Coking wastewater filter pressing sludge secondary dehydration system

Abstract

The utility model provides a coking wastewater filter pressing sludge secondary dehydration system, which belongs to the field of sludge reduction, is arranged at the rear end of a traditional filter press, and comprises an air blower, a heat exchanger and a drying room, wherein the drying room is provided with a sludge inlet and a sludge outlet; the blower communicates with a shell pass inlet of the heat exchanger; a shell pass outlet of the heat exchanger is communicated with the drying room through an air inlet pipeline; the heat exchanger is provided with a tube pass inlet for coking wastewater serving as a heat source to enter. According to the sludge drying device, the sludge is dried by using the dry hot air subjected to heat exchange through the coking wastewater, and the wet hot air obtained after sludge drying is treated by adopting the VOCs waste gas treatment device. According to the whole system, energy of coking wastewater discharged from the ammonia still is recycled, sludge reduction is indirectly achieved, and the purposes of saving the sludge treatment cost and recycling the coking wastewater energy are achieved.

Description

Technical Field

[0001] The utility model belongs to the field of sludge reduction, and relates to a coking wastewater filter press sludge secondary dehydration system, in particular to a coking wastewater filter press sludge secondary dehydration system for sludge reduction, wastewater resource utilization and energy recovery. Background Art

[0002] In the process of coking wastewater treatment, a large amount of residual sludge and coagulated sludge will be generated. These sludges have a high water content and are difficult to dispose of directly, so they need to be dehydrated. The traditional sludge dehydration method usually uses a filter press for initial dehydration, but the water content of the sludge after dehydration is still high and requires further treatment. At the same time, a large amount of ammonia evaporation wastewater will be generated in the process of coking wastewater treatment. These wastewaters are usually discharged after being treated in an ammonia evaporation tower, and the waste heat resources of the ammonia evaporation wastewater generated in the ammonia evaporation tower have not been effectively utilized. Therefore, how to achieve effective dehydration of sludge and recovery of waste heat from ammonia evaporation wastewater are two major problems that need to be solved in the field of coking wastewater treatment. Utility Model Content

[0003] In view of the above problems, the utility model provides a coking wastewater filter press sludge secondary dehydration system, which is a system based on the secondary dehydration of the residual sludge and coagulation sludge of the coking wastewater by utilizing the waste heat of the ammonia evaporation wastewater generated by the ammonia evaporation tower. The system uses the waste heat of the ammonia evaporation wastewater as a heat source, and through indirect heat transfer cycle treatment, realizes the effective dehydration of the sludge and the recycling of energy, has the advantages of energy saving, emission reduction, resource utilization, etc., and provides a new solution for the sludge treatment and recycling of ammonia evaporation wastewater preheating in the field of coking wastewater treatment.

[0004] In order to achieve the above purpose, the technical solution adopted by the utility model is:

[0005] A coking wastewater filter press sludge secondary dehydration system, the coking wastewater filter press sludge secondary dehydration system comprises a blower, a heat exchanger and a drying room;

[0006] Among them, the drying room is equipped with a mud inlet and a mud outlet;

[0007] The blower is connected to the shell side inlet of the heat exchanger; the shell side outlet of the heat exchanger is connected to the drying room through the air inlet duct;

[0008] The heat exchanger is provided with a tube-side inlet for coking wastewater serving as a heat source to enter.

[0009] Furthermore, the drying room is a hollow rectangular parallelepiped structure, with the height direction of the drying room as the up-down relationship, and an upper conveyor belt and a lower conveyor belt are arranged in parallel up and down inside the drying room.

[0010] Furthermore, with the length direction of the drying room as the left-right relationship, a mud inlet is provided at the upper end of the left outer wall of the drying room, and a mud outlet is provided on the left side of the bottom of the drying room.

[0011] Furthermore, scrapers are respectively provided at the end of the upper conveyor belt and the end of the lower conveyor belt.

[0012] Furthermore, the coking wastewater filter press sludge secondary dehydration system also includes a first heat exchanger for first cooling of the coking wastewater;

[0013] The tube side inlet of the first heat exchanger is connected to the ammonia still that produces coking wastewater;

[0014] The tube side outlet of the first heat exchanger is communicated with the tube side inlet of the heat exchanger.

