Energy-saving device of deamination tower

Abstract

The utility model provides a deamination tower energy-saving device which comprises a steam stripping deamination tower and a water scrubber, a heat exchange module is arranged on one side of the steam stripping deamination tower, two ammonia-containing wastewater pumps which are arranged side by side are arranged on one side of the heat exchange module, and two pipelines are arranged on a shell pass and a tube pass in the heat exchange module. According to the scheme, the steam condensate circulating pump of the reboiler of the steam stripping deamination tower is started, the steam condensate is sent back to the gas-liquid separation flash tank again, and circulating heat exchange is carried out again, so that cyclic utilization of the steam condensate is realized, and the effects of energy conservation and environmental protection are achieved. According to the scheme, steam generated by heat exchange at the top of a deamination tower enters a high-temperature-rise compressor through a low-temperature steam output pipeline, enters the top of an inner shell pass of a reboiler through a heat energy backflow pipeline after being compressed, exchanges heat with a material through the reboiler and is cooled into condensed liquid; and then the gas is conveyed to the gas-liquid separation tank again from an outlet in the bottom of the shell pass through a recovery pump for follow-up cyclic utilization.

Description

Technical Field

[0001] The utility model relates to the technical field of energy-saving of deamination towers, in particular to an energy-saving device for deamination towers. Background Art

[0002] Ammonia-containing wastewater is widely found in the chemical, pharmaceutical and metal processing industries. Untreated ammonia-nitrogen wastewater can cause eutrophication of water bodies, endangering the ecosystem and human health. In the production process of nickel-cobalt-manganese ternary precursors, ammonia water is widely used as a key complexing agent in the coprecipitation reaction stage to ensure Ni 2 +, Co2+, and Mn2+ can be uniformly and slowly precipitated to form high-quality composite hydroxides. However, this process inevitably produces a large amount of ammonia-containing wastewater, which is difficult and costly to treat, thus affecting the environmental compliance and economic benefits of the company.

[0003] Traditional deamination towers adjust the pH value of ammonia-containing wastewater and heat it for stripping, but their high energy consumption limits their practical application. By optimizing the energy-saving effect of the deamination tower, especially improving the recovery and utilization of the latent heat of the gas phase at the top of the tower, it is possible to reduce the consumption of raw steam, improve treatment efficiency, reduce enterprise operating costs and reduce environmental pollution.

[0004] In the ammonia wastewater industry, the application of energy-saving deamination towers not only solves the wastewater treatment problem, but also improves the market competitiveness of enterprises and achieves a win-win situation of economic and environmental benefits. Therefore, how to reduce the energy consumption of deamination towers and the treatment cost of ammonia wastewater has become an important issue that needs to be solved urgently. Utility Model Content

[0005] 1. Technical issues to be resolved

[0006] In view of the deficiencies in the prior art, the utility model provides an energy-saving device for a deamination tower, which solves the problems raised in the above-mentioned background technology.

[0007] (II) Technical solution

[0008] To achieve the above objectives, the utility model is implemented through the following technical solutions: a deammonification tower energy-saving device, including a stripping deammonification tower and a water washing tower, a heat exchange module is provided on one side of the stripping deammonification tower, two parallel ammonia-containing wastewater pumps are provided on one side of the heat exchange module, two pipelines are provided in the shell side and the tube side of the heat exchange module, the shell side and the tube side in the heat exchange module respectively play the role of output and input through the ammonia-containing wastewater pump, one side of the stripping deammonification tower is connected to an ammonia-containing wastewater input pipeline, the ammonia-containing wastewater input pipeline is connected to a feed pipeline, a reboiler is provided on one side of the stripping deammonification tower, the bottom of the reboiler is connected to the bottom of the stripping deammonification tower, the reboiler is connected to the side of the stripping deammonification tower to form an internal tube side pipeline.

[0009] Preferably, a falling film heat exchanger is provided on one side of the stripping and ammonia removal tower. A tower top pipeline is communicated between the top end of the stripping and ammonia removal tower and the side surface of the falling film heat exchanger. A gas-liquid separation flash tank is provided on the side surface of the falling film heat exchanger, and the side surface of the falling film heat exchanger is communicated with the gas-liquid separation flash tank through a pipeline.

[0010] Preferably, a pure water circulation pump is provided on one side of the gas-liquid separation flash tank. The pure water circulation pump is communicated with the bottom of the gas-liquid separation flash tank, and the output port on one side of the pure water circulation pump is connected to the interface on one side of the top end of the falling film heat exchanger.

