Feeding system and process for a high-temperature organic wastewater treatment device

Abstract

A feeding system for an organic wastewater treatment device includes a gasifier mixer, a steam supply end, burners, and pipelines. Following the steam flow direction within the mixer, the mixer sequentially includes a swirl atomization section, a throttling atomization section, and a vortex atomization section, which are interconnected. The swirl atomization section is cavity I, with swirl atomizing nozzles disposed inside. Cavity I also has an organic wastewater inlet connected to the swirl atomizing nozzles. The throttling atomization section is cavity II, comprising an upper section with a narrower diameter and a lower section with a wider diameter. The vortex atomization section includes cavity III, which contains a structure for generating vortices. Steam enters the swirl atomization section, and organic wastewater enters the swirl atomization nozzle. The steam and organic wastewater sprayed from the swirl atomization nozzle pass through the throttling atomization section and the vortex atomization section in sequence, and are then discharged from the vortex atomization section. The steam and organic wastewater discharged from the vortex atomization section enter the gasifier through the burner.

Description

Technical Field

[0001] This invention relates to the field of chemical technology, specifically to a feeding system and process for a high-temperature organic wastewater treatment device. Background Technology

[0002] With the rapid development of the national economy and the significant improvement in people's living standards, the output of urban sewage, chemical wastewater, and waste liquids has also increased dramatically. Every year, my country's petrochemical, metallurgical, papermaking, leather tanning, fermentation and brewing, pharmaceutical, and textile printing and dyeing industries generate tens of thousands of tons of organic waste liquids. These industries discharge large quantities of organic waste liquids with high concentrations, and some of them contain toxic and harmful substances, posing a serious challenge to our living environment and ecology.

[0003] Organic wastewater contains a large amount of organic pollutants. Due to the high carbon and hydrogen content in its molecules, treating it as a potential resource, rather than simply treating it as polluting waste, represents a new concept of resource and ecological harmony. Utilizing it as a raw material for some chemical products not only effectively utilizes organic pollutants and prevents their harm at the source, but also generates new profit models through chemical production. This will be the most environmentally friendly and effective way to treat and utilize organic wastewater in the future.

[0004] Resource utilization of high-concentration organic wastewater refers to the reuse of valuable components remaining in wastewater or the reuse of water resources after wastewater treatment. To this end, environmentalists both domestically and internationally have developed many resource utilization technologies for high-concentration organic wastewater based on its characteristics, achieving good results. These technologies are mainly divided into three categories: (1) oxidation and biochemical treatment; (2) incineration; and (3) combustion or gasification of wastewater and coal slurry.

[0005] Oxidation and biochemical treatment methods are used. However, in biochemical treatment, toxic and harmful substances in organic wastewater can easily cause the biochemical bacteria to become inactive. Therefore, it is necessary to build physical and chemical pretreatment devices to ensure the efficiency of biochemical treatment. Moreover, biochemical treatment is only suitable for treating low-concentration organic wastewater.

[0006] Incineration refers to the process of destroying the molecular structure of various harmful substances in wastewater through a controlled high-temperature chemical reaction within the combustion chamber of an incinerator, oxidizing the organic matter in the wastewater into harmless substances such as CO and H2O. It is suitable for treating high-concentration organic wastewater. However, the exhaust gas produced by incinerating organic wastewater mainly consists of steam, soot, SO2, and NO2. To ensure that the exhaust gas meets emission standards, auxiliary devices such as quenching, desulfurization, and denitrification are required. High investment, high operating costs, and low returns are the main factors restricting the widespread application of incineration technology for treating organic wastewater.

[0007] The core flame temperature inside the gasifier of fluidized bed gasification technology is generally around 2000℃. At this high temperature, organic matter decomposes and burns into inorganic gases. Fluidized bed gasification has inherent advantages in treating organic matter in wastewater. Furthermore, harmful substances such as organic matter in the wastewater can undergo gasification reactions within the gasifier to generate syngas. However, currently, my country has many types of fluidized bed technologies and complex raw materials. Retrofitting existing fluidized bed gasification devices for co-firing organic wastewater is limited not only by the gasifier's structure but also by the properties of the gasification feedstock. High investment and large engineering workload in retrofitting hinder the widespread application of fluidized bed gasification technology for treating organic wastewater.

[0008] The existing high-temperature organic wastewater treatment devices and their feeding systems and processes mainly include a pulverized coal co-firing high-concentration organic wastewater composite gasification burner and process method disclosed in Chinese patent application (CN107189820A). The process method involves pulverized coal and organic wastewater being delivered to the burner via a pipeline. The burner's ignition gun is externally mounted separately, and the pulverized coal feed and wastewater co-firing are set up as independent channels. Ignition and start-up venting gas are in the same channel, and the oxygen from the organic wastewater and the start-up oxygen are in the same channel. The pulverized coal channel is set in the outer ring of the burner, and other gasifier structure improvements are made to achieve the co-firing of organic wastewater in pulverized coal gasification.

[0009] Chinese patent application (CN113266836A) discloses a gasifier feeding process for treating organic waste liquid, wherein the organic waste liquid feeding system includes an organic waste liquid buffer tank, an organic waste liquid feed pump, and a waste liquid burner.