[0015] Furthermore, the coking wastewater filter press sludge secondary dehydration system also includes a second heat exchanger for cooling the coking wastewater again; the tube side outlet of the heat exchanger is connected to the tube side inlet of the second heat exchanger.

[0016] Furthermore, the air inlet duct includes an air inlet main pipe and multiple air inlet branch pipes, one end of the air inlet main pipe is connected to the shell outlet of the heat exchanger, and the other end of the air inlet main pipe is connected to multiple air inlet branch pipes; the multiple air inlet branch pipes are evenly arranged at the top of the drying room, and the air outlet direction of each air inlet branch pipe is downward.

[0017] Furthermore, a valve for controlling the air volume of the hot dry air is provided on the air inlet branch pipe.

[0018] Furthermore, the right side of the bottom of the drying room is connected to an air outlet duct.

[0019] Furthermore, the air outlet duct is connected to the induced draft fan, and the induced draft fan is connected to the VOCs gas treatment device.

[0020] The beneficial effects of the coking wastewater filter press sludge secondary dehydration system of the utility model are:

[0021] The utility model aims at recycling the energy of ammonia evaporation wastewater discharged from the ammonia evaporation tower of coking wastewater, and indirectly realizes sludge reduction, so as to achieve the purpose of saving sludge treatment cost and recycling the energy of ammonia evaporation wastewater;

[0022] The utility model utilizes the waste heat of ammonia evaporation wastewater to perform secondary dehydration of sludge, effectively saving the energy consumed in sludge treatment, reducing treatment costs, realizing resource utilization of ammonia evaporation wastewater, and having good economic and social benefits;

[0023] The coking wastewater filter press sludge secondary dehydration system designed by the utility model, especially the drying room, has a simple structure and convenient operation, can realize uniform heating and efficient dehydration of the sludge, and improves the dehydration efficiency and quality;

[0024] The utility model further improves the drying efficiency and energy utilization efficiency by arranging the air inlet main pipe and the air inlet branch pipe;

[0025] The utility model connects the hot and humid air to the VOCs gas treatment device for treatment, thus avoiding environmental pollution and meeting environmental protection requirements;

[0026] The coking wastewater filter press sludge secondary dehydration system provided by the utility model is helpful to promote the green development and sustainable development of the coking industry, and make positive contributions to environmental protection and ecological civilization construction;

[0027] To sum up, the coking wastewater filter press sludge secondary dehydration system provided by the utility model realizes sludge reduction and resource utilization of ammonia evaporated wastewater by rationally utilizing the waste heat of ammonia evaporated wastewater and the latent heat of evaporation of water in the sludge, which not only reduces the sludge treatment cost, but also improves the energy utilization efficiency. It has significant advantages and beneficial effects, provides a new solution for coking wastewater treatment and sludge reduction, and has broad application prospects and promotion value. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 A schematic diagram of the connection relationship of a coking wastewater filter press sludge secondary dehydration system according to an embodiment of the utility model;

[0029] Figure 2 This is a structural schematic diagram of a coking wastewater filter press sludge secondary dehydration system according to an embodiment of the utility model;

[0030] Figure 3 It is a flow chart of the use process of a coking wastewater filter press sludge secondary dehydration system according to an embodiment of the utility model;

[0031] In the figure: 1. Blower; 2. Shell-and-tube heat exchanger; 3. Drying room; 31. Mud inlet; 32. Mud outlet; 33. Upper conveyor belt; 34. Lower conveyor belt; 35. Scraper; 4. Air inlet duct; 41. Air inlet main pipe; 42. Air inlet branch pipe; 5. First heat exchanger; 6. Second heat exchanger; 7. Air outlet duct; 8. Draft fan; 9. VOCs gas treatment device. DETAILED DESCRIPTION

[0032] The technical solutions in the embodiments of the utility model are described clearly and completely below. In the following description, many specific details are set forth to facilitate a full understanding of the utility model, but the utility model can also be implemented in other ways different from those described herein, and those skilled in the art can make similar generalizations without violating the connotation of the utility model, so the utility model is not limited by the specific embodiments disclosed below.

