 3 is arranged on one side of the deacidification tower 1, and a raw material feed pump 4 is arranged on the feed pipeline 3. The feed pipeline 3 is connected to the upper middle part of the deacidification tower 1 through a second feed pipeline 5. The second feed pipeline 5 passes through a primary condenser 6 and a secondary raw material preheater 7. Part of the material enters the upper part of the deacidification tower 1 directly through the feed pipeline 3, and part enters the middle part of the deacidification tower 1 after passing through the primary condenser 6 and the secondary raw material heat exchanger 7; the bottom of the deacidification tower 1 is connected to the deammoniation tower 2 through a deacidification tower bottom product extraction pipeline 8, and the secondary raw material preheater 7 is arranged on the deacidification tower bottom product extraction pipeline 8; the deammoniation tower 2 adopts a negative pressure ammonia distillation process, and the top operating pressure is -10 to -90 Kpa. Negative pressure operation can improve the ammonia removal efficiency, reduce the ammonia nitrogen index of the device effluent, and reduce the subsequent biochemical treatment pressure; the deammoniation tower 2 adopts a plate tower in the prior art, and an alkali addition port 53 is arranged below the feed port of the deammoniation tower 2. More preferably, the alkali addition port 53 is arranged at the position corresponding to the 4th to 5th tower plates below the feed port; the top of the deammoniation tower 2 is connected to a partial condenser 10 through a deammoniation tower top product extraction pipeline 9, and the primary condenser 6 is arranged on the deammoniation tower top product extraction pipeline 9. An ammonia water extraction pipeline 11 is arranged at the top of the partial condenser 10, and a secondary condenser 12 is arranged on the ammonia water extraction pipeline 11. The bottom of the partial condenser 10 is connected to the upper part of the deammoniation tower 2 through a deammoniation tower reflux pipeline 13, and a reflux pump 14 is arranged on the deammoniation tower reflux pipeline 13. The bottom deammoniation tower bottom product extraction pipeline 15 of the deammoniation tower 2 is connected to the tube side inlet of the heating chamber of the first effect evaporation device, and a multi-effect primary preheater 16 and a multi-effect secondary preheater 17 are arranged in sequence on the deammoniation tower bottom product extraction pipeline 15.

[0031] A deacidification tower 1 and a deammoniation tower 2 are respectively provided with a deacidification tower reboiler 18 and a deammoniation tower reboiler 19 at their lower parts. The deacidification tower reboiler 18 is directly heated by 0.5 MPA steam; the deammoniation tower 2 is connected to a multi-effect evaporation device, where the multi-effect can be two-effect, three-effect, four-effect or five-effect concentration, etc. At least one evaporation device in the multi-effect evaporation device is connected to the deammoniation tower reboiler 19 to realize that the secondary steam of the multi-effect evaporation device heats the bottom of the deammoniation tower 2 to achieve thermal coupling, thereby reducing the steam unit consumption for wastewater treatment; the bottom of the last-effect evaporation device is connected to a reduction phase separator 20. A reducing agent feed pipeline 21 is arranged on one side of the reduction phase separator 20. A phenol oil extraction pipeline 22 is arranged at the upper part of the reducing agent feed pipeline 21. A non-condensable gas extraction pipeline 23 is arranged at the top of the reduction phase separator 20. A reduction phase separator bottom extraction pipeline 24 is arranged at the bottom of the reduction phase separator 20. The reduction phase separator 20 uses a reducing agent to reduce sodium phenolate to phenol oil. The phenol oil is separated from the water layer. The upper-layer phenol oil is extracted as a product, and the lower-layer water phase is sent to other devices for further treatment; acidic substances are used as reducing agents for sodium phenolate. The acidic substances are various substances with stronger acidity than phenols such as carbon dioxide and hydrochloric acid. Specific details are not elaborated here, and technicians can make corresponding selections according to specific situations.