[0010] Chinese patent application (CN112226248A) discloses a pulverized coal gasification device and its process for co-firing organic wastewater. The gasifier is equipped with an interface for installing an ignition burner, and the pulverized coal gasification device also includes a wastewater nozzle, which can also be installed on the interface. The interface, originally used for installing the ignition burner, is now used for installing the wastewater nozzle. This eliminates the need to modify the gasifier or install a dedicated wastewater inlet on the gasifier, thus fully utilizing the existing interface of the gasifier and combining it with the newly added wastewater nozzle to atomize the wastewater.

[0011] The existing organic wastewater co-firing process still has the following problems:

[0012] (1) The adjustable range of organic wastewater feed temperature is narrow and it is difficult to reach more than 300℃. For heavy oil gasification burners, low temperature fluid will reduce the burner temperature. The temperature reduction will lead to a significant increase in the viscosity of heavy oil, which will result in an excessive burner pressure difference. In severe cases, it will affect the operation of the device. Currently, the organic wastewater addition technology is limited by the generation of gasification raw materials.

[0013] (2) The adjustable range of organic wastewater feed flow rate is narrow. Because organic wastewater is directly sprayed into the gasifier through the nozzle, the feed needs to ensure that the minimum flow rate of wastewater is atomized in the wastewater nozzle. However, organic wastewater is generally the three wastes of chemical plants, not products. Moreover, some organic reactors are operated intermittently, and the flow rate fluctuates greatly. The existing organic wastewater addition technology is difficult to adapt to the large flow rate fluctuation. In severe cases, the wastewater burner needs to be frequently started and stopped.

[0014] (3) Low-temperature liquid is directly injected into the gasifier through the liquid phase, which has a significant impact on the temperature field and flow field inside the gasifier. This method of addition has poor stability. In order to reduce the impact on the long-term operation of the equipment and product quality, separate wastewater nozzles need to be set up to reduce the impact on the flow field inside the gasifier, which leads to system complexity and increases the cost of the equipment to a certain extent. Some technologies even require modification of the gasifier to optimize the temperature field and flow field inside the furnace. Summary of the Invention

[0015] To address the aforementioned problems in the prior art, this invention proposes a feeding system and process for an organic wastewater treatment device.

[0016] In a first aspect, the present invention proposes a feeding system for an organic wastewater treatment device, wherein the organic wastewater treatment device is a gasifier;

[0017] The feeding system includes: a mixer, a steam supply unit, burners, and piping; the steam supply unit stores steam.

[0018] According to the flow direction of steam in the mixer, the mixer sequentially includes a swirl atomization section, a throttling atomization section, and a vortex atomization section. The swirl atomization section, the throttling atomization section, and the vortex atomization section are connected to each other. Steam flows through the swirl atomization section, the throttling atomization section, and the vortex atomization section in the mixer in sequence. Specifically, the swirl atomization section, the throttling atomization section, and the vortex atomization section are either fixedly connected or detachably connected.

[0019] The swirl atomization section is cavity I, which is equipped with swirl atomizing nozzles and an organic wastewater inlet connected to the swirl atomizing nozzles. A swirl atomizer is installed inside the swirl atomizing nozzles.

[0020] The throttling and atomizing section is cavity II, which consists of an upper section and a lower section. The upper section has a narrower diameter, and the lower section has a wider diameter. The length of the upper section is shorter than the length of the lower section.

[0021] The vortex atomization section includes cavity III, which has a structure for generating vortices inside. Specifically, after the fluid enters the vortex atomization section, the fluid can generate vortices within the vortex atomization section under the action of the structure that generates vortices.

[0022] The structure that generates eddies in this invention can be any structure that generates eddies in the prior art.

[0023] Steam discharged from the steam supply end enters the swirl atomization section through pipeline I. Organic wastewater enters the swirl atomization nozzle through the organic wastewater inlet. After the steam and the organic wastewater sprayed from the swirl atomization nozzle are mixed, they pass through the throttling atomization section and the vortex atomization section in sequence, and are discharged from the vortex atomization section. The steam discharged from the vortex atomization section and the organic wastewater enter the gasifier through the burner through pipeline II.

[0024] Steam enters cavity I through the top of cavity I, while organic wastewater enters the swirl atomizing nozzle through the organic wastewater inlet. After being atomized for the first time by the swirl atomizer, it is sprayed out from the swirl atomizer nozzle.

[0025] The organic wastewater sprayed from the swirl atomizing nozzle mixes with steam and enters chamber II. In chamber II, after the upper section narrows and throttles, a high-speed fluid is formed. The high-speed fluid enters the lower section and rapidly diffuses after throttling, forming a partial negative pressure zone. Strong turbulence is generated in this zone. The organic wastewater is further atomized in this section and further mixed with steam to form mist I. Mist I includes organic wastewater droplets and steam. Mist I is discharged from chamber II.

[0026] Aerosol I enters the vortex atomization section (cavity III), where organic wastewater droplets and steam undergo full heat and mass transfer. Part of the organic wastewater on the surface of the droplets is vaporized in this stage, further reducing the droplet diameter. The organic wastewater is further atomized in this section, and the organic wastewater and steam form aerosol II. Aerosol II is discharged from the bottom of cavity III and enters the gasifier through the burner.

