Coking ammonia distillation waste heat recycling system
Patent Information
- Application Number
- CN202510664668.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-05-22
- Publication Date
- 2025-08-05
AI Technical Summary
During the ammonia steaming process in coking plants, how to reasonably utilize the heat carried by steam to reduce the use of frozen water and circulating water and improve energy utilization efficiency.
The first and second lithium bromide refrigerators are used to exchange heat with high-temperature ammonia vapor with circulating water and refrigerated water through parallel pipelines to form frozen water, and heat is further recovered through gas-liquid separation, concentrated ammonia water cooling and other steps to be used for desulfurization devices and other stages.
The use of frozen water and circulating water is reduced, and the energy utilization efficiency is improved. The produced frozen water can meet the needs of equipment such as primary coolers, pre-cooling towers, etc., and reduce the use of steam in conventional refrigeration stations.
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Figure CN120426682A_ABST
Abstract
Description
Technical Field
[0001] The present application relates to the field of heat energy recovery technology, and in particular to a coking ammonia evaporation waste heat recovery and utilization system. Background Art
[0002] At present, coking plants mostly use indirect ammonia distillation, using steam to heat ammonia distillation wastewater. Part of the ammonia vapor is cooled with circulating water in the ammonia fractionator at the top of the tower and then returned to the ammonia distillation tower. Part of the ammonia vapor is cooled with chilled water and then sent to the desulfurization section. The ammonia distillation process transformation often uses heat pumps to recover heat and produce steam to achieve the goal of energy saving and consumption reduction. How to rationally utilize the heat carried by this steam is currently an unresolved problem. Summary of the Invention
[0003] The purpose of this application is to provide a coking ammonia evaporation waste heat recovery and utilization system to address at least one technical problem involved in the background technology.
[0004] In order to achieve the above objectives, this application adopts the following technical solutions:
[0005] The present application provides a coking ammonia evaporation waste heat recovery and utilization system, comprising an ammonia evaporation tower, a first lithium bromide refrigerator, and a second lithium bromide refrigerator. A high-temperature ammonia vapor outlet is formed at the top of the ammonia evaporation tower. A first ammonia vapor inlet, a mixed ammonia outlet, a first circulating water inlet, a first circulating water outlet, a first chilled water inlet, and a first chilled water outlet are formed on the first lithium bromide refrigerator. A second ammonia vapor inlet, a first ammonia water outlet, a second circulating water inlet, a second circulating water outlet, a second chilled water inlet, and a second chilled water outlet are formed on the second lithium bromide refrigerator.
[0006] The high-temperature ammonia vapor outlet is connected to the first ammonia vapor inlet, the mixed ammonia outlet is connected to the second ammonia vapor inlet, the first circulating water inlet and the second circulating water inlet are connected in parallel to the first circulating water supply pipeline, the first circulating water outlet and the second circulating water outlet are connected in parallel to the first circulating water return pipeline, the first chilled water inlet and the second chilled water inlet are connected in parallel to the first chilled water return pipeline, and the first chilled water outlet and the second chilled water outlet are connected in parallel to the first chilled water supply pipeline.
[0007] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a gas-liquid separator, on which a mixed ammonia inlet, a second ammonia vapor outlet and a second ammonia aqueous solution outlet are formed, the mixed ammonia outlet is connected to the mixed ammonia inlet, the second ammonia vapor outlet is connected to the second ammonia vapor inlet, and the second ammonia aqueous solution outlet is connected to the ammonia evaporation tower.
[0008] The beneficial effect of this technical solution is that: in this way, the mixed ammonia including both ammonia water and ammonia vapor first enters the gas-liquid separator from the mixed ammonia outlet for gas-liquid separation, the separated ammonia water is sent back to the ammonia distillation tower through the second ammonia water outlet, and the separated ammonia vapor is then sent to the second lithium bromide refrigerator through the second ammonia vapor outlet and the second ammonia vapor inlet in sequence.