[0032] The evaporation device includes a heating chamber and an evaporation chamber. The heating chamber includes a shell side and a tube side. The tube side is the internal channel of the heat exchange tubes in the heating chamber, and the shell side refers to the space between the outside of the heat exchange tubes in the heating chamber and the shell; the tube side inlet of the heating chamber of the first-effect evaporation device is connected to the deammoniation tower 2, the tube side outlet of the heating chamber of the first-effect evaporation device is connected to the evaporation chamber of the first-effect evaporation device, and the bottom material side of the evaporation chamber of the first-effect evaporation device is respectively connected to the tube side inlet of the next-effect heating chamber and the tube side inlet of the first-effect heating chamber; the top of the evaporation chamber of the first-effect evaporation device is connected to the shell side inlet of the heating chamber of the next-effect evaporation device; the bottom material side of the evaporation chamber of the last-effect evaporation device is respectively connected to the reduction phase separator 20 and the tube side inlet of the heating chamber of the last-effect evaporation device; at least one evaporation chamber is connected to the deammoniation tower reboiler 19, and the secondary steam at the top of the evaporation chamber provides heat for the deammoniation tower reboiler 19.

[0033] In this embodiment, the multi-effect evaporation device adopts a triple-effect evaporation device. The triple-effect evaporation device includes a first-effect heating chamber 25. The tube-side outlet at the top of the first-effect heating chamber 25 is connected to the upper middle part of the first-effect evaporation chamber 26. The shell-side inlet of the first-effect heating chamber 25 is connected to a steam supply pipeline 52, and the shell-side outlet of the first-effect heating chamber 25 is connected to a steam condensate extraction pipeline 27. The steam condensate extraction pipeline 27 passes through the multi-effect secondary preheater 17. The top of the first-effect evaporation chamber 26 is connected to the shell-side inlet of the second-effect heating chamber 29 through a first-effect evaporation chamber top extraction pipeline 28. The material side at the bottom of the first-effect evaporation chamber 26 is respectively connected to the tube-side inlet of the first-effect heating chamber 25 and the tube-side inlet of the second-effect heating chamber 29 through a first-effect evaporation chamber bottom extraction pipeline 30. The tube-side outlet at the top of the second-effect heating chamber 29 is connected to the upper middle part of the second-effect evaporation chamber 31. The shell-side outlet on one side of the second-effect heating chamber 29 is connected to a waste water extraction pipeline 34 through a second-effect steam pipeline 32 and a waste water main pipeline 33. The waste water extraction pipeline 34 passes through the multi-effect primary preheater 16. The top of the second-effect evaporation chamber 31 is connected to the upper middle part of the third-effect heating chamber 36 through a second-effect evaporation chamber top extraction pipeline 35. The material side at the bottom of the second-effect evaporation chamber 31 is respectively connected to the tube-side inlet at the bottom of the second-effect heating chamber 29 and the tube-side inlet at the bottom of the third-effect heating chamber 36 through a second-effect evaporation chamber bottom extraction pipeline 37. The top of the third-effect heating chamber 36 is connected to the upper middle part of the third-effect evaporation chamber 38. The shell-side outlet on one side of the third-effect heating chamber 36 is connected to a waste water extraction pipeline 34 through a third-effect steam pipeline 39 and a waste water main pipeline 33. The top of the third-effect evaporation chamber 38 is connected to the reboiler 19 of the deammoniation tower through a third-effect evaporation chamber top extraction pipeline 40. The output end of the reboiler 19 of the deammoniation tower is connected to a waste water extraction pipeline 34 through an output pipeline 41. The material side at the bottom of the third-effect evaporation chamber 38 is respectively connected to the tube-side inlet at the bottom of the third-effect heating chamber 36 and a reduction phase separator 20 through a third-effect evaporation chamber bottom extraction pipeline 42 and a third-effect evaporation chamber bottom kettle pipeline 43.

[0034] The working principle of this embodiment is as follows:

[0035] Part of the wastewater directly enters the top of the deacidification tower 1, and part of it enters the upper part of the deacidification tower 1 after being preheated by the primary condenser 6 and the raw material secondary preheater 7 to remove the sulfide-containing components; the wastewater material at the bottom of the deacidification tower 1 enters the deammoniation tower 2, and the deammoniation tower 2 removes ammonia nitrogen from the wastewater. Then, the desulfurized and deammoniated wastewater in the deammoniation tower 2 exchanges heat with the multi-effect primary preheater 16 and the multi-effect secondary preheater 17 and enters the first-effect heating chamber 25. After being heated by steam in the first-effect heating chamber 25, first-effect secondary steam is generated in the first-effect evaporation chamber 26, and the steam pressure is adjusted according to the actual situation. The first-effect secondary steam enters the second-effect heating chamber 29 to exchange heat with the second-effect material, and the secondary steam generated in the second-effect evaporation chamber 31 enters the third-effect heating chamber 36 to exchange heat with the third-effect material. The secondary steam generated in the third-effect evaporation chamber 38 is used as a heat source to supply heat to the deammoniation tower reboiler 19, realizing the heat coupling between the multi-effect evaporation and the deammoniation tower 2; the condensate of the first-effect heating chamber 25 is collected separately and sent out as steam condensate; the secondary steam condensate extracted from the second-effect heating chamber 29 and the third-effect heating chamber 36 is combined, exchanges heat with the bottom material of the deammoniation tower 2 through the multi-effect primary preheater 16, and then is sent to the biochemical system for further treatment. The evaporation mother liquor extracted from the third-effect evaporation chamber 38 enters the reduction phase separator 20, and the sodium phenolate is reduced to phenol oil by the reducing agent. The phenol oil is phase-separated from the water layer. The upper-layer phenol oil is extracted as a product, and the lower-layer water phase is sent to other devices for separate treatment.

[0036] Example 2:

[0037] The difference between this embodiment and the first embodiment is that the multiple-effect evaporation device in this embodiment adopts a four-effect evaporation device. The four-effect evaporation device includes a first-effect heating chamber 25. The tube-side outlet at the top of the first-effect heating chamber 25 is connected to the upper middle part of the first-effect evaporation chamber 26. A steam supply pipeline 52 is connected to the shell-side inlet of the first-effect heating chamber 25, and a steam condensate extraction pipeline 27 is connected to the shell-side outlet of the first-effect heating chamber 25. The steam condensate extraction pipeline 27 passes through the multiple-effect secondary preheater 17. The top of the first-effect evaporation chamber 26 is connected to the shell-side inlet of the second-effect heating chamber 29 through the first-effect evaporation chamber top extraction pipeline 28. The material side at the bottom of the first-effect evaporation chamber 26 is respectively connected to the tube-side inlet at the bottom of the first-effect heating chamber 25 and the tube-side inlet at the bottom of the second-effect heating chamber 29 through the first-effect evaporation chamber bottom extraction pipeline 30. The tube-side outlet at the top of the second-effect heating chamber 29 is connected to the upper middle part of the second-effect evaporation chamber 31. The shell-side outlet on one side of the second-effect heating chamber 29 is connected to the wastewater extraction pipeline 34 through the second-effect steam pipeline 32 and the wastewater main pipeline 33. The wastewater extraction pipeline 34 passes through the multiple-effect primary preheater 16. The top of the second-effect evaporation chamber 31 is connected to the shell-side inlet of the third-effect heating chamber 36 through the second-effect evaporation chamber top extraction pipeline 35. The material side at the bottom of the second-effect evaporation chamber 31 is respectively connected to the tube-side inlet at the bottom of the second-effect heating chamber 29 and the tube-side inlet at the bottom of the third-effect heating chamber 36 through the second-effect evaporation chamber bottom extraction pipeline 37. The tube-side outlet at the top of the third-effect heating chamber 36 is connected to the upper middle part of the third-effect evaporation chamber 38. The shell-side outlet on one side of the third-effect heating chamber 36 is connected to the wastewater extraction pipeline 34 through the third-effect steam pipeline 39 and the wastewater main pipeline 33. The top of the third-effect evaporation chamber 38 is connected to the reboiler 19 of the deammoniation tower through the third-effect evaporation chamber top extraction pipeline 40. The top of the third-effect evaporation chamber 38 is also connected to the shell-side inlet of the fourth-effect heating chamber 45 through the third-effect evaporation chamber top extraction pipeline 44. The material side at the bottom of the third-effect evaporation chamber 38 is respectively connected to the tube-side inlet at the bottom of the third-effect heating chamber 36 and the tube-side inlet at the bottom of the fourth-effect heating chamber 45 through the third-effect evaporation chamber bottom extraction pipeline 42. The tube-side outlet at the top of the fourth-effect heating chamber 45 is connected to the fourth-effect evaporation chamber 46. The shell-side outlet on one side of the fourth-effect heating chamber 45 is connected to the wastewater extraction pipeline 34 through the fourth-effect steam pipeline 47 and the wastewater main pipeline 33. The top of the fourth-effect evaporation chamber 46 is connected to the wastewater main pipeline 33 through the fourth-effect evaporation chamber top extraction pipeline 48. A final-effect condenser 49 is arranged on the fourth-effect evaporation chamber top extraction pipeline 48. The gas phase extracted from the fourth-effect evaporation chamber 46 is condensed by the final-effect condenser 49 and then discharged as wastewater. The material side at the bottom of the fourth-effect evaporation chamber 46 is respectively connected to the tube-side inlet at the bottom of the fourth-effect heating chamber 45 and the reduction phase separator 20 through the fourth-effect evaporation chamber bottom extraction pipeline 50 and the fourth-effect evaporation chamber bottom kettle pipeline 51.