[0027] In a specific embodiment of the present invention, the structure that generates vortex atomization is a plurality of cross-shaped baffles arranged sequentially from top to bottom inside cavity III. The baffles in the present invention can be other baffle structures capable of generating vortices in the fluid inside cavity III.

[0028] Preferably, the cross-shaped stop bar includes an intersection point and four sides. The four sides are arranged in cavity III, and the side lengths of the four sides are equal. The intersection point is on the same straight line in the vertical direction. In the bottom view of cavity III, the four sides of several cross-shaped stop bars do not overlap.

[0029] As a specific embodiment of the present invention, the feeding system also includes a buffer tank, which stores organic wastewater. The buffer tank includes a buffer tank outlet and a buffer tank return port, and the buffer tank outlet is connected to the organic wastewater inlet through pipeline III.

[0030] Specifically, the buffer tank is a sealed container.

[0031] As a specific embodiment of the present invention, the feeding system also includes a booster pump, which is installed in pipeline III, located between the buffer tank and the mixer.

[0032] As a specific embodiment of the present invention, the burner is a composite burner.

[0033] As a specific embodiment of the present invention, pipeline III is further provided with a flow regulating valve and a shut-off valve. The flow regulating valve is located between the booster pump and the mixer; the shut-off valve is located between the flow regulating valve and the mixer.

[0034] In a specific embodiment of the present invention, the return port and the booster pump are connected by pipeline IV, and pipeline IV is equipped with shut-off valve II.

[0035] In a specific embodiment of the present invention, the buffer tank includes a pressure regulating valve one and a pressure regulating valve two. The pressure regulating valve one and the pressure regulating valve two are used to regulate the pressure inside the buffer tank.

[0036] In a specific embodiment of the present invention, the buffer tank further includes a safety valve and a shut-off valve. The safety valve has an automatic pressure relief function to ensure the safety of the buffer tank. The shut-off valve is used to control whether upstream organic wastewater enters the buffer pipe.

[0037] In a specific embodiment of the present invention, pipeline I is equipped with a flow regulating valve II and a shut-off valve IV. The flow regulating valve II is used to regulate the gas flow rate entering the mixer, and the shut-off valve IV is used to control whether gas enters the mixer.

[0038] In a second aspect, the present invention provides a feeding process for an organic wastewater treatment device, employing the feeding system for the organic wastewater treatment device provided in the first aspect of the present invention, comprising the following steps:

[0039] Step 1: Steam from the steam supply end enters the swirl atomization section, and organic wastewater enters the swirl atomization nozzle through the organic wastewater inlet. The organic wastewater is then atomized by the swirl atomization nozzle and sprayed out.

[0040] Step 2: The organic wastewater sprayed from the swirl atomizing nozzle and the steam enter the throttling atomization section together. In the throttling atomization section, the organic wastewater continues to atomize and mixes with the steam to form mist I. Mist I is discharged from the throttling atomization section.

[0041] Step 3: Aerosol I enters the vortex atomization section, where the organic wastewater in aerosol I continues to be atomized. The atomized organic wastewater and steam form aerosol II, which is discharged from the vortex atomization section and enters the gasifier through the burner.

[0042] As a specific embodiment of the present invention, in step one, the organic wastewater is collected by the buffer tank and discharged from the outlet of the buffer tank. The organic wastewater discharged from the outlet of the buffer tank enters the swirl atomization section.

[0043] As a specific embodiment of the present invention, the organic wastewater discharged from the outlet of the buffer tank enters the swirl atomization section under the action of the booster pump.

[0044] In a specific embodiment of the present invention, the flow rate of the organic wastewater discharged from the outlet of the buffer tank in step one is controlled by a flow regulating valve during the process of entering the vortex atomization section.

[0045] As a specific embodiment of the present invention, the flow rate of organic wastewater discharged from the outlet of the buffer tank is 0-35t / h.

[0046] In a specific embodiment of the present invention, the mass ratio of the organic wastewater entering the gasifier to the amount of coal fed into the gasifier is 1:5. This mass ratio is a dry basis mass ratio.

[0047] In a specific embodiment of the present invention, the mass ratio of the organic wastewater entering the gasifier to the amount of coal fed into the gasifier is less than 1:5. This mass ratio is a dry basis mass ratio.

[0048] As a specific embodiment of the present invention, the amount of steam used per ton of organic wastewater is greater than 20m³. 3 .

[0049] As a specific embodiment of the present invention, the amount of steam used per ton of organic wastewater is equal to 20m³. 3 .

[0050] To ensure the atomization effect of organic wastewater, the amount of steam used per ton of organic wastewater must be no less than 20m³. 3 .

[0051] In a specific embodiment of the present invention, the steam flow rate is greater than 100 m³ / h. 3 / h.

[0052] In a specific embodiment of the present invention, the steam flow rate is equal to 100m³. 3 / h.

[0053] When no organic wastewater is added to the mixer or the amount of organic wastewater is small, the steam flow rate must be greater than or equal to 100 m³ / h to ensure continuous system operation. 3 / h.