[0009] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a controller and a first temperature sensor that are communicatively connected to each other. The first temperature sensor is installed at the first ammonia water outlet to obtain the ammonia water temperature value at the first ammonia water outlet in real time, and discharge the ammonia water from the first ammonia water outlet to the second lithium bromide refrigeration machine when the ammonia water temperature value is not lower than 65°C.
[0010] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a concentrated ammonia water cooler, on which an ammonia water inlet, a concentrated ammonia water outlet, a third chilled water inlet and a third chilled water outlet are formed. The ammonia water inlet is connected to the first ammonia water outlet, the concentrated ammonia water outlet is connected to the concentrated ammonia water delivery pipeline, the third chilled water inlet is connected to the second chilled water supply pipeline, and the third chilled water outlet is connected to the second chilled water return pipeline.
[0011] The beneficial effect of this technical solution is that: in this way, ammonia vapor is condensed and cooled in the second lithium bromide refrigerator to release heat and then liquefied into ammonia water. The ammonia water enters the concentrated ammonia water cooler through the first ammonia water outlet and the ammonia water inlet in sequence. The chilled water enters the concentrated ammonia water cooler through the third chilled water inlet to exchange heat with the ammonia water. The formed concentrated ammonia water is sent from the concentrated ammonia water outlet to the concentrated ammonia water delivery pipeline, and then sent to the desulfurization device to replenish ammonia. The chilled water that completes the heat exchange is sent to the second chilled water return pipeline.
[0012] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a second temperature sensor communicatively connected to the controller, and the second temperature sensor is installed in the concentrated ammonia water cooler. The second temperature sensor is used to obtain the temperature value of the concentrated ammonia water in the concentrated ammonia water cooler in real time, and discharge the concentrated ammonia water from the concentrated ammonia water cooler when the temperature value of the concentrated ammonia water is not higher than 30°C.
[0013] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a reboiler, on which a first wastewater inlet, a gasification outlet, a low-pressure steam inlet and a condensate outlet are formed, and on the ammonia evaporation tower, a first wastewater outlet and a gasification reflux port are formed, the gasification reflux port is located above the first wastewater outlet, the wastewater outlet is connected to the first wastewater inlet, and the gasification reflux port is connected to the gasification outlet.
[0014] The beneficial effect of this technical solution is that: in this way, the low-pressure steam enters the reboiler through the low-pressure steam inlet, and exchanges heat with the ammonia evaporation wastewater flowing out from the wastewater outlet and entering the reboiler from the first wastewater inlet in the reboiler. After the ammonia evaporation wastewater is vaporized, it enters the ammonia evaporation tower through the vaporization outlet and the vaporization reflux port in sequence, and the ammonia evaporation wastewater is reused. The steam condensate formed after the low-pressure steam completes the heat exchange is discharged through the condensate outlet.
[0015] Optionally, a second wastewater outlet and a first residual ammonia water inlet are formed on the ammonia evaporation tower, and the first residual ammonia water inlet is located above the second wastewater outlet. The coking ammonia evaporation waste heat recovery and utilization system also includes an ammonia water heat exchanger, and a second wastewater inlet, a third wastewater outlet, a second residual ammonia water inlet and a residual ammonia water outlet are formed on the ammonia water heat exchanger. The second wastewater outlet is connected to the second wastewater inlet, the residual ammonia water outlet is connected to the first residual ammonia water inlet, and the second residual ammonia water inlet is connected to the residual ammonia water feed pipeline.
[0016] The beneficial effect of this technical solution is that: in this way, the ammonia wastewater in the ammonia still flows through the second wastewater outlet and the second wastewater inlet in sequence to enter the ammonia heat exchanger, and the remaining ammonia water enters the ammonia heat exchanger through the remaining ammonia water feeding pipeline and the second remaining ammonia water inlet. After the remaining ammonia water exchanges heat with the ammonia wastewater in the ammonia heat exchanger, the heated remaining ammonia water enters the ammonia still through the first remaining ammonia water inlet, and the ammonia wastewater that completes the heat exchange in the ammonia heat exchanger is sent out of the ammonia heat exchanger from the third wastewater outlet.