[0033] Embodiment A coking wastewater filter press sludge secondary dehydration system

[0034] See also Figures 1 to 3 The utility model provides a coking wastewater filter press sludge secondary dehydration system, which is a system based on the secondary dehydration of coking wastewater residual sludge and coagulation sludge (all of which are preliminarily dehydrated by a screw filter press, collectively referred to as filter press sludge) using the waste heat of ammonia evaporation wastewater discharged from an ammonia evaporation tower (coking wastewater in this embodiment is ammonia evaporation wastewater, and ammonia evaporation wastewater is used to represent coking wastewater in the following).

[0035] The coking wastewater filter press sludge secondary dehydration system is arranged at the rear end of the conventional filter press (i.e., the screw filter press), and includes a blower 1, a heat exchanger (a shell-and-tube heat exchanger 2 is used in this embodiment) and a drying room 3;

[0036] The drying room 3 is provided with a mud inlet 31 and a mud outlet 32;

[0037] The blower 1 is connected to the shell side inlet of the shell-and-tube heat exchanger 2, and the dry cold air enters the shell-and-tube heat exchanger 2 through the shell side inlet via the blower 1; the shell side outlet of the shell-and-tube heat exchanger 2 is connected to the drying room 3 through the air inlet duct 4;

[0038] The shell-and-tube heat exchanger 2 is provided with a tube-side inlet for the ammonia evaporation wastewater as a heat source to enter; the ammonia evaporation wastewater discharged from the ammonia evaporation tower enters the shell-and-tube heat exchanger 2 through the tube-side inlet of the shell-and-tube heat exchanger 2, and exchanges heat with the dry cold air in the tube bundle of the shell-and-tube heat exchanger 2 to heat the dry cold air into dry hot air, while reducing the temperature of the ammonia evaporation wastewater.

[0039] The coking wastewater filter press sludge secondary dehydration system also includes a first heat exchanger 5 for cooling the ammonia evaporation wastewater for the first time and a second heat exchanger 6 for cooling the ammonia evaporation wastewater again. In this embodiment, the second heat exchanger 6 is a circulating cooling water heat exchanger;

[0040] The tube side inlet of the first heat exchanger 5 is connected to the ammonia evaporation tower, so as to cool the ammonia evaporation wastewater discharged from the ammonia evaporation tower for the first time;

[0041] The tube-side outlet of the first heat exchanger 5 is communicated with the tube-side inlet of the shell-and-tube heat exchanger 2 ; at the same time, the tube-side outlet of the shell-and-tube heat exchanger 2 is communicated with the tube-side inlet of the second heat exchanger 6 .

[0042] Further, such as Figure 2As shown, the drying room 3 is a hollow rectangular structure, with the length direction of the drying room 3 as the left-right relationship and the height direction of the drying room 3 as the up-down relationship. A mud inlet 31 is provided at the upper end of the left outer wall of the drying room 3, and a mud outlet 32 ​​is provided on the left side of the bottom of the drying room 3; an upper conveyor belt 33 and a lower conveyor belt 34 are arranged in parallel in the drying room 3, the upper conveyor belt 33 is almost in contact with the left inner wall of the drying room 3, and has a certain distance from the right inner wall of the drying room 3, the lower conveyor belt 34 is almost in contact with the right inner wall of the drying room 3, and has a certain distance from the right inner wall of the drying room 3, and the upper conveyor belt 33 and the lower conveyor belt 34 are arranged in parallel in the up-down direction.

[0043] The ends of the upper conveyor belt 33 and the lower conveyor belt 34 are also provided with scrapers 35, that is, one end of the upper conveyor belt 33 away from the inner wall of the drying room 3 (the right end of the upper conveyor belt 33) is provided with a scraper 35, and one end of the lower conveyor belt 34 away from the inner wall of the drying room 3 (the left end of the lower conveyor belt 34) is also provided with a scraper 35. The upper conveyor belt 33 and the lower conveyor belt 34 are collectively referred to as conveyor belts, and the upper conveyor belt 33 and the scraper 35 and the lower conveyor belt 34 and the scraper 35 can be connected by any existing method that can enable the scraper 35 to scrape off the sludge on the conveyor belt.