[0054] As a specific embodiment of the present invention, after the feeding system of the organic wastewater treatment device is started, the first shut-off valve is closed and the second shut-off valve is opened. The booster pump controls the organic wastewater to flow back to the buffer tank through the return port. After the outlet pressure of the booster pump stabilizes, the first shut-off valve is opened and the second shut-off valve is closed. The booster pump controls the organic wastewater to enter the mixer.

[0055] As a specific embodiment of the present invention, before shutting down the feeding system of the organic wastewater treatment device, the shut-off valve is closed first, and then the booster pump is shut down, so that the organic wastewater addition system operates independently of the gasifier system.

[0056] In a specific embodiment of the present invention, the pressure inside the buffer tank is controlled by adjusting pressure regulating valve one and pressure regulating valve two during the reaction process.

[0057] In a specific embodiment of the present invention, the organic wastewater is controlled by a shut-off valve three to determine whether it enters the buffer tank.

[0058] As a specific embodiment of the present invention, the safety of the buffer tank is ensured by the automatic pressure relief function of the safety valve.

[0059] In a specific embodiment of the present invention, the flow rate of steam entering the mixer is controlled by adjusting the flow regulating valve 2, and the temperature of the organic wastewater discharged from the vortex atomization section is adjusted by controlling the gas flow rate.

[0060] In a specific embodiment of the present invention, the gas is controlled to enter the mixer by means of a shut-off valve.

[0061] Thirdly, the present invention provides an application of the feeding system of the organic wastewater treatment device provided in the first aspect of the present invention or the organic wastewater treatment feeding process provided in the second aspect of the present invention in the treatment of organic wastewater, wherein the organic wastewater is organic wastewater generated by coal chemical industry or organic wastewater generated by petrochemical industry.

[0062] Preferably, the organic wastewater is one of the organic wastewater generated by the MTO unit, the PDH unit, and the EVA unit. Because the organic wastewater generated by the MTO unit, PDH unit, and EVA unit has high calorific value, low boiling point, and high volatility, the feeding system and process of the organic wastewater treatment device of this invention provide good economic benefits when used to treat it.

[0063] The MTO unit is a methanol-to-olefins unit, the PDH unit is a propane dehydrogenation unit, and the EVA unit is an ethylene-vinyl acetate unit.

[0064] Because the gasifier has a coaxial confined jet flow field structure, there are jet zone and recirculation zone. The recirculation zone is relatively large and intense. The organic wastewater liquid phase feed has a large disturbance to the original flow field and a significant impact on particle residence time. In severe cases, it can lead to insufficient reaction in some areas. However, gas phase feed can optimize the particle residence time distribution and create conditions to promote the coal char reaction.

[0065] When organic waste liquid is fed into the gasifier at low temperature in the liquid phase, it evaporates rapidly and undergoes a decomposition reaction. The decomposition zone is larger and occurs earlier than that of coal, which ultimately leads to a downward shift of the secondary reaction zone of coal and char, reducing the carbon conversion rate of the original reaction. In contrast, when organic waste liquid is fed into the gas phase at high temperature, it undergoes a decomposition reaction directly in the gasifier, significantly reducing the downward shift of the secondary reaction zone of coal and char and having little impact on the carbon conversion rate of the original reaction.

[0066] Under the condition of constant oxygen and coal flow, the addition of waste liquid will cause the gasifier temperature to drop because the waste liquid needs to absorb heat and lower the temperature. However, the effect of high-temperature gas phase feed on the reaction temperature and temperature field inside the gasifier is much smaller than that of low-temperature liquid phase feed in the existing technology.

[0067] Based on the above findings, the present invention provides a process system and method for stably and reliably feeding wastewater into a gasifier. Through the structural design of the mixer, organic wastewater is introduced into the gasifier in the form of gas or tiny droplets, so that the organic wastewater has little impact on the temperature field and flow field inside the gasifier, and will not affect the process operability or product quality, and no modification to existing equipment is required.

[0068] The feeding system of the organic wastewater treatment device of the present invention provides a method for feeding organic wastewater into a gasifier. By controlling the flow rate of steam entering the mixer, the feeding temperature of the organic wastewater can be controlled, making it suitable for gasifiers with various processes and raw materials.

[0069] The feeding system of the organic wastewater treatment device provided by this invention has high operational flexibility. By adding a pump, shut-off valve one, and shut-off valve two to the pipeline of the system, the operation process is achieved by adding the pump, shut-off valve one, and shut-off valve two in conjunction with the buffer tank and mixer, so that there is no minimum flow limit for the organic wastewater feed rate in the gasifier, the adjustable range is wide, and the gasifier's operational stability is not affected by fluctuations in the organic wastewater feed rate. Attached Figure Description

[0070] Figure 1 This is a schematic diagram of the feeding system of the organic wastewater treatment device in Embodiment 2 of the present invention;

[0071] Figure 2 This is a structural diagram of the mixer in Embodiment 2 of the present invention;

[0072] Figure 3 This is a structural diagram of the swirling atomizing nozzle in Embodiment 2 of the present invention;

[0073] Figure 4 This is a BB view of the cyclone atomizer in Embodiment 2 of the present invention;

[0074] Figure 5 This is a side view of the cyclone atomizer in Embodiment 2 of the present invention;

