Device for preparing dilute ammonia water and creosote from semi-coke wastewater

Abstract

The utility model relates to a device for preparing dilute ammonia water and creosote from semi-coke wastewater, and belongs to the field of special equipment for the semi-coke industry. The system comprises a semi-coke wastewater raw water pump, a coalescence separator, a deoiled water storage tank, a deoiled water pump, an alkalization reaction kettle, an alkalized water pump, a rectifying tower, a creosote pump, a compressor, a heat recovery heat exchanger, a main heater, a dilute ammonia water tank and a dilute ammonia water pump. Tar is fully recovered by centrifugal ultrasonic coalescence separation, dilute ammonia water and creosote are separated through alkalization and rectification, and three types of useful products are formed, so that waste is turned into use, and the environmental protection pressure is relieved.

Description

Technical Field

[0001] This utility model belongs to the field of special equipment for the semi-coke industry, specifically relating to a device for producing dilute ammonia and creosote from semi-coke wastewater. Background Technology

[0002] Semi-coke wastewater, also known as semi-coke wastewater, refers to an industrial wastewater formed during the medium- and low-temperature dry distillation (approximately 600–800℃) of low-rank coal (such as non-caking coal, weakly caking coal, and long-flame coal) as well as during coal gas purification and semi-coke steam quenching. This wastewater has a complex composition, containing a large number of recalcitrant and highly toxic pollutants, such as benzene compounds, phenols, polycyclic aromatic hydrocarbons, nitrogen oxide heterocyclic compounds, and other organic pollutants, as well as heavy metal inorganic pollutants. It is difficult to degrade through biological means and is a typical example of highly polluting and highly toxic industrial wastewater.

[0003] Against the backdrop of the coordinated promotion of coal chemical industry upgrading and environmental governance, the resource utilization treatment of semi-coke wastewater has become a key link restricting the sustainable development of the industry. The usable components in semi-coke wastewater can be roughly divided into three categories: tar, ammonia and creosote. After separation and purification, the tar can be used for gasoline and diesel production, the dilute ammonia water can be used for flue gas desulfurization and denitrification, and the creosote can be used for coking powder and coal powder bonding or for brick demolding.

[0004] Therefore, in order to alleviate environmental pressure and simplify the wastewater purification process of semi-coke, it is necessary to develop devices that can separate pollutants and convert them into usable products, especially to solve the problem of efficient separation of three types of components: tar, dilute ammonia, and creosote. Utility Model Content

[0005] To address the aforementioned problems in the existing technology, this utility model provides an apparatus for producing dilute ammonia and creosote from semi-coke wastewater. The technical problem to be solved by this utility model is achieved through the following technical solution:

[0006] This utility model provides an apparatus for producing dilute ammonia and creosote from semi-coke wastewater, comprising: a semi-coke wastewater raw water pump, a coalescing separator, a de-oiled water storage tank, a de-oiled water pump, an alkalization reaction vessel, an alkalization water pump, a distillation column, a creosote pump, a compressor, a heat recovery heat exchanger, a main heater, a dilute ammonia tank, and a dilute ammonia pump; wherein, the semi-coke wastewater raw water pump is connected to an external semi-coke wastewater source, and the coalescing separator is connected to the semi-coke wastewater raw water pump; the coalescing separator is used to separate tar by centrifugation, ultrasonication, and coalescing treatment, and the separated tar is discharged from the lower outlet of the coalescing separator; the upper outlet of the coalescing separator is connected to the de-oiled water storage tank, and the de-oiled water storage tank, the de-oiled water pump, and the... The alkalization reactors are connected in sequence; the alkalization reactors are connected to the heat recovery heat exchanger via the alkalization pump, and the heat recovery heat exchanger is connected to the middle feed inlet of the distillation column via the main heater; the bottom outlet of the distillation column is connected to the creosote pump, and creosote is discharged from the outlet of the creosote pump; the top of the distillation column is connected to the compressor, and the compressor, the heat recovery heat exchanger, the dilute ammonia tank, and the dilute ammonia pump are connected in sequence, and dilute ammonia is discharged from the outlet of the dilute ammonia pump; the tops of the deoiled water storage tank, the alkalization reactor, and the dilute ammonia tank are connected by a gas connection pipe, and a breather valve is installed on the top of the deoiled water storage tank, which is connected to the external atmospheric environment.