[0011] Preferably, a gas-liquid separation tank is provided side by side on one side of the falling film heat exchanger. The bottom of the gas-liquid separation tank is communicated with the interface on one side of the top end of the stripping and ammonia removal tower, and a material circulation pump is communicated between the bottom of the gas-liquid separation tank and the stripping and ammonia removal tower.

[0012] Preferably, a steam condensate buffer tank is provided on one side of the gas-liquid separation tank. A steam condensate pump is provided on one side of the steam condensate buffer tank. The steam condensate pump is communicated with the bottom of the steam condensate buffer tank, and the other interface of the steam condensate pump is communicated with the upper side of the side surface of the gas-liquid separation flash tank.

[0013] Preferably, the pipe orifice on one side of the top of the gas-liquid separation tank is communicated with the bottom of the side surface of the falling film heat exchanger through a gasification connection pipeline. The tower top pipeline is communicated with the tube pass in the gasification connection pipeline to form a communicating pipeline, and an ammonia recovery pipeline for output is communicated with the top of the gas-liquid separation tank.

[0014] Preferably, a high temperature rise compressor is provided on one side of the gas-liquid separation flash tank. A steam output pipeline is communicated between the top of the gas-liquid separation flash tank and one side of the high temperature rise compressor. One interface of the high temperature rise compressor is communicated with a heat energy return pipeline. The heat energy return pipeline is communicated with the interface above the shell side of the reboiler, and the interface below the shell side of the reboiler is communicated with the pipe orifice above the side surface of the gas-liquid separation flash tank.

[0015] Preferably, a vacuum pump module is provided on one side of the steam condensate buffer tank, and the vacuum pump module is connected to the top of the steam condensate buffer tank.

[0016] Preferably, the two water washing towers are arranged side by side. A cooler is provided on one side of the water washing tower. The inlet of the cooler is communicated with the ammonia recovery pipeline and is connected to the interface below the side surface of one side of the water washing tower. An input water pipe is connected to the top of the side surface of the water washing tower. A connecting pipeline is communicated between the two side-by-side water washing towers. One end of the connecting pipeline is connected to the top interface of one side of the water washing tower, and the other end of the connecting pipeline is connected to the interface below the side surface of the other side of the water washing tower. An output pipeline is connected to the top end of the other side of the water washing tower.

[0017] (III) Beneficial Effects

[0018] The utility model provides an energy-saving device for an ammonia stripping tower, which has the following beneficial effects:

[0019] 1. In this solution, the steam condensate circulation pump is started to send the condensate back to the top of the falling film heat exchanger for secondary cyclic heat exchange work, and the cyclic utilization achieves the effects of energy conservation and environmental protection.

[0020] 2. In this solution, the ammonia gas produced by the ammonia stripping tower is output through the ammonia recovery pipeline, and the ammonia-containing wastewater after gas-liquid separation is refluxed and input into the stripping ammonia tower through the material circulation pump for subsequent secondary stripping, improving the utilization efficiency of ammonia nitrogen in the ammonia-containing wastewater.

[0021] 3. In this solution, the steam generated at the top of the ammonia stripping tower is introduced into the high-temperature compressor through the low-temperature steam transmission pipeline for compression, temperature increase and pressure boost, and then is transported to the top of the shell side of the reboiler through the heat energy reflux pipeline. After the steam exchanges heat with the material in the reboiler, it condenses into pure water, and then is transported to the gas-liquid separation tank through the outlet at the bottom of the shell side by the recovery pump for subsequent cyclic utilization. Description of the Drawings

[0022] Figure 1 It is a schematic diagram of the overall process connection of the components of the stripping ammonia tower of the utility model;

[0023] Figure 2 It is a schematic diagram of the process connection of the water washing tower of the utility model.

[0024] In the figure: 101, stripping ammonia tower; 102, reboiler; 103, gas-liquid separation tank; 104, material circulation pump; 105, heat energy reflux pipeline; 106, high-temperature rise compressor; 107, steam output pipeline; 108, gas-liquid separation flash tank; 109, falling film heat exchanger; 110, tower top pipeline; 111, heat exchange module; 112, ammonia-containing wastewater pump; 113, water washing tower; 114, ammonia-containing wastewater input pipeline; 115, cooler; 117, pure water circulation pump; 119, gasification connection pipeline; 120, ammonia recovery pipeline; 122, steam condensate pump; 123, steam condensate buffer tank; 124, connection pipeline; 125, vacuum pump module. Detailed Embodiments