[0044] For example, the conveyor belt is made of waterproof material, and the conveyor belt is wound on the rotating sleeves at both ends. As the rotating sleeves rotate, the conveyor belt moves, thereby moving the sludge on the conveyor belt to the end. The conveyor belt also includes fixed shafts at both ends, and the rotating sleeves are coaxially sleeved on the fixed shafts. The fixed shafts at both ends are respectively fixed on the inner walls on both sides of the drying room 3; wherein, the center positions of the two fixed shafts of the upper conveyor belt 33 are close to the left inner wall of the drying room 3, the upper conveyor belt 33 is almost in contact with the left inner wall of the drying room 3, and has a certain distance from the right inner wall of the drying room 3, the left side of the upper conveyor belt 33 is the starting end, and the right side is the end; the center positions of the two fixed shafts of the lower conveyor belt 34 are close to the right inner wall of the drying room 3, the lower conveyor belt 34 is almost in contact with the right inner wall of the drying room 3, and has a certain distance from the left inner wall of the drying room 3, the right side of the lower conveyor belt 34 is the starting end, and the left side is the end;

[0045] The fixed shaft at the end of the upper conveyor belt 33 and the fixed shaft at the end of the lower conveyor belt 34 are respectively fixedly connected to the corresponding scrapers 35, and one end of the scraper 35 (i.e., the knife part) is in contact with the surface of the conveyor belt; wherein, as the upper conveyor belt 33 moves, the scraper 35 on the upper conveyor belt 33 scrapes the sludge on the upper conveyor belt 33 and drops it onto the lower conveyor belt 34, and as the lower conveyor belt 34 moves, the scraper 35 on the lower conveyor belt 34 scrapes the sludge on the lower conveyor belt 34 and drops it into the mud outlet 32.

[0046] During use, the sludge from the filter press that has been initially dehydrated by the screw filter press (i.e., the conventional filter press) is put into the drying room 3 from the sludge inlet 31, falls to the starting end of the upper conveyor belt 33, and moves to the end of the upper conveyor belt 33 as the upper conveyor belt 33 rotates. During this period, it is blown and dried by hot dry air. After moving to the end of the upper conveyor belt 33, the sludge is scraped off by the scraper 35. At this time, the sludge falls to the starting end of the lower conveyor belt 34, and then moves to the end of the lower conveyor belt 34 as the lower conveyor belt 34 rotates. During this period, it is still blown and dried by hot dry air. After moving to the end of the lower conveyor belt 34, the sludge is scraped off by the scraper 35. At this time, the sludge falls to the sludge outlet 32 ​​for discharge for subsequent treatment, such as incineration, landfill, or resource utilization.

[0047] The air inlet duct 4 includes an air inlet main pipe 41 and a plurality of air inlet branches 42. One end of the air inlet main pipe 41 is connected to the shell outlet of the shell-and-tube heat exchanger 2, and the other end of the air inlet main pipe 41 enters the drying room 3 and connects to the plurality of air inlet branches 42. The plurality of air inlet branches 42 are evenly arranged at the top of the drying room 3, and the air outlet direction of each air inlet branch pipe 42 is downward (i.e., the air outlet direction of the air inlet branch pipe 42 is toward the upper conveyor belt 33 and the lower conveyor belt 34). The hot dry air flowing out of the shell outlet of the shell-and-tube heat exchanger 2 passes through the air inlet main pipe 41 and the air inlet branch pipe 42 in sequence, and is ejected from the air outlet of the air inlet branch pipe 42 to blow and dry the sludge on the upper conveyor belt 33 and the sludge on the lower conveyor belt 34.

[0048] Furthermore, a valve (not shown in the figure) is provided on the air inlet branch pipe 42 to control the air volume of the dry hot air.

[0049] The right side of the bottom of the drying room 3 is also connected to an air outlet duct 7, which is connected to an induced draft fan 8, and the induced draft fan 8 is connected to a VOCs gas treatment device 9; the hot and humid air generated in the drying room 3 passes through the air outlet duct 7 and is discharged into the VOCs gas treatment device 9 through the induced draft fan 8 for treatment to avoid pollution to the environment.