[0007] In one embodiment of this utility model, the coalescing separator includes: a spiral centrifuge cylinder, a settling inclined plate, an ultrasonic transducer, and coalescing packing; wherein, the spiral centrifuge cylinder is located near the raw water pump of the semi-coke wastewater, and the spiral centrifuge cylinder, the settling inclined plate, the ultrasonic transducer, and the coalescing packing are arranged in sequence; the coalescing separator is provided with tar outlets at the bottom positions of the front end, the middle part, and the rear end, respectively.

[0008] In one embodiment of this utility model, the deoiled water storage tank is a vertical insulated storage tank, including a liquid inlet at the top and a bottom inner extension section communicating with the liquid inlet.

[0009] In one embodiment of this utility model, the alkalization reactor is an atmospheric pressure jacketed glass-lined reactor, with a star-shaped feed valve, a covered funnel and a manhole at the top, and a ball valve at the bottom; a pressure gauge and a vent pipe are provided at the top of the alkalization reactor near the manhole, and the vent pipe is connected to the top of the deoiled water storage tank.

[0010] In one embodiment of this invention, NaOH or KOH is added to the alkalization reactor from the top to achieve ammonia substitution separation.

[0011] In one embodiment of this utility model, the distillation column is a negative pressure distillation column, comprising: a stripping section and a rectification section, wherein the stripping section is located below the rectification section, the stripping section is filled with Pall ring packing, and the rectification section is filled with corrugated packing.

[0012] In one embodiment of this utility model, the compressor is a Roots type, used to evacuate the top gas phase of the distillation column and to pressurize and heat the gas phase as a mechanically powered heat pump.

[0013] In one embodiment of this utility model, the main heater is any one of an electric heater, a steam heater, or a thermal oil heater.

[0014] In one embodiment of this utility model, the dilute ammonia tank is an atmospheric pressure horizontal tank, the dilute ammonia tank is equipped with a liquid level self-control, and the liquid level of the dilute ammonia tank is interlocked with the outlet valve of the dilute ammonia pump; the reflux valve of the dilute ammonia pump is interlocked with the top of the distillation column through temperature interlocking.

[0015] In one embodiment of this utility model, the dilute ammonia water in the dilute ammonia water pump is divided into two paths after being pressurized by the dilute ammonia water pump. The first path returns to the rectification section of the distillation column, and the second path is discharged from the outlet of the dilute ammonia water pump.

[0016] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0017] This invention provides an apparatus for producing dilute ammonia and creosote from semi-coke wastewater. It utilizes centrifugal ultrasonic coalescence separation to fully recover tar from the organic wastewater discharged during semi-coke production, and separates dilute ammonia and creosote through alkalization and distillation, thus achieving the separation and utilization of useful components in the semi-coke wastewater. This simplifies the semi-coke wastewater purification process, separating pollutants and converting them into usable products. It achieves efficient separation of three components: tar, dilute ammonia, and creosote. The tar can be used for hydrogenation to produce gasoline and diesel, the dilute ammonia for flue gas desulfurization and denitrification, and the creosote can be used in coking and coal pulverization, as well as brick demolding, thus turning waste into resources and alleviating environmental pressure.