[0038] The working principle of this embodiment is as follows:

[0039] Part of the wastewater directly enters the top of the deacidification tower 1, and part of it enters the upper part of the deacidification tower 1 after being preheated by the primary condenser 6 and the raw material secondary preheater 7 to remove the sulfide-containing components; the wastewater material at the bottom of the deacidification tower 1 enters the deammoniation tower 2, and the deammoniation tower 2 removes ammonia nitrogen from the wastewater. Then, the desulfurized and deammoniated wastewater in the deammoniation tower 2 exchanges heat with the multi-effect primary preheater 16 and the multi-effect secondary preheater 17 and enters the first-effect heating chamber 25. The first-effect heating chamber 25 is heated by 0.5 MPA live steam to generate first-effect secondary steam in the first-effect evaporation chamber 26. The first-effect secondary steam enters the second-effect heating chamber 29 to exchange heat with the second-effect material. The secondary steam generated in the second-effect evaporation chamber 31 enters the third-effect heating chamber 36 to exchange heat with the third-effect material. Part of the secondary steam generated in the third-effect evaporation chamber 38 is used as a heat source to supply heat to the deammoniation tower reboiler 19, and part of it enters the fourth-effect heating chamber 45 to exchange heat with the fourth-effect material. The secondary steam in the fourth-effect evaporation chamber 46 is condensed by the final-effect condenser 49 and merged with the secondary steam condensate extracted from the second-effect heating chamber 29, the third-effect heating chamber 36, and the fourth-effect heating chamber 45. After exchanging heat with the bottom material of the deammoniation tower 2 through the multi-effect primary preheater 16, it is sent to the biochemical system for further treatment; the condensate in the first-effect heating chamber 25 is collected separately and sent out as steam condensate; the fourth-effect evaporation mother liquor extracted from the fourth-effect evaporation chamber 46 enters the reduction phase separator 20 to reduce the sodium phenolate to phenol oil using a reducing agent. The phenol oil is phase-separated from the water layer. The upper-layer phenol oil is extracted as a product, and the lower-layer water phase is sent to other devices for separate treatment.

[0040] In summary, due to the adoption of the above technical solutions, the present application has the following advantages:

[0041] 1. Using a multi-effect evaporation device and cooperating with a reduction phase separator, adopting the method of multi-effect evaporation concentration and sodium phenolate reduction to replace the traditional extraction phenol removal process, the effluent index is more guaranteed, the process flow of the phenol removal device is shortened, the operation is simpler and easier to control, the operation is more stable, and this process does not require an extractant, has a low safety level, and is safer to operate;

[0042] 2. When the deammoniation tower operates under negative pressure, the deammoniation efficiency is higher, the ammonia nitrogen index of the effluent from the device is reduced, and the subsequent biochemical treatment pressure is reduced; however, the deammoniation tower can also operate under positive pressure;

[0043] 3. Ensure a low steam specific consumption and achieve an energy-saving effect: Use the secondary steam of a certain effect in multi-effect evaporation as a heat source to supply heat to the deammoniation tower reboiler, realize the heat coupling between the deammoniation and phenol removal processes, and reduce the steam specific consumption of wastewater treatment;

[0044] 4. The process is simple, and there are fewer treatment devices than those for stripping and treating amino-phenol wastewater, simplifying the steps for treating amino-phenol wastewater.

[0045] The devices, connection relationships, etc. not specifically described above all belong to the prior art, and the present utility model will not specifically elaborate on them here.

[0046] The preferred embodiments of the present application have been described in detail above in conjunction with the accompanying drawings. However, the present application is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present application, various simple modifications can be made to the technical solutions of the present application, and these simple modifications all fall within the protection scope of the present application.