[0050] The specific use steps of a coking wastewater filter press sludge secondary dehydration system are as follows:

[0051] S1. Introduction of ammonia wastewater

[0052] In the coking industry, the remaining ammonia water is combined with other wastewater to enter the ammonia evaporation tower, and steam is introduced into the ammonia evaporation tower to blow off the free ammonia in the wastewater. The wastewater after the stripping is called ammonia evaporation wastewater. After the high-temperature stripping ammonia evaporation wastewater undergoes the first heat exchange with the wastewater entering the ammonia evaporation tower in the first heat exchanger 5, its temperature can be reduced to 60-80°C.

[0053] S2. Gas-liquid heat exchange

[0054] Part of the evaporated ammonia wastewater after the first heat exchange is used as a heat source and enters the shell-and-tube heat exchanger 2. Dry cold air is used as a heat exchange medium and is synchronously blown into the shell-and-tube heat exchanger 2 by the blower 1 for heat exchange. The dry cold air is heated in the shell-and-tube heat exchanger 2, and the evaporated ammonia wastewater is cooled. After heat exchange through the shell-and-tube heat exchanger 2, the temperature of the cooled evaporated ammonia wastewater is reduced to 45-50°C, and the dry cold air is heated to dry hot air with a temperature of 43-48°C.

[0055] The cooled ammonia evaporated wastewater and the remaining ammonia evaporated wastewater after the first heat exchange enter the second heat exchanger 6 for a second heat exchange to reduce the temperature to below 40°C, thereby meeting the requirements of biochemical treatment; wherein the second heat exchanger 6 generally adopts a circulating cooling water heat exchanger, with circulating cooling water as the cold source.

[0056] In the traditional process, the measures adopted to reduce the ammonia wastewater to the acceptable range of biochemical treatment are all circulating cooling water heat exchange. By using the coking wastewater filter press sludge secondary dehydration system of the utility model, by drawing out part of the ammonia wastewater for cooling, the circulating cooling water consumption and evaporation loss can be reduced to a certain extent. According to calculations, when the flow rate is 10m 3 When the ammonia wastewater of / h is cooled by the coking wastewater filter press sludge secondary dehydration system of the utility model, the temperature of the ammonia wastewater is reduced from 70°C to 40°C, which can reduce the heat flow received by the circulating cooling water by about 1300kW.

[0057] S3, further dehydration of sludge

[0058] After the sludge is initially dehydrated by the screw filter press, the moisture content is about 85%. The obtained filter press sludge is introduced into the drying room 3 through the mud inlet 31. After entering the drying room 3, it falls to the starting end of the upper conveyor belt 33, and moves to the end of the upper conveyor belt 33 as the upper conveyor belt 33 rotates. After moving to the end of the upper conveyor belt 33, the sludge is scraped off by the scraper 35. At this time, the sludge falls to the starting end of the lower conveyor belt 34, and then moves to the end of the lower conveyor belt 34 as the lower conveyor belt 34 rotates. After moving to the end of the lower conveyor belt 34, the sludge is scraped off by the scraper 35. At this time, the sludge falls to the mud outlet 32 ​​for subsequent treatment, such as incineration, landfill or resource utilization. When the sludge is moved to the end of the upper conveyor belt 33 or the end of the lower conveyor belt 34, the sludge is scraped off by the scraper 35, which can prevent the partially dried sludge from adhering to the upper conveyor belt 33 or the lower conveyor belt 34.

[0059] At the same time, the valve on the air inlet branch pipe 42 is adjusted to control the air volume of the dry hot air. The dry hot air flowing out of the shell outlet of the shell-and-tube heat exchanger 2 passes through the air inlet main pipe 41 and the air inlet branch pipe 42 in sequence, and is ejected through the air distribution port of the air inlet branch pipe 42. The dry hot air is ejected into the drying room 3 to blow and dry the sludge on the upper conveyor belt 33 and the sludge on the lower conveyor belt 34.