[0018] The above description is merely an overview of the technical solution of this utility model. In order to better understand the technical means of this utility model and to implement it in accordance with the contents of the specification, and to make the above and other objects, features and advantages of this utility model more apparent and understandable, preferred embodiments are described below in detail with reference to the accompanying drawings. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the structure of an apparatus for producing dilute ammonia and creosote from semi-coke wastewater according to an embodiment of the present invention;

[0020] Figure 2 This is a schematic diagram of the coalescing separator provided in an embodiment of the present invention.

[0021] Figure labels: 1-Raw water pump for semi-coke wastewater; 2-Coalescing separator; 21-Spiral centrifuge cylinder; 22-Settling inclined plate; 23-Ultrasonic transducer; 24-Coalescing packing; 3-Water storage tank after oil removal; 4-Water pump after oil removal; 5-Alkalization reactor; 6-Water pump after alkalization; 7-Distillation column; 8-Cresol pump; 9-Compressor; 10-Heat recovery heat exchanger; 11-Main heater; 12-Dilute ammonia tank; 13-Dilute ammonia pump. Detailed Implementation

[0022] To further illustrate the technical means and effects adopted by this utility model to achieve its intended purpose, the following describes in detail, with reference to the accompanying drawings and specific embodiments, an apparatus for producing dilute ammonia and creosote from semi-coke wastewater according to this utility model.

[0023] The foregoing and other technical contents, features, and effects of this utility model will be clearly presented in the following detailed description of the specific embodiments with reference to the accompanying drawings. Through the description of the specific embodiments, a more in-depth and specific understanding can be gained of the technical means and effects adopted by this utility model to achieve the intended purpose. However, the accompanying drawings are only provided for reference and illustration and are not intended to limit the technical solution of this utility model.

[0024] Example 1

[0025] Typical oil-water separation effluent from semi-coke wastewater (mainly composed of residual ammonia) has a pH of 8-9, with petroleum hydrocarbon concentrations of 570-700 mg / L, ammonia nitrogen concentrations of 2650-3200 mg / L, and volatile phenol concentrations of 2000-4000 mg / L. To alleviate environmental pressure and simplify the semi-coke wastewater purification process, it is suitable to separate the wastewater to obtain three useful products: tar, dilute ammonia, and phenols. Therefore, to achieve efficient separation of these three components, this embodiment provides an apparatus for producing dilute ammonia and phenols from semi-coke wastewater, such as... Figure 1 As shown, Figure 1 This is a schematic diagram of an apparatus for producing dilute ammonia and creosote from semi-coke wastewater, provided as an embodiment of the present invention.

[0026] In this embodiment, the apparatus for producing dilute ammonia and creosote from semi-coke wastewater includes: a semi-coke wastewater raw water pump 1, a coalescing separator 2, a de-oiled water storage tank 3, a de-oiled water pump 4, an alkalization reactor 5, an alkalization water pump 6, a distillation column 7, a creosote pump 8, a compressor 9, a heat recovery heat exchanger 10, a main heater 11, a dilute ammonia tank 12, and a dilute ammonia pump 13; wherein, the semi-coke wastewater raw water pump 1 is connected to an external semi-coke wastewater source, and the semi-coke wastewater raw water pump 1 is connected to the coalescing separator 2; the coalescing separator 2 is used to separate tar by centrifugation, ultrasonication, and coalescence treatment, and the separated tar is then processed by the coalescing separator 2. The lower outlet of the coalescence separator 2 is connected to the de-oiled water storage tank 3. The de-oiled water storage tank 3, the de-oiled water pump 4, and the alkalization reactor 5 are connected in sequence. The alkalization reactor 5 is connected to the heat recovery heat exchanger 10 via the alkalization water pump 6. The heat recovery heat exchanger 10 is connected to the middle feed port of the distillation column 7 via the main heater 11. The bottom outlet of the distillation column 7 is connected to the phenol pump 8. The phenol is discharged from the outlet of the phenol pump 8. The top of the distillation column 7 is connected to the compressor 9. The compressor 9, the heat recovery heat exchanger 10, the dilute ammonia water tank 12, and the dilute ammonia water pump 13 are connected in sequence. The dilute ammonia water is discharged from the outlet of the dilute ammonia water pump 13.