[0017] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a controller and a third temperature sensor that are communicatively connected to each other. The third temperature sensor is installed on the ammonia water heat exchanger to obtain the temperature value of the remaining ammonia water in the ammonia water heat exchanger in real time, and discharge the remaining ammonia water from the ammonia water heat exchanger when the temperature value of the remaining ammonia water is not lower than 98°C.
[0018] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes an ammonia evaporation wastewater heat exchanger, and a third wastewater inlet, a fourth wastewater outlet, a third circulating water inlet and a third circulating water outlet are formed on the ammonia evaporation wastewater heat exchanger, the third circulating water inlet is connected to the second circulating water supply pipeline, the third circulating water outlet is connected to the second circulating water return pipeline, the third wastewater inlet is connected to the third wastewater outlet, and the fourth wastewater outlet is connected to the ammonia evaporation wastewater delivery pipeline.
[0019] The beneficial effect of this technical solution is that: in this way, the ammonia vapor wastewater cooled in the ammonia vapor heat exchanger enters the ammonia vapor wastewater heat exchanger through the third wastewater outlet and the third wastewater inlet in sequence, and the circulating water enters the ammonia vapor wastewater heat exchanger through the third circulating water inlet. The circulating water exchanges heat with the ammonia vapor wastewater in the ammonia vapor wastewater heat exchanger, and after the ammonia vapor wastewater is cooled again, the ammonia vapor wastewater is sent to the downstream treatment device.
[0020] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the present application also includes a fourth temperature sensor communicatively connected to the controller, and the fourth temperature sensor is installed in the ammonia evaporation wastewater heat exchanger to obtain the temperature value of the ammonia evaporation wastewater in the ammonia evaporation wastewater heat exchanger in real time, and discharge the ammonia evaporation wastewater from the ammonia evaporation wastewater heat exchanger after the temperature value of the ammonia evaporation wastewater is no higher than 40°C.
[0021] The technical solution provided by this application can achieve at least one of the following beneficial effects:
[0022] The coking ammonia evaporation waste heat recovery and utilization system provided in the present application utilizes a first lithium bromide refrigerator and a second lithium bromide refrigerator to recover the heat carried by the high-temperature ammonia vapor generated by the ammonia evaporation tower, and utilizes this heat to form chilled water. This chilled water can supplement the chilled water demand of equipment such as the primary cooler, pre-cooling tower, ammonia condenser cooler and final cooling tower, and further utilizes the heat carried by the high-temperature ammonia vapor to generate chilled water, thereby providing a solution to the problem of how to reasonably utilize the heat carried by the high-temperature ammonia vapor.
[0023] The additional technical features and advantages of this application will be more clearly explained in the following description, or can be understood through the specific practice of this application. BRIEF DESCRIPTION OF THE DRAWINGS
[0024] To more clearly illustrate the technical solutions of the specific embodiments of this application, the following briefly introduces the drawings required for describing the specific embodiments. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be derived from these drawings without inventive effort.
[0025] Figure 1 This is a structural schematic diagram of an embodiment of the coking ammonia evaporation waste heat recovery and utilization system provided in the examples of the present application.