[0075] Figure 6 This is a view AA of the eddy current mixer in Embodiment 2 of the present invention;

[0076] Figure 7 This is a diagram showing the temperature field changes inside the gasifier;

[0077] Among them, 1-buffer tank, 11-pressure regulating valve one, 12-pressure regulating valve two, 13-safety valve, 14-shut-off valve three;

[0078] 2-Mixer, 21-Swirl atomization section, 211-Cavity I, 212-Swirl atomization nozzle, 213-Organic wastewater inlet, 2121-Swirl atomizer, 2122-Atomization nozzle head;

[0079] 22-Throttle atomization section, 221-Cavity II, 222-Upper section, 223-Lower section;

[0080] 23-Vortex atomization section, 231-Cavity III, 232-Cross lever;

[0081] 3- Burner;

[0082] 4-Steam supply end;

[0083] 5-Pipeline, 51-Pipeline I, 52-Pipeline II, 53-Pipeline III, 54-Pipeline IV;

[0084] 6-Boost pump; 7-Flow regulating valve one; 8-Shut-off valve one; 9-Shut-off valve two; 10-Flow control valve two; 101-Shut-off valve four. Detailed Implementation

[0085] The present invention will be further described below with reference to specific embodiments, but this does not constitute any limitation on the present invention.

[0086] Example 1

[0087] The feeding system of the organic wastewater treatment device is a gasifier. The feeding system includes a mixer, a steam supply end, burners, and pipelines. The steam supply end stores steam. The mixer is placed vertically and consists of a swirl atomization section, a throttling atomization section, and a vortex atomization section from front to back, which are interconnected. The swirl atomization section is cavity I, which contains swirl atomizing nozzles and swirl atomizers. Cavity I has an organic wastewater inlet connected to the swirl atomizing nozzles. The throttling atomization section is cavity II, which includes an upper section with a narrower diameter and a lower section with a wider diameter. The vortex atomization section is cavity III, which contains a structure that generates vortex atomization.

[0088] Steam discharged from the steam supply end enters the swirl atomization section through pipeline I. Organic wastewater enters the swirl atomization nozzle through the organic wastewater inlet. After passing through the throttling atomization section and the vortex atomization section, the steam and organic wastewater are discharged from the vortex atomization section. The steam and organic wastewater discharged from the vortex atomization section enter the gasifier through the burner via pipeline II.

[0089] Steam enters cavity I through the top of cavity I, and organic wastewater enters the swirl atomizing nozzle through the organic wastewater inlet. After being atomized by the swirl atomizer for the first time, it is sprayed out from the swirl atomizer nozzle.

[0090] The organic wastewater sprayed from the swirl atomizing nozzle mixes with steam and enters chamber II. In chamber II, after the upper section narrows and throttles, a high-speed fluid is formed. The high-speed fluid enters the lower section and rapidly diffuses after throttling, forming a partial negative pressure zone. Strong turbulence is generated in this zone. The organic wastewater is further atomized in this section and further mixed with steam to form mist I. Mist I includes organic wastewater droplets and steam. Mist I is discharged from chamber II.

[0091] Aerosol I enters the vortex atomization section (cavity III), where organic wastewater droplets and steam undergo full heat and mass transfer. Part of the organic wastewater on the surface of the droplets is vaporized in this stage, further reducing the droplet diameter. The organic wastewater is further atomized in this section, and the organic wastewater and steam form aerosol II. Aerosol II is discharged from the bottom of cavity III and enters the gasifier through the burner.

[0092] Example 2

[0093] like Figure 2As shown, the feeding system of the organic wastewater treatment device is a gasifier. The feeding system includes a buffer tank 1, a mixer 2, a burner 3, a steam supply end 4, a pipeline 5, and a booster pump. The buffer tank 1 stores organic wastewater; the steam supply end 4 stores steam. The mixer 2 is placed vertically and includes, from front to back, a swirl atomizing section 21, a throttling atomizing section 22, and a vortex atomizing section 23. The swirl atomizing section 21, the throttling atomizing section 22, and the vortex atomizing section 23 are connected by flanges and are interconnected. The swirl atomizing section includes a cavity I211, inside which a swirl atomizing nozzle 212 is installed. The swirl atomizing nozzle 212 includes a swirl atomizer 2121 and an atomizing nozzle. The head 2122 and cavity I 211 are equipped with an organic wastewater inlet 213, which is connected to the swirl atomizing nozzle 212. The throttling atomizing section 22 is cavity II 221, which includes an upper section 222 and a lower section 223. The upper section 222 is a narrowed diameter section, and the lower section 223 is an expanded diameter section. The length of the lower section 223 is greater than the length of the upper section 222. The vortex atomizing section 23 includes cavity III 231, which contains several cross-shaped baffles 232 arranged sequentially from top to bottom. Each cross-shaped baffle 232 includes a junction point and four sides. The four sides are fixed to the inner wall of cavity III 231 and are of equal length. The junction point is on the same straight line in the vertical direction. In the bottom view of cavity III 231, the four sides of the cross-shaped baffles do not coincide. The buffer tank 1 is a sealed tank, which includes a buffer tank outlet and a buffer tank return port. Steam discharged from steam supply end 4 enters the swirl atomization section 21 through pipeline I51. The outlet of buffer tank 1 is connected to the organic wastewater inlet 213 through pipeline III53, which is equipped with a booster pump 6. After being discharged from buffer tank 1, the organic wastewater, under the action of the booster pump 6, enters the swirl atomization nozzle 212 through the organic wastewater inlet 213. The organic wastewater is atomized by the swirl atomizer 2121 within the swirl atomization nozzle 212 and then discharged from the swirl atomization nozzle 2122. The organic wastewater discharged from the swirl atomization nozzle 2122 mixes with steam and enters the throttling atomization section 22 and the vortex atomization section 23. Under the action of steam, the organic wastewater is further atomized or vaporized in the throttling atomization section 22 and the vortex atomization section 23. The atomized or vaporized organic wastewater and steam are then discharged from the vortex atomization section 23.