[0027] In one optional embodiment, the tops of the deoiled water storage tank 3, the alkalization reactor 5, and the dilute ammonia tank 12 are connected by an air-to-water connection pipe. The top of the deoiled water storage tank 3 is equipped with a breather valve, which is connected to the external atmospheric environment.

[0028] like Figure 2 As shown, Figure 2 This is a schematic diagram of the coalescing separator provided in an embodiment of the present invention.

[0029] In one optional embodiment, the coalescing separator 2 includes: a spiral centrifuge cylinder 21, a settling inclined plate 22, an ultrasonic transducer 23, and coalescing packing 24; wherein, the spiral centrifuge cylinder 21 is located on the side close to the raw water pump 1 for semi-coke wastewater, and the spiral centrifuge cylinder 21, the settling inclined plate 22, the ultrasonic transducer 23, and the coalescing packing 24 are arranged in sequence; the coalescing separator 2 is provided with tar outlets at the bottom positions of the front end, the middle part, and the rear end, respectively.

[0030] For example, the aqueous phase separated by the coalescing separator 2 is discharged from the upper outlet at the tail end to the de-oiled water storage tank 3, and then connected to the upper inlet of the alkali reaction vessel 5 by the de-oiled water pump 4. The tar is discharged from the tar outlets at the front, middle and rear bottom, respectively. The function of each tar outlet is to discharge the separated tar at different stages, ensuring that the tar can be discharged from the coalescing separator 2 in a timely manner, avoiding the accumulation of tar in the coalescing separator 2, thereby improving the tar separation efficiency.

[0031] Specifically, the tar outlets are located below the settling inclined plate 22 and below the front and rear ends of the coalescing packing 24.

[0032] In one optional embodiment, the deoiled water storage tank 3 is a vertical insulated tank, including an inlet at the top and a bottom extension communicating with the inlet. The top inlet helps reduce static electricity accumulation, improving the safety of the tank and the uniformity of the liquid. Meanwhile, the bottom extension extends downwards to the bottom of the tank. When the liquid enters the tank through the bottom extension, it creates a certain agitation at the bottom, helping to stir up sediment and prevent its accumulation. The bottom extension also ensures that the liquid is evenly distributed at the bottom, preventing it from concentrating at a single point and ensuring uniform distribution throughout the tank. This improves the mixing effect of the liquid and further enhances the efficiency of subsequent processing.

[0033] For example, the top of the deoiled water storage tank 3 is equipped with a breather valve with a flame arrester, and the top and bottom sides are also equipped with maintenance manholes. Ladders that meet safety standards are installed inside and outside the tank body, and the tank body is grounded to protect against lightning and static electricity after installation.

[0034] In one optional embodiment, the alkalization reactor 5 is an atmospheric pressure jacketed glass-lined reactor, with a star-shaped feed valve, a covered funnel and a manhole at the top, and a ball valve at the bottom; a pressure gauge and a vent pipe are installed at the top of the alkalization reactor 5 near the manhole.

[0035] For example, the vent pipe is connected to the top of the deoiled water storage tank 3 to maintain atmospheric pressure and ensure that the gas pressure is consistent throughout.

[0036] For example, the top of the alkalization reactor 5 is equipped with a liquid level monitor and a sight glass with a light.

[0037] In an optional embodiment, NaOH or KOH is added from the top of the alkalization reactor 5 to achieve ammonia substitution separation.

[0038] In one optional embodiment, the distillation column 7 is a negative pressure distillation column, including a stripping section and a rectification section, wherein the stripping section is located below the rectification section and is filled with Pall ring packing, and the rectification section is filled with corrugated packing.

[0039] For example, the distillation column 7 is designed to operate at a pressure of -0.1 MPa to 0.4 MPa, and the stripping section is filled with... Pall ring packing, and 250Y corrugated packing for the rectification section.