[0047] In addition, it should be noted that, among the various specific technical features described in the above specific embodiments, they can be combined in any appropriate manner without conflict. To avoid unnecessary repetition, various possible combination methods of the present application will not be described separately.

[0048] Furthermore, any combination can be made among various different embodiments of the present application, as long as it does not violate the idea of the present application, and it should also be regarded as the content disclosed in the present application.

Claims

1. An acetaminophen wastewater treatment device, comprising a deacidification tower (1) and a deamination tower (2) connected in sequence, wherein the lower parts of the deacidification tower (1) and the deamination tower (2) are respectively provided with a deacidification tower reboiler (18) and a deamination tower reboiler (19), characterized in that: The deamination tower (2) is connected to a multi-effect evaporation device, wherein at least one effect evaporation device in the multi-effect evaporation device is connected to a deamination tower reboiler (19), and the bottom of the last effect evaporation device is connected to a reduction phase separator (20).

2. A acetaminophen wastewater treatment device according to claim 1, characterized in that, Each effect evaporation device comprises a heating chamber and an evaporation chamber, wherein the heating chamber comprises a shell side and a tube side; wherein the tube side inlet of the heating chamber of the first effect evaporation device is connected to a deamination tower (2), the tube side outlet of the heating chamber of the first effect evaporation device is connected to the evaporation chamber of the first effect evaporation device, the bottom material side of the evaporation chamber of the first effect evaporation device is respectively connected to the tube side inlet of the next effect heating chamber and the tube side inlet of the first effect heating chamber; the top of the evaporation chamber of the first effect evaporation device is connected to the shell side inlet of the heating chamber of the next effect evaporation device; the bottom material side of the evaporation chamber of the last effect evaporation device is respectively connected to a reduction phase separator (20) and the tube side inlet of the heating chamber of the last effect evaporation device; wherein the top of at least one evaporation chamber is connected to a deamination tower reboiler (19).

3. A acetaminophen wastewater treatment device according to claim 1, characterized in that, A feed pipeline (3) is provided on one side of the deacidification tower (1), and the feed pipeline (3) is also connected to the upper part of the deacidification tower (1) through a second feed pipeline (5), and the second feed pipeline (5) passes through a primary condenser (6) and a secondary raw material preheater (7).

4. A acetaminophen wastewater treatment device according to claim 3, characterized in that, The bottom of the deacidification tower (1) is connected to the deammonification tower (2) via a deacidification tower kettle extraction pipeline (8), and the raw material secondary preheater (7) is arranged on the deacidification tower kettle extraction pipeline (8).

5. A acetaminophen wastewater treatment device according to claim 3, characterized in that, The top of the deamination tower (2) is connected to the partial condenser (10) via a deamination tower top extraction pipeline (9), the primary condenser (6) is arranged on the deamination tower top extraction pipeline (9), the top of the partial condenser (10) is provided with an ammonia water extraction pipeline (11), the ammonia water extraction pipeline (11) is provided with a secondary condenser (12), the bottom of the partial condenser (10) is connected to the upper part of the deamination tower (2) via a deamination tower reflux pipeline (13), and a reflux pump (14) is arranged on the deamination tower reflux pipeline (13).

6. A acetaminophen wastewater treatment device according to claim 2, characterized in that, The bottom of the deamination tower (2) is connected to the tube side inlet of the heating chamber of the first effect evaporation device through the deamination tower kettle extraction pipeline (15), and the deamination tower kettle extraction pipeline (15) is sequentially provided with a multi-effect primary preheater (16) and a multi-effect secondary preheater (17).