[0060] During the treatment process, the sludge moves with the rotation of the upper conveyor belt 33 and the lower conveyor belt 34, and is scraped off by the scraper 35, which can turn and push the sludge so that it is evenly heated.

[0061] The dry hot air enters through the air inlet branch pipe 42 above the drying room 3 and is discharged from the air outlet duct 7 below. After heat exchange with the sludge, the moisture in the sludge is further evaporated, and the temperature of the air itself is reduced to form humid hot air.

[0062] S4. Hot and humid air treatment

[0063] The hot and humid air generated in the drying room 3 passes through the air outlet duct 7 and is discharged into the VOCs gas treatment device 9 through the induced draft fan 8 for treatment to avoid pollution to the environment.

[0064] S5. Sludge collection and treatment

[0065] After drying in the drying room 3, the moisture content of the sludge is greatly reduced. After the filter press sludge with an initial moisture content of 85% is treated by the coking wastewater filter press sludge secondary decolorization system, the moisture content of the obtained dried sludge is reduced to below 50%. After being discharged from the sludge outlet 32, subsequent treatment such as incineration, landfill or resource utilization can be continued. According to actual needs and actual conditions, select a suitable treatment method for the final disposal of the sludge.

[0066] After being treated by the coking wastewater filter press sludge secondary dehydration system, the water content of the sludge is greatly reduced, achieving the purpose of secondary dehydration, thereby reducing the sludge treatment cost; at the same time, after the ammonia wastewater is heat exchanged in the shell and tube heat exchanger 2, the temperature is also reduced, which can save the amount of circulating cooling water and realize the resource utilization of ammonia wastewater, with good economic and social benefits.

[0067] During the entire treatment process, various parameters need to be monitored and recorded in real time, such as sludge moisture content, air temperature, air humidity, exhaust gas emission concentration, etc. In actual application, the coking wastewater filter press sludge secondary dehydration system can also be optimized and improved according to specific conditions to meet the needs and actual conditions of different enterprises.

[0068] The following is a specific application example of a coking wastewater filter press sludge secondary dehydration system of the utility model:

[0069] A coking wastewater treatment plant in Hebei Province has an average hourly flow rate of 40m3 of ammonia wastewater. 3 / h (annual average), a coking wastewater filter press sludge secondary dehydration system of the utility model is used to treat part of the ammonia evaporation wastewater, and 10m 3 / h of ammonia evaporated wastewater is introduced into the shell-and-tube heat exchanger 2. The temperature of the ammonia evaporated wastewater after the first heat exchange of the coking plant is 75°C (that is, the temperature of the ammonia evaporated wastewater entering the shell-and-tube heat exchanger 2 is 75°C).

[0070] 1. Basic parameter settings are as follows:

[0071] Table 1 Basic parameters of cold and hot sources

[0072]

[0073]

[0074] Table 2 Physical properties at qualitative temperature

[0075]

[0076] 2. Design Calculation

[0077] Based on the above data, the heat exchanger required in this embodiment is calculated.

[0078] Table 3 Basic parameters of heat exchanger

[0079] project Numeric unit Heat flow 333.33 kw Average heat transfer temperature difference 39.03 ℃ Cooling air consumption 54.55 t / h Temperature correction factor 0.80 Heat transfer temperature difference correction 31.22 ℃ Overall heat transfer coefficient 400 W / (㎡.℃) Heat transfer area 26.69 ㎡ Heat exchange tube specifications Φ19mmx2mm Flow rate in tube 0.70 m / s Number of heat exchange tubes 23 root Heat exchange tube length 24.64 m Specifications Tube Length 4.50 m

[0080] In the above scheme, the heat transfer medium used for sludge drying is dry hot air, and the moisture in the sludge is dried by the air. At the same time, the air always maintains a low humidity state during the treatment process of the entire coking wastewater filter press sludge secondary dehydration system, and is finally discharged after entering the VOCs gas treatment device 9 for treatment.