[0040] For example, the distillation column 7 is provided with a top gas phase outlet, which is connected to a compressor 9. The gas phase is pressurized and heated by the compressor 9 to achieve sufficient heat exchange, and after being further heated in the heat recovery heat exchanger 10, it enters the distillation column 7 from the middle.

[0041] For example, the bottom of the distillation column 7 is equipped with a local level gauge and a remote level gauge, and the top is equipped with a local pressure gauge, a remote positive and negative pressure gauge and a thermometer, and the pressure gauge at the top is 7 meters above the ground.

[0042] In an alternative implementation, since the heavy components at the bottom of the distillation column 7 gradually concentrate and become significantly viscous, the creosote pump 8 can be a gear or screw positive displacement pump, while the semi-coke wastewater pump 1, the deoiling pump 4, the alkalization pump 6, and the dilute ammonia pump 13 can all be self-priming pumps.

[0043] In an alternative implementation, the compressor 9 is a Roots type, used to evacuate the top vapor phase of the distillation column 7 and to pressurize and heat the vapor phase as a mechanically powered heat pump.

[0044] It is worth noting that the compressor 9 uses the principle of a mechanically operated heat pump to raise the vapor phase at the top of the distillation column 7 from a low temperature to a high temperature. Then, the heat is transferred to the cold feed through the heat recovery heat exchanger 10, achieving full recovery and reuse of thermal energy. This process not only improves energy utilization efficiency but also reduces the operating cost of the unit, demonstrating significant energy-saving effects and environmental benefits.

[0045] In one alternative embodiment, the main heater 11 is any one of an electric heater, a steam heater, or a thermal oil heater.

[0046] For example, the main heater 11 may be an electric heater, and the temperature of the electric heater may be automatically controlled by the input electrical power.

[0047] In one optional embodiment, the dilute ammonia tank 12 is an atmospheric pressure horizontal tank. The dilute ammonia tank 12 is equipped with a liquid level control system, and the liquid level of the dilute ammonia tank 12 is interlocked with the outlet valve of the dilute ammonia pump 13. The reflux valve of the dilute ammonia pump 13 is interlocked with the top of the distillation column 7 through temperature control. If the top temperature of the distillation column 7 exceeds the set threshold, the reflux valve of the dilute ammonia pump 13 will automatically open to return the dilute ammonia to the distillation section.

[0048] For example, the dilute ammonia water separated from the distillation column 7 enters the upper inlet of the dilute ammonia water tank 12 through the heat recovery heat exchanger 10, and is then connected to the dilute ammonia water pump 13 through the lower outlet of the dilute ammonia water tank 12.

[0049] In one optional embodiment, the dilute ammonia water in the dilute ammonia water pump 13 is pressurized by the dilute ammonia water pump 13 and then divided into two paths. The first path returns to the rectification section of the distillation column 7, and the second path is discharged from the outlet of the dilute ammonia water pump 13.

[0050] Understandably, the apparatus for producing dilute ammonia and creosote from semi-coke wastewater in this embodiment uses stainless steel that meets pressure and corrosion standards for all main equipment, pipelines, instruments and pumps, and is equipped with an external insulation structure to meet the needs of the operating environment. The electrical automation also meets explosion-proof requirements and the communication protocols of the operating site.