[0025] The embodiment of the utility model provides an energy-saving device for an ammonia stripping tower, as Figure 1-2As shown in the figure, it includes a stripping and ammonia removal tower 101 and a water washing tower 113. One side of the stripping and ammonia removal tower 101 is provided with a heat exchange module 111. One side of the heat exchange module 111 is provided with two parallel ammonia-containing wastewater pumps 112. There are two pipelines in the shell side and the tube side of the heat exchange module 111. The shell side and the tube side in the heat exchange module 111 respectively play the roles of output and input through the ammonia-containing wastewater pumps 112. One side of the stripping and ammonia removal tower 101 is connected and provided with an ammonia-containing wastewater input pipeline 114. The ammonia-containing wastewater input pipeline 114 is connected with the feed pipeline. One side of the stripping and ammonia removal tower 101 is provided with a reboiler 102. The bottom of the reboiler 102 is connected with the bottom of the stripping and ammonia removal tower 101. The reboiler 102 is connected with the side of the stripping and ammonia removal tower 101, and the two form an internal tube side pipeline.

[0026] It should be further noted that the pipeline connected to the ammonia-containing wastewater pump 112 on the left is a heat exchange and temperature-raising pipeline, and the pipeline connected to the ammonia-containing wastewater pump 112 on the right is a material reflux pipeline. One side of the ammonia-containing wastewater pump 112 on the right is connected with the bottom of the stripping and ammonia removal tower 101 to play the role of reflux.

[0027] Furthermore, one side of the stripping and ammonia removal tower 101 is provided with a falling film heat exchanger 109. There is a tower top pipeline 110 connected between the top of the stripping and ammonia removal tower 101 and the side of the falling film heat exchanger 109. One side of the falling film heat exchanger 109 is provided with a gas-liquid separation flash tank 108. The falling film heat exchanger 109 and the gas-liquid separation flash tank 108 are connected through a pipeline.

[0028] Furthermore, one side of the gas-liquid separation flash tank 108 is provided with a pure water circulation pump 117. The pure water circulation pump 117 is connected with the bottom of the gas-liquid separation flash tank 108. One output port of the pure water circulation pump 117 is connected with one side interface at the top of the falling film heat exchanger 109.

[0029] It should be further noted that a liquid level detector is provided inside the gas-liquid separation flash tank 108, which can detect the liquid level height of the liquid inside the gas-liquid separation flash tank 108.

[0030] Furthermore, one side of the falling film heat exchanger 109 is provided with a gas-liquid separation tank 103. The bottom of the gas-liquid separation tank 103 is connected with one side interface at the top of the stripping and ammonia removal tower 101. A material circulation pump 104 is connected between the bottom of the gas-liquid separation tank 103 and the stripping and ammonia removal tower 101.

[0031] Furthermore, one side of the gas-liquid separation tank 103 is provided with a steam condensate buffer tank 123. One side of the steam condensate buffer tank 123 is provided with a steam condensate pump 122. The steam condensate pump 122 is connected with the bottom of the steam condensate buffer tank 123. The other interface of the steam condensate pump 122 is connected with the upper side of the side of the gas-liquid separation flash tank 108.

[0032] Further, the upper middle pipe orifice on the side of the gas-liquid separation tank 103 is communicated with the bottom of the side of the falling film heat exchanger 109 through a gasification connection pipe 119. The top pipe 110 is communicated with the tube side in the gasification connection pipe 119 to form a communicating pipeline. An ammonia recovery pipe 120 for output is connected to the top of the gas-liquid separation tank 103.

[0033] Further, a high-temperature rise compressor 106 is provided on one side of the gas-liquid separation flash tank 108. A steam output pipe 107 is connected between the top of the gas-liquid separation flash tank 108 and one side of the high-temperature rise compressor 106. One side interface of the high-temperature rise compressor 106 is connected with a heat energy return pipe 105. The heat energy return pipe 105 is communicated with the upper interface of the shell side of the reboiler 102. The lower interface of the shell side of the reboiler 102 is communicated with the upper middle pipe orifice on the side of the steam condensate buffer tank 123.

[0034] Further, a vacuum pump module 125 is provided on one side of the steam condensate buffer tank 123. The vacuum pump module 125 is connected to the top of the steam condensate buffer tank 123.

[0035] As Figure 2 shown, two water scrubbers 113 are arranged side by side. A cooler 115 is provided on one side of the water scrubber 113. The inlet of the cooler 115 is communicated with the ammonia recovery pipe 120. The cooler 115 is connected to the lower side interface of the side water scrubber. An input water pipe is connected to the top of the side of the water scrubber 113. A connection pipe 124 is connected between the two side-by-side water scrubbers 113. One end of the connection pipe 124 is connected to the top interface of one side water scrubber 113, and the other end of the connection pipe 124 is connected to the lower side interface of the other side water scrubber. An output pipe is connected to the top of the other side water scrubber.