[0094] The steam and organic wastewater discharged from the vortex atomization section enter the gasifier through the burner via pipeline II52.

[0095] During operation, mixer 2 can atomize organic wastewater into droplets with a particle size of 50 μm or less. As the amount of steam added increases, the droplet diameter gradually decreases. When the amount of steam is sufficient, the droplets can be completely vaporized. The atomized feed has little impact on the flow field inside the gasifier and can form a low-temperature gas film area at the burner head, extending the burner's service life. Pure gas phase feed has the best effect.

[0096] Pipeline III53 is also equipped with flow regulating valve 7 and shut-off valve 8. Flow regulating valve 7 is located between booster pump 6 and mixer 2; shut-off valve 8 is located between flow regulating valve 7 and mixer 2. Buffer tank 1 is connected to booster pump 6 via pipeline IV54, which is equipped with shut-off valve 9. Buffer tank 1 includes pressure regulating valve 11 and pressure regulating valve 12. Buffer tank 1 also includes safety valve 13 and shut-off valve 14. Pipeline I51 is also equipped with flow control valve 10 and shut-off valve 101.

[0097] The feeding system of the organic wastewater treatment device in this embodiment includes the following steps during operation:

[0098] Step 1: Steam from the steam supply end enters the swirl atomization section, and organic wastewater enters the swirl atomization nozzle from the organic wastewater inlet. After the first atomization by the swirl atomization nozzle, it is sprayed out.

[0099] Step 2: The organic wastewater sprayed from the swirl atomizing nozzle and the steam enter the throttling atomization section together. In the throttling atomization section, the organic wastewater continues to atomize and mixes with the steam to form mist I. Mist I is discharged from the throttling atomization section.

[0100] Step 3: Aerosol I enters the vortex atomization section, where the organic wastewater in the aerosol continues to be atomized. The atomized organic wastewater and steam form aerosol II, which is discharged from the vortex atomization section and enters the gasifier through the burner.

[0101] Organic wastewater enters the gasifier through the integrated burner starter channel.

[0102] The maximum flow rate of organic wastewater addition is determined by the amount of coal fed into the gasifier. The mass ratio of the organic wastewater entering the gasifier to the mass of coal fed into the gasifier (dry basis) is less than or equal to 1:5. There is no minimum flow rate limit for organic wastewater addition. Even when the addition amount is 0, the organic wastewater addition system can be switched to self-circulation operation or shut down. Its operation can be independent of the gasifier system.

[0103] To ensure atomization effect, a minimum ratio is set between the amount of steam added and the amount of organic wastewater added; the amount of steam used per ton of organic wastewater is no less than 20m³. 3 And the steam consumption is not less than 100m³ 3 / h, used to protect the burner flow channel and burner head. That is, when the amount of organic wastewater is 1 ton, in order to protect the burner flow channel and burner head, the steam usage should not be less than 100m³ / h. 3 / h.

[0104] Steam is selected as the power source for atomization, and the temperature of the organic wastewater discharged from the vortex atomization section is controlled by adjusting the flow rate of steam flow regulating valve two. High-temperature feeding not only reduces the stress on the burner but also lowers the specific oxygen consumption of the unit.

[0105] In step one, the flow rate of the organic wastewater from the buffer tank is controlled by a flow regulating valve during the process of introducing the wastewater into the mixer.

[0106] The instantaneous flow rate of organic wastewater source fluctuates greatly and is unstable. Buffer tank storage can cope with the fluctuation of instantaneous flow rate of organic wastewater source. During the feeding process, the flow rate value of organic wastewater flow regulating valve one is set to the average flow rate of organic wastewater during long-term operation.

[0107] Organic wastewater in a buffer tank is pressurized by a wastewater booster pump to a pressure 0.5 MPa higher than that of the gasifier. The pressurized organic wastewater then enters the mixer via a flow regulating valve. The transport of organic wastewater mainly relies on the booster pump to pressurize the wastewater to a pressure 0.5 MPa higher than that of the gasifier, giving it sufficient power to overcome the resistance of the flow regulating valve and the mixer before entering the gasifier.

[0108] After the feeding system of the organic wastewater treatment device is started, first close the first shut-off valve and open the second shut-off valve. The booster pump controls the organic wastewater to flow back to the buffer tank. After the outlet pressure of the booster pump stabilizes, open the first shut-off valve and close the second shut-off valve. The booster pump then controls the organic wastewater to enter the mixer.