[0026] Reference numerals:
[0027] 01. Ammonia wastewater heat exchanger; 02. Ammonia water heat exchanger;
[0028] 03. Ammonia still; 04. Reboiler;
[0029] 05. Concentrated ammonia water cooler; 06. Second lithium bromide refrigerator;
[0030] 07. The first lithium bromide refrigerator; 08. Gas-liquid separator;
[0031] 09. Low-pressure steam inlet pipe; 10. Condensate outlet pipe;
[0032] 11. Residual ammonia water feeding pipeline; 12. Second circulating water supply pipeline;
[0033] 13. Ammonia distillation wastewater delivery pipeline; 14. Secondary circulating water return pipeline;
[0034] 15. Second chilled water supply pipeline; 16. Concentrated ammonia delivery pipeline;
[0035] 17. Second chilled water return pipeline; 18. First chilled water supply pipeline;
[0036] 19. First circulating water supply pipeline; 20. First circulating water return pipeline;
[0037] 21. The first chilled water return pipeline. DETAILED DESCRIPTION
[0038] The following will clearly and completely describe the technical solution of this application in conjunction with the accompanying drawings. Obviously, the embodiments described are only part of the embodiments of this application, not all of them. Based on the embodiments in this application, all other embodiments obtained by ordinary technicians in this field without making any creative efforts are within the scope of protection of this application.
[0039] In the description of this application, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating orientations or positional relationships, are based on the orientations or positional relationships shown in the accompanying drawings and are intended solely to facilitate the description of this application and simplify the description. They do not indicate or imply that the devices or components referred to must have a specific orientation, be constructed, or operate in a specific orientation. Therefore, they should not be construed as limitations on this application. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.
[0040] In the description of this application, it should be noted that, unless otherwise expressly specified or limited, the terms "mounted," "connected," and "connected" should be understood in a broad sense. For example, they can refer to fixed connections, detachable connections, or integral connections; mechanical connections or electrical connections; direct connections or indirect connections through an intermediate medium; and internal connections between two components. Those skilled in the art will understand the specific meanings of the above terms in this application based on the specific circumstances.
[0041] like Figure 1 As shown in the figure, based on the whole process of the coking plant, coke ovens mostly use waste heat recovery devices to produce a large amount of steam for power generation. Therefore, the coking plant does not lack steam, but lacks chilled water. Equipment such as the primary cooler, pre-cooling tower, ammonia condensing cooler and final cooling tower need to use chilled water to cool the coal gas or ammonia vapor. Therefore, how to use the heat carried by the steam to produce more chilled water has become a problem to be solved.
[0042] The present application provides a coking ammonia evaporation waste heat recovery and utilization system comprising an ammonia evaporation tower 03, a first lithium bromide refrigerator 07, and a second lithium bromide refrigerator 06. A high-temperature ammonia vapor outlet is formed at the top of the ammonia evaporation tower 03. A first ammonia vapor inlet, a mixed ammonia outlet, a first circulating water inlet, a first circulating water outlet, a first chilled water inlet, and a first chilled water outlet are formed on the first lithium bromide refrigerator 07. A second ammonia vapor inlet, a first ammonia water outlet, a second circulating water inlet, a second circulating water outlet, a second chilled water inlet, and a second chilled water outlet are formed on the second lithium bromide refrigerator 06.
[0043] The high-temperature ammonia vapor outlet is connected to the first ammonia vapor inlet, the mixed ammonia outlet is connected to the second ammonia vapor inlet, the first circulating water inlet and the second circulating water inlet are connected in parallel to the first circulating water supply pipeline 19, the first circulating water outlet and the second circulating water outlet are connected in parallel to the first circulating water return pipeline 20, the first chilled water inlet and the second chilled water inlet are connected in parallel to the first chilled water return pipeline 21, and the first chilled water outlet and the second chilled water outlet are connected in parallel to the first chilled water supply pipeline 18.