[0036] It should be further noted that the liquid used for heat exchange in the shell side of the cooler 115 is circulating cooling water. The cooler 115 can heat-exchange the ammonia input from the ammonia recovery pipe 120 and then input it into the water scrubber 113 for spray recovery into ammonia water for convenient subsequent secondary utilization. The output pipe connected to the top of the side water scrubber is used to send the waste gas for subsequent treatment.

[0037] When using this solution, first connect the pipelines between the components according to the standards. At this time, the reaction bottom liquid is input into the stripping ammonia tower 101 through the ammonia-containing wastewater input pipeline 114. Then, the reaction bottom liquid is pumped into the ammonia-containing wastewater pump 112 on one side by the ammonia-containing wastewater pump 112 on the right, and then input into the top of the stripping ammonia tower 101 after passing through the heat exchange module 111 upwards. At this time, the ammonia-containing wastewater pump 112 on the other side inputs the ammonia-containing wastewater into the other side of the heat exchange module 111 and exchanges heat with the deammoniated liquid, achieving a preliminary heating reaction effect. At this time, the ammonia-containing wastewater after heat exchange is controlled within the deammoniation temperature, and the stripping gas-liquid mixture is input into the falling film heat exchanger 109 through the tower top pipeline 110. After the falling film heat exchange in the falling film heat exchanger 109, the stripping gas-liquid mixture is output and refluxed into the gas-liquid separation tank 103 through the gasification connection pipeline 119. The ammonia produced by deammoniation is output through the ammonia recovery pipeline 120, and the ammonia-containing wastewater separated by gas-liquid is refluxed into the stripping ammonia tower 101 through the material circulation pump 104 for subsequent secondary deammoniation.

[0038] At the same time, the pure water in the falling film heat exchanger 109 exchanges heat with the stripping gas-liquid mixture input from the shell side. At this time, the pure water gas-liquid mixture after heat exchange is input into the gas-liquid separation flash tank 108 through the connection with the gas-liquid separation flash tank 108 for gas-liquid separation. At the same time, a part of the pure water does not completely vaporize due to incomplete heat exchange and flows into the bottom of the falling film heat exchanger 109. Then, the pure water circulation pump 117 is started to pump the pure water back into the top of the falling film heat exchanger 109 for secondary circulating heat exchange work, achieving the effect of recycling the pure water, saving energy and protecting the environment. The pure water is re-input into the falling film heat exchanger 109 through the pure water circulation pump 117 for multiple heat exchange operations. Subsequently, the steam with heat energy is input into the high-temperature rise compressor 106 through the steam output pipeline 107 for temperature rise and pressure boost, and then input back into the top of the shell side of the reboiler 102 through the heat energy reflux pipeline 105. After being cooled into pure water liquid through the heat exchange in the reboiler 102, it is re-refluxed into the steam condensate buffer tank 123 through the bottom outlet of the shell side, and the steam condensate is re-output and refluxed into the gas-liquid separation flash tank 108 through the steam condensate pump 122 for subsequent recycling.

[0039] During the deammoniation process, the ammonia-containing wastewater in the stripping ammonia tower 101 is reheated and reboiled by the reboiler 102 on the side, and then refluxed into the stripping ammonia tower 101 to reach the appropriate temperature for deammoniation. The hot steam in the shell side of the reboiler 102 is heat-exchanged to achieve the effect of recycling heat energy, and thus the overall process flow becomes more energy-saving and environmentally friendly.

[0040] After the ammonia recovery pipeline 120 sends the ammonia generated by stripping and deammoniation into the cooler 115 for heat exchange, it enters the 2-4 stage water washing tower 113 for spray washing to directly generate ammonia water, which is convenient for subsequent recycling and utilization, thereby improving the material utilization rate of the process flow. At this time, after passing through the water washing tower 113 on one side, the ammonia passes through the connecting pipeline 124 again and enters the water washing tower 113 on the other side for series recovery, and the excess waste gas is discharged for subsequent treatment. When the ammonia water concentration in one side of the water washing tower 113 reaches 10%-15% by mass ratio, the connection between the cooler 115 and this water washing tower is disconnected by switching the valve, the ammonia water reaching the established concentration is discharged, and the ammonia is allowed to enter the water washing tower on the other side through the connecting pipeline 124 for continuous spray washing. The ammonia after spray washing returns to the original water washing tower for continuous recovery. When the ammonia water concentration in the water washing tower on the other side reaches the predetermined value, the connection method is switched again to make the ammonia re-enter the front water washing tower for spray recovery operation.