[0051] The working process of the apparatus for producing dilute ammonia and creosote from semi-coke wastewater in this embodiment is as follows:

[0052] The raw wastewater from semi-coke contains emulsified and dissolved tar. Pressurized by pump 1, it enters the coalescing separator 2. First, a centrifugal force field is formed in the spiral centrifuge cylinder 21, causing large tar particles with significant density differences and mechanical impurities to coalesce and aggregate, overcoming buoyancy limitations and settling at the bottom. The tar is periodically discharged from the tar outlet at the bottom front. Then, the aqueous phase rises through the settling inclined plate 22, further separating the tar by reducing flow velocity and expanding the settling area, forming a tar layer that drips back to the bottom front of the coalescing separator 2. This de-oiled aqueous phase enters the middle section of the coalescing separator 2, where, under the action of the ultrasonic transducer 23, it overcomes the limitations of the microemulsion double electric layer, forming larger tar droplets for further tar separation. The tar is periodically discharged and recovered from the tar outlet at the bottom center. The aqueous phase continues downstream, passing through the surface-modified coalescing packing 24, where a undulating flow field promotes the gradual affinity adsorption and sedimentation of the mist-like tar, resulting in a clear and transparent aqueous phase, reaching the physical oil separation limit. The coalesced tar is deposited at the tar outlet at the bottom end and discharged periodically; the aqueous phase is monitored by a liquid level analyzer and discharged from the top end, entering the deoiled water storage tank 3.

[0053] After oil removal, the water storage tank 3 has a top-inlet and bottom-outlet design. The inlet is recessed to the bottom of the tank and turned horizontally to ensure thorough mixing. Static electricity generated during liquid transport is discharged via external grounding. The top of the water storage tank 3 is equipped with a breather valve with a flame arrester to maintain pressure consistent with the outside atmosphere. A radar level gauge is also installed on the top of the water storage tank 3 to prevent overflow. To avoid heat waste, the pipelines and tank body are insulated to meet environmental requirements. The water storage tank 3 serves as a homogenizing and buffering storage system, facilitating continuous operation between upstream and downstream processes and achieving flexible balance.

[0054] After oil removal, water pump 4 pumps the de-oiled water from storage tank 3 into the alkalization reactor 5 in batches. NaOH or KOH is added from the top at a mass ratio of 0.1% to 1%, and after stirring for 1 to 5 minutes for appropriate alkalization, the alkalized water is pumped by water pump 6 to subsequent units. The chemical principle of this process is to replace the bound ammonia with alkali, increasing ammonia collection; through alkalization, the weak acid organic compounds are fully attracted to the active metal ions, preventing azeotropic entrainment during distillation, resulting in a colorless and clear light phase with thorough purification, while the heavy phase is free of foaming, with a clear interface, preventing packing blockage and upward movement, thus improving separation efficiency; and through the combination of trace amounts of alkali with organic components, a surfactant effect is formed, improving the long-term storage resistance of phenols.

[0055] After alkalization, water pump 6 delivers the aqueous phase to heat recovery heat exchanger 10, where it fully exchanges heat with the vapor phase at the top of distillation column 7 after being pressurized and heated by compressor 9. After preheating, it enters the main heater 11 for further heating and enters from the stripping section of distillation column 7 via flash evaporation. It is fully dispersed in the packing to expand the evaporation area and achieve separation of light and heavy components. The light components pass upward through the packing of the distillation section and fully exchange heat with the top reflux superfluous liquid. After purification, the vapor phase enters the compressor 9 from the top. The compressor 9 forms a mechanical energy heat pump. After the vapor phase is compressed and heated by the compressor 9, it exchanges heat with the cold feed of the heat recovery heat exchanger 10 through the high temperature difference. Afterwards, the liquefied ammonia enters the dilute ammonia tank 12 after the steam trap. The dilute ammonia in the dilute ammonia tank 12 is pressurized and transported by the dilute ammonia pump 13 and divided into two paths. One path returns to the packing of the rectification section at the top of the distillation column 7, and is evenly distributed to control the temperature and purity of the top of the column. The other path discharges the excess amount under the control of the liquid level in the dilute ammonia tank 12 as dilute ammonia product.