[0044] The coking ammonia evaporation waste heat recovery and utilization system provided in the present application, when in use, the high-temperature ammonia vapor sent from the high-temperature ammonia vapor outlet at the top of the ammonia evaporation tower 03 enters the first ammonia vapor inlet of the first lithium bromide refrigerator 07, and part of the heat of the high-temperature ammonia vapor is utilized in the first lithium bromide refrigerator 07 to form liquid-gas mixed ammonia, which is sent from the mixed ammonia outlet and enters the second lithium bromide refrigerator 06 from the second ammonia vapor inlet, and the heat of the liquid-gas mixed ammonia is further utilized in the second lithium bromide refrigerator 06 to form ammonia water, which is sent from the first ammonia water outlet to complete the release of the heat of the high-temperature ammonia vapor sent from the top of the ammonia evaporation tower 03 The circulating water enters the first lithium bromide refrigerator 07 from the first circulating water inlet and the second lithium bromide refrigerator 06 from the second circulating water inlet through the first circulating water supply pipeline 19, and accordingly, enters the first circulating water return pipeline 20 from the first circulating water outlet and the second circulating water outlet respectively. The refluxed chilled water enters the first lithium bromide refrigerator 07 from the first chilled water inlet and the second lithium bromide refrigerator 06 from the second chilled water inlet through the first chilled water return pipeline 21, and accordingly, enters the first chilled water supply pipeline 18 from the first chilled water outlet and the second chilled water outlet respectively to complete the preparation of chilled water.
[0045] The coking ammonia evaporation waste heat recovery and utilization system provided by the present application utilizes a first lithium bromide refrigerator 07 and a second lithium bromide refrigerator 06 to recover the heat carried by the high-temperature ammonia vapor generated by the ammonia evaporation tower 03, and utilizes this heat to generate chilled water. This chilled water can supplement the chilled water demand of equipment such as the primary cooler, pre-cooling tower, ammonia condenser cooler, and final cooling tower. Furthermore, by utilizing the heat carried by the high-temperature ammonia vapor to generate chilled water, a method is provided to solve the problem of how to reasonably utilize the heat carried by the high-temperature ammonia vapor. In one embodiment of the present application, a lithium bromide refrigerator is used to directly utilize the waste heat of the ammonia vapor at the top of the ammonia evaporation tower 03 to produce a large amount of chilled water, thereby reducing the use of chilled water and circulating water in the ammonia evaporation section. The use of circulating water is reduced by 30%. In addition to being used in this section, the produced chilled water can also be supplied to other sections, supplying approximately 6 tons of chilled water per 1 ton of residual ammonia water, thereby reducing the steam usage of conventional refrigeration stations and even replacing the steam refrigerators of refrigeration stations.
[0046] Optionally, the coking ammonia evaporation waste heat recovery system provided in the embodiments of the present application further includes a gas-liquid separator 08, which is provided with a mixed ammonia inlet, a second ammonia vapor outlet, and a second ammonia aqueous solution outlet. The mixed ammonia outlet is connected to the mixed ammonia inlet, the second ammonia vapor outlet is connected to the second ammonia vapor inlet, and the second ammonia aqueous solution outlet is connected to the ammonia evaporation column 03. In this way, the mixed ammonia, which includes both ammonia aqueous solution and ammonia vapor, first enters the gas-liquid separator 08 from the mixed ammonia outlet for gas-liquid separation. The separated ammonia aqueous solution is returned to the ammonia evaporation column 03 through the second ammonia aqueous solution outlet. The separated ammonia vapor is then sequentially fed into the second lithium bromide refrigerator 06 through the second ammonia vapor outlet and the second ammonia vapor inlet.
[0047] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application also includes a controller and a first temperature sensor that are communicatively connected to each other. The first temperature sensor is installed at the first ammonia water outlet to obtain the ammonia water temperature value at the first ammonia water outlet in real time, and discharge the ammonia water from the first ammonia water outlet to the second lithium bromide refrigeration machine 06 when the ammonia water temperature value is not lower than 65°C.