[0109] Before shutting down the feed system of the organic wastewater treatment unit, first close the shut-off valve one, then close the booster pump, so that the organic wastewater addition system operates independently of the gasifier system. This makes the wastewater suitable for start-up and shutdown conditions.

[0110] When the upstream wastewater flow rate is low and the liquid level in the organic wastewater buffer tank is also low, the wastewater from the outlet of the wastewater booster pump can be returned to the buffer tank by opening shut-off valve one and shut-off valve two, while closing flow regulating valve one to achieve stable operation of the device under the condition of adding organic wastewater at a small flow rate.

[0111] During the reaction, the pressure inside the buffer tank is controlled by adjusting pressure regulating valve one and pressure regulating valve two.

[0112] The flow of organic wastewater into the buffer tank is controlled by shut-off valve four.

[0113] Organic wastewater from upstream enters the buffer tank. The pressure inside the buffer tank is about 0.5 MPa and the temperature is normal. When the flow rate of organic wastewater from upstream is low or the liquid level in the organic wastewater buffer tank is high, the shut-off valve is closed to stop the organic wastewater from entering the buffer tank.

[0114] During use, the pressure inside the buffer tank is controlled by nitrogen. Low-pressure nitrogen enters the buffer tank through pressure regulating valve one. When the pressure inside the tank is too high, the gas inside the buffer tank is released to the VOCs (volatile organic compounds) treatment system or flare through pressure regulating valve two.

[0115] The safety of the buffer tank is ensured by the automatic pressure relief function of the safety valve.

[0116] Organic wastewater storage mainly relies on buffer tanks to cope with fluctuations in the upstream organic wastewater flow, while low-pressure nitrogen sealing reduces the volatilization of organic wastewater.

[0117] Example 3

[0118] The organic wastewater is sprayed into the gasifier for treatment using the feeding system of the organic wastewater treatment device in Example 2.

[0119] Comparative Example 1

[0120] Comparative Example 1 uses the gasifier feeding process in patent application CN113266836A to send organic wastewater into the gasifier for treatment.

[0121] In both Example 3 and Comparative Example 1, the dry basis coal feed rate was 62.5 t / h, and the organic wastewater was vinyl acetate, with an addition rate of 5 t / h. In Example 3, the gasification steam flow rate was 10 t / h, the pressure was 5.5 MPaG, and the temperature was 400℃. In Comparative Example 1, the organic wastewater was fed at ambient temperature (25℃). The gasifier reaction pressure was set to 4.0 MPaG. The temperature field inside the gasifier was simulated using CFD (Computational Fluid Dynamics) simulation technology (Fluent), and the carbon conversion rate inside the gasifier was calculated using process flow simulation software (ASPEN HYSYS). The results are shown in Table 1.

[0122] Table 1. Temperature and carbon conversion rate inside the gasifier

[0123] Process Flow No organic wastewater added Example 3 Comparative Example 1 Temperature inside the gasifier (°C) 1819 1752 1685 Carbon conversion rate within the gasification rate (%) 99.01 98.42 96.58

[0124] The results of the simulation of the temperature field inside the gasifier are as follows: Figure 2 As shown in the diagram. The shades of color in the graph represent different temperatures; darker colors indicate higher temperatures. From... Figure 2It can be seen that in Comparative Example 1, when organic wastewater is added to the gasifier using the existing technology, the high-temperature zone inside the gasifier is significantly reduced, while the low-temperature zone shifts downwards noticeably. In contrast, in Example 3, when organic wastewater is added to the gasifier using the system of Example 2, the impact on the temperature field inside the gasifier is relatively small. Furthermore, when organic wastewater is added to the gasifier using the system of the present invention, the carbon conversion rate in the organic wastewater can still be maintained at a high level.

[0125] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.

Claims

1. A feeding system for an organic wastewater treatment device, characterized in that, The device for treating organic wastewater is a gasifier. The feeding system includes: a mixer, a steam supply end, a burner, and pipelines; According to the flow direction of steam in the mixer, the mixer sequentially includes a swirl atomization section, a throttling atomization section and a vortex atomization section, and the swirl atomization section, the throttling atomization section and the vortex atomization section are connected to each other; The swirl atomization section is a cavity I, and a swirl atomization nozzle is provided inside the cavity I. An organic wastewater inlet is provided in the cavity I, and the organic wastewater inlet is connected to the swirl atomization nozzle. A swirl atomizer is provided inside the swirl atomization nozzle. The throttling atomizing section is cavity II, which includes an upper section and a lower section. The upper section is a narrowing section, and the lower section is an expanding section. The vortex atomizing section is cavity III, and cavity III has a structure for generating vortices; the structure for generating vortices consists of several cross-shaped baffles arranged sequentially from top to bottom inside cavity III, and the four sides of the several cross-shaped baffles do not overlap in the bottom view of cavity III. The steam discharged from the steam supply end enters the swirl atomization section through pipeline I. The organic wastewater enters the swirl atomization nozzle through the organic wastewater inlet. After the steam and the organic wastewater sprayed from the swirl atomization nozzle are mixed, they pass through the throttling atomization section and the vortex atomization section in sequence, and are discharged from the vortex atomization section. The steam discharged from the vortex atomization section and the organic wastewater enter the gasifier through the burner through pipeline II.