[0056] The heavy components at the bottom of the distillation column 7 are pressurized and transported by the creosote pump 8. In the initial stage, before the temperature field inside the column is established, the bottom product creosote is refluxed to the heat recovery heat exchanger 10 and is not discharged. After the concentration reaches the standard and the column distillation balance is established, it is gradually changed to discharge, and the circulation ratio is gradually reduced until the self-circulation is shut off. Finally, all of it is discharged through liquid level control, becoming the product creosote.

[0057] During shutdown, to prevent freezing and blockage due to temperature drop, the raw water pump 1 and coalescing separator 2 for semi-coke wastewater are first washed and replaced with hot soft water. After thorough drainage, they are dried with compressed nitrogen. The deoiled water storage tank 3 is allowed to store liquid for a long time and does not require treatment. Next, the deoiled water pump 4, alkalization reactor 5, alkalization water pump 6, distillation column 7, creosote pump 8, compressor 9, heat recovery heat exchanger 10, main heater 11, dilute ammonia tank 12, and dilute ammonia pump 13 are sequentially washed and drained with hot soft water and dried with compressed nitrogen.

[0058] To avoid substandard products during initial use, the discharged tar, dilute ammonia, and phenols can be returned to the front of the unit to achieve a circulating feed until a stable and balanced product output is achieved, after which the process can be switched to output harvesting.

[0059] Understandably, the apparatus for producing dilute ammonia and creosote from semi-coke wastewater in this embodiment allows for frequency conversion control of all pump components to maximize energy savings; and anti-vibration blocks are installed between moving parts and fixed areas (such as platform foundations or steel structures) to effectively prevent resonance damage and control noise levels. Furthermore, soft connections and expansion bends are used for buffering in areas of concentrated temperature stress, but this invention does not impose structural limitations on these aspects.

[0060] This invention provides an apparatus for producing dilute ammonia and creosote from semi-coke wastewater. It utilizes centrifugal ultrasonic coalescence separation to fully recover tar from the organic wastewater discharged during semi-coke production, and separates dilute ammonia and creosote through alkalization and distillation, thus achieving the separation and utilization of useful components in the semi-coke wastewater. This simplifies the semi-coke wastewater purification process, separating pollutants and converting them into usable products. It achieves efficient separation of three components: tar, dilute ammonia, and creosote. The tar can be used for hydrogenation to produce gasoline and diesel, the dilute ammonia for flue gas desulfurization and denitrification, and the creosote can be used in coking and coal pulverization, as well as brick demolding, thus turning waste into resources and alleviating environmental pressure.

[0061] It should be noted that, in this document, relational terms such as "first" and "second" are used merely to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations are intended to cover non-exclusive inclusion, such that an article or device comprising a list of elements includes not only those elements but also other elements not expressly listed. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the article or device comprising said element. Terms such as "connected" or "linked" are not limited to physical or mechanical connections but can include electrical connections, whether direct or indirect. The orientations or positional relationships indicated by terms such as "upper," "lower," "left," and "right" are based on the orientations or positional relationships shown in the accompanying drawings and are used only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the invention.

[0062] The above description, in conjunction with specific preferred embodiments, provides a further detailed explanation of the present invention. It should not be construed that the specific implementation of the present invention is limited to these descriptions. For those skilled in the art, various simple deductions or substitutions can be made without departing from the concept of the present invention, and all such modifications and substitutions should be considered within the protection scope of the present invention.