[0048] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application further includes a concentrated ammonia water cooler 05, on which an ammonia water inlet, a concentrated ammonia water outlet, a third chilled water inlet, and a third chilled water outlet are formed. The ammonia water inlet is connected to the first ammonia water outlet, the concentrated ammonia water outlet is connected to the concentrated ammonia water delivery pipeline 16, the third chilled water inlet is connected to the second chilled water supply pipeline 15, and the third chilled water outlet is connected to the second chilled water return pipeline 17. In this way, after the ammonia vapor is condensed and cooled in the second lithium bromide refrigerator 06 and the heat is released, it is liquefied into ammonia water. The ammonia water enters the concentrated ammonia water cooler 05 through the first ammonia water outlet and the ammonia water inlet in sequence. The chilled water enters the concentrated ammonia water cooler 05 through the third chilled water inlet to exchange heat with the ammonia water. The concentrated ammonia water formed is sent from the concentrated ammonia water outlet to the concentrated ammonia water delivery pipeline 16, and then sent to the desulfurization device to replenish ammonia. The chilled water that has completed the heat exchange is sent to the second chilled water return pipeline 17. It can be understood that the discharge of ammonia water can be achieved through a control valve that is in communication with the controller.
[0049] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application also includes a second temperature sensor communicatively connected to the controller, and the second temperature sensor is installed in the concentrated ammonia water cooler 05. The second temperature sensor is used to obtain the temperature value of the concentrated ammonia water in the concentrated ammonia water cooler 05 in real time, and discharge the concentrated ammonia water from the concentrated ammonia water cooler 05 when the temperature value of the concentrated ammonia water is not higher than 30°C.
[0050] Optionally, the coking ammonia evaporation waste heat recovery system provided in the embodiment of the present application further includes a reboiler 04, which is formed with a first wastewater inlet, a vaporization outlet, a low-pressure steam inlet, and a condensate outlet. A first wastewater outlet and a vaporization reflux port are formed on the ammonia evaporation tower 03. The vaporization reflux port is located above the first wastewater outlet, the wastewater outlet is connected to the first wastewater inlet, and the vaporization reflux port is connected to the vaporization outlet. The low-pressure steam inlet is connected to the low-pressure steam inlet pipe 09, and the condensate outlet is connected to the condensate outlet pipe 10. In this way, low-pressure steam enters the reboiler 04 through the low-pressure steam inlet, and in the reboiler 04, heat is exchanged with the ammonia evaporation wastewater flowing out of the wastewater outlet and entering the reboiler 04 from the first wastewater inlet. After the ammonia evaporation wastewater is vaporized, it enters the ammonia evaporation tower 03 through the vaporization outlet and the vaporization reflux port in turn. The ammonia evaporation wastewater is reused, and the steam condensate formed after the low-pressure steam completes the heat exchange is discharged through the condensate outlet.
[0051] Optionally, a second wastewater outlet and a first residual ammonia water inlet are formed on the ammonia evaporation tower 03, and the first residual ammonia water inlet is located above the second wastewater outlet. The coking ammonia evaporation waste heat recovery and utilization system also includes an ammonia water heat exchanger 02, and a second wastewater inlet, a third wastewater outlet, a second residual ammonia water inlet and a residual ammonia water outlet are formed on the ammonia water heat exchanger 02. The second wastewater outlet is connected to the second wastewater inlet, the residual ammonia water outlet is connected to the first residual ammonia water inlet, and the second residual ammonia water inlet is connected to the residual ammonia water feed pipeline 11. In this way, the ammonia evaporation wastewater in the ammonia evaporation tower 03 flows through the second wastewater outlet and the second wastewater inlet in sequence and enters the ammonia water heat exchanger 02. The remaining ammonia water enters the ammonia water heat exchanger 02 through the remaining ammonia water supply pipeline 11 and the second remaining ammonia water inlet. After the remaining ammonia water exchanges heat with the ammonia evaporation wastewater in the ammonia water heat exchanger 02, the heated remaining ammonia water enters the ammonia evaporation tower 03 through the first remaining ammonia water inlet. The ammonia evaporation wastewater that has completed the heat exchange in the ammonia water heat exchanger 02 is sent out of the ammonia water heat exchanger 02 through the third wastewater outlet.
[0052] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application also includes a controller and a third temperature sensor that are communicatively connected to each other. The third temperature sensor is installed in the ammonia water heat exchanger 02 to obtain the temperature value of the remaining ammonia water in the ammonia water heat exchanger 02 in real time, and discharge the remaining ammonia water from the ammonia water heat exchanger 02 when the temperature value of the remaining ammonia water is not lower than 98°C.