2. The feeding system of the organic wastewater treatment device according to claim 1, characterized in that, The cross-shaped stop bar includes an intersection point and four sides. The four sides are located in cavity III, and the side lengths of the four sides are equal. The intersection point is on the same straight line in the vertical direction.

3. The feeding system of the organic wastewater treatment device according to claim 1 or 2, characterized in that, The feeding system also includes a buffer tank that stores organic wastewater. The buffer tank includes a buffer tank outlet and a buffer tank return port. The buffer tank outlet is connected to the organic wastewater inlet via pipeline III.

4. The feeding system of the organic wastewater treatment device according to claim 3, characterized in that, The feeding system also includes a booster pump, which is located in pipeline III between the buffer tank and the mixer.

5. The feeding system of the organic wastewater treatment device according to claim 4, characterized in that, Pipeline III is also provided with a flow regulating valve and a shut-off valve. The flow regulating valve is located between the booster pump and the mixer. The shut-off valve is located between the flow regulating valve and the mixer. And / or, the buffer tank return port and the booster pump are connected through pipeline IV, and pipeline IV is provided with a shut-off valve.

6. The feeding system of the organic wastewater treatment device according to claim 5, characterized in that, The buffer tank includes a pressure regulating valve one and a pressure regulating valve two; and / or, the buffer tank further includes a safety valve and a shut-off valve three.

7. The feeding system of the organic wastewater treatment device according to claim 6, characterized in that, Pipeline I is equipped with flow regulating valve II and shut-off valve IV.

8. A feeding process for an organic wastewater treatment device, characterized in that, The feeding system of the organic wastewater treatment apparatus according to any one of claims 1-7 includes the following steps: Step 1: Steam from the steam supply end enters the swirl atomization section, and organic wastewater enters the swirl atomization nozzle through the organic wastewater inlet. The organic wastewater is then atomized by the swirl atomization nozzle and sprayed out. Step 2: The organic wastewater sprayed from the swirl atomizing nozzle and the steam enter the throttling atomization section together. In the throttling atomization section, the organic wastewater continues to atomize and mixes with the steam to form mist I. Mist I is discharged from the throttling atomization section. Step 3: Aerosol I enters the vortex atomization section, where the organic wastewater continues to be atomized. The atomized organic wastewater and steam form aerosol II. After being discharged from the vortex atomization section, aerosol II enters the gasifier through the burner.

9. The feeding process of the organic wastewater treatment device according to claim 8, characterized in that, In step one, the organic wastewater is collected by the buffer tank and then discharged from the buffer tank outlet; the organic wastewater discharged from the buffer tank outlet enters the swirl atomization section under the action of the booster pump; and / or, the flow rate of the organic wastewater discharged from the buffer tank outlet is controlled by the flow regulating valve during the process of entering the swirl atomization section.

10. The feeding process of the organic wastewater treatment device according to claim 9, characterized in that, The flow rate of organic wastewater discharged from the buffer tank outlet is 0-35t / h, and the ratio of the mass of organic wastewater entering the gasifier to the dry basis mass of coal fed into the gasifier is less than or equal to 1:

5.

11. The feeding process of the organic wastewater treatment device according to claim 9 or 10, characterized in that, The amount of steam used per ton of organic wastewater shall not be less than 20m³. 3 .

12. The feeding process of the organic wastewater treatment device according to claim 11, characterized in that, The steam flow rate is greater than or equal to 100 m³ / h. 3 / h.

13. The feeding process of the organic wastewater treatment device according to claim 12, characterized in that, After the feeding system is started, first close the shut-off valve one and open the shut-off valve two. The booster pump controls the organic wastewater to flow back to the buffer tank. After the outlet pressure of the booster pump stabilizes, open the shut-off valve one and close the shut-off valve two. The booster pump controls the organic wastewater to enter the cyclone atomization section. And / or, before shutting down the feeding system, first close the shut-off valve one and then shut down the booster pump.

14. The feeding process of the organic wastewater treatment device according to claim 13, characterized in that, During the reaction, the pressure inside the buffer tank is controlled by pressure regulating valve one and pressure regulating valve two; and / or, organic wastewater is controlled to flow into the buffer tank by shut-off valve three; and / or, the safety of the buffer tank is ensured by the automatic pressure relief function of the safety valve; and / or, the flow rate of steam entering the mixer is controlled by adjusting flow regulating valve two; and / or, steam is controlled to enter the vortex atomization section by shut-off valve four.

15. The application of a feeding system for an organic wastewater treatment device according to any one of claims 1-7 or a feeding process for an organic wastewater treatment device according to any one of claims 8-14 in the treatment of organic wastewater, wherein the organic wastewater is organic wastewater generated by a coal chemical plant or organic wastewater generated by a petrochemical plant.

16. The application according to claim 15, characterized in that, The organic wastewater is one of the organic wastewater generated by the MTO unit, the organic wastewater generated by the PDH unit, and the organic wastewater generated by the EVA unit.

Images