[0041] Although the embodiments of the present invention have been shown and described, for those of ordinary skill in the art, it can be understood that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principle and spirit of the present invention. The scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A deamination tower energy-saving device, comprising a stripping deamination tower (101) and a water washing tower (113), characterized in that: A heat exchange module (111) is provided on one side of the stripping deamination tower (101). Two parallel ammonia-containing wastewater pumps (112) are provided on one side of the heat exchange module (111). Two pipelines are provided in the shell side and the tube side of the heat exchange module (111). The shell side and the tube side of the heat exchange module (111) respectively play the role of output and input through the ammonia-containing wastewater pump (112). An ammonia-containing wastewater input pipeline (114) is provided on one side of the stripping deamination tower (101). The ammonia-containing wastewater input pipeline (114) is connected to the feed pipeline. A reboiler (102) is provided on one side of the stripping deamination tower (101). The bottom of the reboiler (102) is connected to the bottom of the stripping deamination tower (101). The reboiler (102) is connected to the side of the stripping deamination tower (101) to form an internal tube side pipeline.

2. A deamination tower energy-saving device according to claim 1, characterized in that: A falling film heat exchanger (109) is provided on one side of the stripping deamination tower (101), a tower top pipeline (110) is provided between the top of the stripping deamination tower (101) and the side of the falling film heat exchanger (109), a gas-liquid separation flash tank (108) is provided on the side of the falling film heat exchanger (109), and the side of the falling film heat exchanger (109) and the gas-liquid separation flash tank (108) are connected through a pipeline.

3. A deamination tower energy-saving device according to claim 2, characterized in that: A pure water circulation pump (117) is provided on one side of the gas-liquid separation flash tank (108). The pure water circulation pump (117) is connected to the bottom of the gas-liquid separation flash tank (108). An output port on one side of the pure water circulation pump (117) is connected to an interface on one side of the top of the falling film heat exchanger (109).

4. A deamination tower energy-saving device according to claim 3, characterized in that: A gas-liquid separation tank (103) is provided on one side of the falling film heat exchanger (109), and the bottom of the gas-liquid separation tank (103) is connected to an interface on one side of the top of the stripping deamination tower (101), and a material circulation pump (104) is provided between the bottom of the gas-liquid separation tank (103) and the stripping deamination tower (101).

5. A deamination tower energy-saving device according to claim 4, characterized in that: A steam condensate buffer tank (123) is provided on one side of the gas-liquid separation tank (103), and a steam condensate pump (122) is provided on one side of the steam condensate buffer tank (123). The steam condensate pump (122) is connected to the bottom of the steam condensate buffer tank (123), and the other side interface of the steam condensate pump (122) is connected to the upper side of the gas-liquid separation flash tank (108).

6. A deamination tower energy-saving device according to claim 5, characterized in that: The upper pipe opening in the middle of the side of the gas-liquid separation tank (103) is connected to the bottom of the side of the falling film heat exchanger (109) through a gasification connecting pipe (119), and the tower top pipe (110) is connected to the pipe path in the gasification connecting pipe (119) to form a connecting pipeline. The top of the gas-liquid separation tank (103) is connected to an output ammonia recovery pipe (120).

7. A deamination tower energy-saving device according to claim 6, characterized in that: A high temperature rise compressor (106) is provided on one side of the gas-liquid separation flash tank (108); a steam output pipeline (107) is provided at the top of the gas-liquid separation flash tank (108) and is connected to one side of the high temperature rise compressor (106); a heat energy reflux pipeline (105) is provided at an interface on one side of the high temperature rise compressor (106); the heat energy reflux pipeline (105) is connected to an interface above the shell side of the reboiler (102); and an interface below the shell side of the reboiler (102) is connected to an upper pipe opening on the side of the gas-liquid separation flash tank (108).

8. A deamination tower energy-saving device according to claim 7, characterized in that: A vacuum pump module (125) is provided on one side of the steam condensate buffer tank (123), and the vacuum pump module (125) is connected to the top of the steam condensate buffer tank (123).

9. A deamination tower energy-saving device according to claim 8, characterized in that: The two water washing towers (113) are arranged side by side, and a cooler (115) is provided on one side of the water washing tower (113). The inlet of the cooler (115) is connected to an ammonia recovery pipeline (120). The (115) is connected to an interface at the lower side of the water washing tower on one side, and an input water pipe is connected to the top of the side of the water washing tower (113). A connecting pipe (124) is connected between the two parallel water washing towers (113). One end of the connecting pipe (124) is connected to an interface at the top of the water washing tower (113) on one side, and the other end of the connecting pipe (124) is connected to an interface at the lower side of the water washing tower on the other side. The top of the water washing tower on the other side is connected to an output pipe.

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