[0053] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application further includes an ammonia evaporation wastewater heat exchanger 01, on which a third wastewater inlet, a fourth wastewater outlet, a third circulating water inlet, and a third circulating water outlet are formed. The third circulating water inlet is connected to the second circulating water supply pipeline 12, the third circulating water outlet is connected to the second circulating water return pipeline 14, the third wastewater inlet is connected to the third wastewater outlet, and the fourth wastewater outlet is connected to the ammonia evaporation wastewater delivery pipeline 13. In this way, the ammonia evaporation wastewater cooled in the ammonia evaporation heat exchanger 02 enters the ammonia evaporation wastewater heat exchanger 01 through the third wastewater outlet and the third wastewater inlet in sequence, and the circulating water enters the ammonia evaporation wastewater heat exchanger 01 through the third circulating water inlet. In the ammonia evaporation wastewater heat exchanger 01, the circulating water exchanges heat with the ammonia evaporation wastewater, and after the ammonia evaporation wastewater is cooled again, it is sent to the downstream treatment device.
[0054] Optionally, the coking ammonia evaporation waste heat recovery and utilization system provided in the embodiment of the present application further includes a fourth temperature sensor communicatively connected to the controller, and the fourth temperature sensor is installed in the ammonia evaporation wastewater heat exchanger 01 to obtain the temperature value of the ammonia evaporation wastewater in the ammonia evaporation wastewater heat exchanger 01 in real time, and discharge the ammonia evaporation wastewater from the ammonia evaporation wastewater heat exchanger 01 after the temperature value of the ammonia evaporation wastewater is no higher than 40°C.
[0055] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit them. Although the present application has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some or all of the technical features therein. These modifications or replacements do not deviate the essence of the corresponding technical solutions from the scope of the technical solutions of the embodiments of the present application.
Claims
1. Coking ammonia evaporation waste heat recovery and utilization system, characterized by: The invention comprises an ammonia still tower, a first lithium bromide refrigerator and a second lithium bromide refrigerator. The top of the ammonia still tower is formed with a high-temperature ammonia vapor outlet. The first lithium bromide refrigerator is formed with a first ammonia vapor inlet, a mixed ammonia outlet, a first circulating water inlet, a first circulating water outlet, a first chilled water inlet and a first chilled water outlet. The second lithium bromide refrigerator is formed with a second ammonia vapor inlet, a first ammonia water outlet, a second circulating water inlet, a second circulating water outlet, a second chilled water inlet and a second chilled water outlet. The high-temperature ammonia vapor outlet is connected to the first ammonia vapor inlet, the mixed ammonia outlet is connected to the second ammonia vapor inlet, the first circulating water inlet and the second circulating water inlet are connected in parallel to the first circulating water supply pipeline, the first circulating water outlet and the second circulating water outlet are connected in parallel to the first circulating water return pipeline, the first chilled water inlet and the second chilled water inlet are connected in parallel to the first chilled water return pipeline, and the first chilled water outlet and the second chilled water outlet are connected in parallel to the first chilled water supply pipeline.
2. The coking ammonia evaporation waste heat recovery and utilization system according to claim 1, characterized in that: It also includes a gas-liquid separator, on which a mixed ammonia inlet, a second ammonia vapor outlet and a second ammonia aqueous solution outlet are formed, the mixed ammonia outlet is connected to the mixed ammonia inlet, the second ammonia vapor outlet is connected to the second ammonia vapor inlet, and the second ammonia aqueous solution outlet is connected to the ammonia evaporation tower.
3. The coking ammonia evaporation waste heat recovery and utilization system according to claim 2, characterized in that: It also includes a controller and a first temperature sensor that are communicatively connected to each other. The first temperature sensor is installed at the first ammonia water outlet to obtain the ammonia water temperature value at the first ammonia water outlet in real time, and discharges the ammonia water from the first ammonia water outlet to the second lithium bromide refrigerator when the ammonia water temperature value is not lower than 65°C.