[0081] Through the coking wastewater filter press sludge secondary dehydration system treatment of the utility model, combined with the above implementation plan, after low-temperature heat exchange of a coking wastewater and sludge drying, the following beneficial effects are obtained:

[0082] Table 4 Effect of program implementation

[0083] project Numeric unit Moisture content of filter press sludge 77.50 ％ Moisture content of dried sludge 47.44 ％ Heat flow 297 kw Saving of circulating water evaporation (estimated) 0.47 t / h

[0084] Through the above specific implementation methods, the residual sludge and coagulation sludge of coking wastewater can be effectively treated and resourced, and the moisture content of the sludge can be reduced by 30%, which is beneficial to the difficulty and energy consumption of subsequent sludge treatment. By draining and cooling the ammonia wastewater, the heat flow of the circulating cooling water can be reduced by 297kW. Calculated by the vaporization heat of water, about 0.47 tons of evaporated water can be saved per hour.

[0085] The coking wastewater filter press sludge secondary dehydration system of the utility model not only has significant economic and social benefits, but also helps to promote the green development and sustainable development of the coking industry, and makes positive contributions to environmental protection and ecological civilization construction.

[0086] Although the embodiments of the present invention have been shown and described, it is understandable to those skilled in the art that various changes, modifications, substitutions and variations may be made to these embodiments without departing from the principle and spirit of the present invention, all of which fall within the scope of protection of the present invention.

Claims

1. A coking wastewater filter press sludge secondary dehydration system, characterized in that: The coking wastewater filter press sludge secondary dehydration system comprises a blower, a heat exchanger and a drying room; Among them, the drying room is equipped with a mud inlet and a mud outlet; The blower is connected to the shell side inlet of the heat exchanger; the shell side outlet of the heat exchanger is connected to the drying room through the air inlet duct; The heat exchanger is provided with a tube-side inlet for coking wastewater serving as a heat source to enter.

2. The coking wastewater filter press sludge secondary dehydration system according to claim 1 is characterized in that: The drying room is a hollow rectangular structure, with the height direction of the drying room as the up and down relationship, and an upper conveyor belt and a lower conveyor belt are arranged in parallel up and down inside the drying room.

3. The coking wastewater filter press sludge secondary dehydration system according to claim 2 is characterized in that: Taking the length direction of the drying room as the left-right relationship, a mud inlet is arranged at the upper end of the left outer wall of the drying room, and a mud outlet is arranged at the left side of the bottom of the drying room.

4. The coking wastewater filter press sludge secondary dehydration system according to claim 2 or 3, characterized in that: The ends of the upper conveyor belt and the lower conveyor belt are respectively provided with scrapers.

5. The coking wastewater filter press sludge secondary dehydration system according to any one of claims 1 to 3, characterized in that: The coking wastewater filter press sludge secondary dehydration system also includes a first heat exchanger for first cooling of the coking wastewater; The tube side inlet of the first heat exchanger is connected to the ammonia still that produces coking wastewater; The tube side outlet of the first heat exchanger is communicated with the tube side inlet of the heat exchanger.

6. The coking wastewater filter press sludge secondary dehydration system according to any one of claims 1 to 3, characterized in that: The coking wastewater filter press sludge secondary dehydration system also includes a second heat exchanger for cooling the coking wastewater again; the tube side outlet of the heat exchanger is connected to the tube side inlet of the second heat exchanger.

7. The coking wastewater filter press sludge secondary dehydration system according to any one of claims 1 to 3, characterized in that: The air inlet duct includes an air inlet main pipe and multiple air inlet branches. One end of the air inlet main pipe is connected to the shell outlet of the heat exchanger, and the other end of the air inlet main pipe is connected to multiple air inlet branches. The multiple air inlet branches are evenly arranged at the top of the drying room, and the air outlet of each air inlet branch pipe is facing downward.

8. The coking wastewater filter press sludge secondary dehydration system according to claim 7, characterized in that: The air inlet branch pipe is also provided with a valve for controlling the air volume of the dry hot air.

9. The coking wastewater filter press sludge secondary dehydration system according to any one of claims 1 to 3, characterized in that: The right side of the bottom of the drying room is also connected with an air outlet duct.

10. The coking wastewater filter press sludge secondary dehydration system according to claim 9, characterized in that: The air outlet duct is connected with the induced draft fan, and the induced draft fan is connected with the VOCs gas treatment device.

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