7. A acetaminophen wastewater treatment device according to claim 6, characterized in that, The multi-effect evaporation device adopts a triple-effect evaporation device, which comprises a first-effect heating chamber (25), wherein the tube side outlet at the top of the first-effect heating chamber (25) is connected to the middle and upper part of the first-effect evaporation chamber (26), the shell side inlet of the first-effect heating chamber (25) is connected to a steam heating pipeline (52), and the shell side outlet of the first-effect heating chamber (25) is connected to a steam condensate extraction pipeline (27); the top of the first-effect evaporation chamber (26) is connected to the shell side inlet of the second-effect heating chamber (29), and the material side of the bottom of the first-effect evaporation chamber (26) is respectively connected to the tube side inlet of the first-effect heating chamber (25) and the tube side inlet of the second-effect heating chamber (29); the tube side outlet at the top of the second-effect heating chamber (29) is connected to the middle and upper part of the second-effect evaporation chamber (31), and the second-effect heating chamber ( The shell side outlet on one side of the second-effect evaporation chamber (29) is connected to the wastewater extraction pipeline (34), the top of the second-effect evaporation chamber (31) is connected to the shell side inlet of the third-effect heating chamber (36), and the material side at the bottom of the second-effect evaporation chamber (31) is respectively connected to the tube side inlet at the bottom of the second-effect heating chamber (29) and the tube side inlet at the bottom of the third-effect heating chamber (36); the tube side outlet at the top of the third-effect heating chamber (36) is connected to the middle and upper part of the third-effect evaporation chamber (38), the shell side outlet on one side of the third-effect heating chamber (36) is connected to the wastewater extraction pipeline (34), the top of the third-effect evaporation chamber (38) is connected to the deamination tower reboiler (19), and the material side at the bottom of the third-effect evaporation chamber (38) is respectively connected to the tube side inlet at the bottom of the third-effect heating chamber (36) and the reduction phase separator (20).

8. A acetaminophen wastewater treatment device according to claim 6, characterized in that: The multiple-effect evaporation device adopts a four-effect evaporation device, which comprises a first-effect heating chamber (25), wherein the tube side outlet at the top of the first-effect heating chamber (25) is connected to the middle and upper part of the first-effect evaporation chamber (26), the shell side inlet of the first-effect heating chamber (25) is connected to a steam heating pipeline (52), and the shell side outlet of the first-effect heating chamber (25) is connected to a steam condensate extraction pipeline (27); the top of the first-effect evaporation chamber (26) is connected to the shell side inlet of the second-effect heating chamber (29), and the bottom of the first-effect evaporation chamber (26) is connected to the steam condensate extraction pipeline (27). The material side of the second effect evaporation chamber (31) is connected to the tube side inlet at the bottom of the first effect heating chamber (25) and the tube side inlet at the bottom of the second effect heating chamber (29); the tube side outlet at the top of the second effect heating chamber (29) is connected to the middle and upper part of the second effect evaporation chamber (31); the shell side outlet on one side of the second effect heating chamber (29) is connected to the wastewater extraction pipeline (34); the top of the second effect evaporation chamber (31) is connected to the shell side inlet of the third effect heating chamber (36); the material side of the bottom of the second effect evaporation chamber (31) is connected to the shell side inlet at the bottom of the second effect heating chamber (29); The tube side inlet is connected to the tube side inlet at the bottom of the triple-effect heating chamber (36); the tube side outlet at the top of the triple-effect heating chamber (36) is connected to the middle and upper part of the triple-effect evaporation chamber (38); the shell side outlet on one side of the triple-effect heating chamber (36) is connected to the wastewater extraction pipeline (34); the top of the triple-effect evaporation chamber (38) is connected to the deamination tower reboiler (19); the top of the triple-effect evaporation chamber (38) is also connected to the shell side inlet of the quadruple-effect heating chamber (45); the material side at the bottom of the triple-effect evaporation chamber (38) is connected to the triple-effect heating tower reboiler (19); The tube side inlet at the bottom of the chamber (36) is connected to the tube side inlet at the bottom of the four-effect heating chamber (45); the top of the four-effect heating chamber (45) is connected to the four-effect evaporation chamber (46); the shell side outlet on one side of the four-effect heating chamber (45) is connected to the wastewater extraction pipeline (34); the tube side outlet at the top of the four-effect evaporation chamber (46) is connected to the wastewater extraction pipeline (34); the material side at the bottom of the four-effect evaporation chamber (46) is respectively connected to the tube side inlet at the bottom of the four-effect heating chamber (45) and the reduction phase separator (20).

9. A acetaminophen wastewater treatment device according to claim 7 or 8, characterized in that: The steam condensate extraction pipeline (27) passes through the multi-effect secondary preheater (17).

10. A acetaminophen wastewater treatment device according to claim 7 or 8, characterized in that: The wastewater extraction pipeline (34) passes through a multi-effect primary preheater (16).

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