4. The coking ammonia evaporation waste heat recovery and utilization system according to claim 3 is characterized in that: It also includes a concentrated ammonia water cooler, on which an ammonia water inlet, a concentrated ammonia water outlet, a third chilled water inlet and a third chilled water outlet are formed. The ammonia water inlet is connected to the first ammonia water outlet, the concentrated ammonia water outlet is connected to the concentrated ammonia water delivery pipeline, the third chilled water inlet is connected to the second chilled water supply pipeline, and the third chilled water outlet is connected to the second chilled water return pipeline.
5. The coking ammonia evaporation waste heat recovery and utilization system according to claim 4, characterized in that: It also includes a second temperature sensor that is communicatively connected to the controller, and the second temperature sensor is installed in the concentrated ammonia water cooler. The second temperature sensor is used to obtain the temperature value of the concentrated ammonia water in the concentrated ammonia water cooler in real time, and discharge the concentrated ammonia water from the concentrated ammonia water cooler when the temperature value of the concentrated ammonia water is not higher than 30°C.
6. The coking ammonia evaporation waste heat recovery and utilization system according to claim 1, characterized in that: It also includes a reboiler, on which a first wastewater inlet, a vaporization outlet, a low-pressure steam inlet and a condensate outlet are formed, and on the ammonia still, a first wastewater outlet and a vaporization reflux port are formed, the vaporization reflux port is located above the first wastewater outlet, the wastewater outlet is connected to the first wastewater inlet, and the vaporization reflux port is connected to the vaporization outlet.
7. The coking ammonia evaporation waste heat recovery and utilization system according to any one of claims 1 to 6, characterized in that: A second wastewater outlet and a first residual ammonia water inlet are formed on the ammonia evaporation tower, and the first residual ammonia water inlet is located above the second wastewater outlet. The coking ammonia evaporation waste heat recovery and utilization system also includes an ammonia water heat exchanger, and a second wastewater inlet, a third wastewater outlet, a second residual ammonia water inlet and a residual ammonia water outlet are formed on the ammonia water heat exchanger. The second wastewater outlet is connected to the second wastewater inlet, the residual ammonia water outlet is connected to the first residual ammonia water inlet, and the second residual ammonia water inlet is connected to the residual ammonia water feed pipeline.
8. The coking ammonia evaporation waste heat recovery and utilization system according to claim 7, characterized in that: It also includes a controller and a third temperature sensor that are communicatively connected to each other. The third temperature sensor is installed on the ammonia water heat exchanger to obtain the temperature value of the remaining ammonia water in the ammonia water heat exchanger in real time, and discharge the remaining ammonia water from the ammonia water heat exchanger when the temperature value of the remaining ammonia water is not lower than 98°C.
9. The coking ammonia evaporation waste heat recovery and utilization system according to claim 8, characterized in that: It also includes an ammonia vapor wastewater heat exchanger, on which a third wastewater inlet, a fourth wastewater outlet, a third circulating water inlet and a third circulating water outlet are formed, the third circulating water inlet is connected to the second circulating water supply pipeline, the third circulating water outlet is connected to the second circulating water return pipeline, the third wastewater inlet is connected to the third wastewater outlet, and the fourth wastewater outlet is connected to the ammonia vapor wastewater delivery pipeline.
10. The coking ammonia evaporation waste heat recovery and utilization system according to claim 9, characterized in that: It also includes a fourth temperature sensor that is communicatively connected to the controller. The fourth temperature sensor is installed in the ammonia evaporation wastewater heat exchanger to obtain the temperature value of the ammonia evaporation wastewater in the ammonia evaporation wastewater heat exchanger in real time, and discharges the ammonia evaporation wastewater from the ammonia evaporation wastewater heat exchanger after the temperature value of the ammonia evaporation wastewater is no higher than 40°C.