Claims

1. An apparatus for producing dilute ammonia and creosote from semi-coke wastewater, characterized in that, The application relates to a device for treating green coke wastewater, which comprises a green coke wastewater raw water pump (1), a coalescence separator (2), a water storage tank after oil removal (3), a water pump after oil removal (4), an alkalization reaction kettle (5), a water pump after alkalization (6), a rectifying tower (7), a phenol pump (8), a compressor (9), a heat recovery heat exchanger (10), a main heater (11), a dilute ammonia water tank (12) and a dilute ammonia water pump (13). The green coke wastewater raw water pump (1) is connected with external green coke wastewater raw water, and the green coke wastewater raw water pump (1) is connected with the coalescence separator (2); the coalescence separator (2) is used for separating tar through centrifugal, ultrasonic and coalescence treatment; the separated tar is discharged from a lower outlet of the coalescence separator (2); an upper outlet of the coalescence separator (2) is connected with the water storage tank after oil removal (3), and the water storage tank after oil removal (3), the water pump after oil removal (4) and the alkalization reaction kettle (5) are sequentially connected. The alkalization reaction kettle (5) is connected with the heat recovery heat exchanger (10) through the water pump after alkalization (6), the heat recovery heat exchanger (10) is connected with the middle feeding port of the rectifying tower (7) through the main heater (11). The bottom liquid outlet of the rectifying tower (7) is connected with the phenol pump (8), and the phenol is discharged from the outlet of the phenol pump (8); the top of the rectifying tower (7) is connected with the compressor (9), and the compressor (9), the heat recovery heat exchanger (10), the dilute ammonia water tank (12) and the dilute ammonia water pump (13) are sequentially connected; the dilute ammonia water is discharged from the outlet of the dilute ammonia water pump (13). The top of the water storage tank after oil removal (3), the alkalization reaction kettle (5) and the dilute ammonia water tank (12) is connected through a gas phase communication pipe, a breather valve is arranged at the top of the water storage tank after oil removal (3), and the breather valve is connected with an external atmosphere. The coalescence separator (2) comprises a spiral centrifugal cylinder (21), a settlement inclined plate (22), an ultrasonic vibrator (23) and coalescence filler (24); the spiral centrifugal cylinder (21) is arranged on the side close to the green coke wastewater raw water pump (1), and the spiral centrifugal cylinder (21), the settlement inclined plate (22), the ultrasonic vibrator (23) and the coalescence filler (24) are sequentially arranged; tar outlets are arranged at the bottom positions of the front end, the middle and the rear end of the coalescence separator (2).

2. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The water storage tank after oil removal (3) is a vertical heat preservation storage tank, which comprises an inlet arranged at the upper portion and a bottom inner extension section communicated with the inlet.

3. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The alkalization reaction kettle (5) is a normal pressure jacketed glass reaction kettle, which is provided with a star-shaped feeding valve, a funnel with a cover and a manhole at the top and a ball valve at the bottom; a pressure gauge and a venting pipeline are arranged at the top of the alkalization reaction kettle (5) close to the manhole, and the venting pipeline is communicated with the top of the water storage tank after oil removal (3).

4. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, NaOH or KOH is added into the alkalization reaction kettle (5) from the top, so that ammonia replacement separation is realized.

5. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, ​ 6. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The rectification tower (7) is a negative pressure rectification tower, comprising a stripping section and a rectification section, the stripping section is below the rectification section, the stripping section is filled with Pall ring packing, and the rectification section is filled with corrugated packing.

7. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The compressor (9) is a Roots compressor, which is used for vacuumizing the top gas phase of the rectification tower (7) and pressurizing and heating the gas phase as a mechanical work heat pump.

8. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The main heater (11) is any one of an electric heater, a steam heater or a heat conducting oil heater.

9. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 1, characterized in that, The dilute ammonia water tank (12) is a normal pressure horizontal tank, the dilute ammonia water tank (12) is provided with liquid level self-control, and the liquid level of the dilute ammonia water tank (12) is interlocked controlled with the take-out valve of the dilute ammonia water pump (13); the backflow valve of the dilute ammonia water pump (13) is temperature interlocked controlled with the top of the rectification tower (7).

10. The apparatus for producing dilute ammonia water and creosote from semicoke wastewater according to claim 6, characterized in that, The dilute ammonia water in the dilute ammonia water pump (13) is divided into two ways after being pressurized by the dilute ammonia water pump (13), wherein the first way returns to the rectification section of the rectification tower (7); and the second way is discharged from the outlet of the dilute ammonia water pump (13).

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