Oily sludge reduction treatment device and method

Abstract

The invention provides an oily sludge reduction treatment device and method, and relates to the technical field of oily sludge treatment.The device comprises a shell, a first cavity is formed in the shell, and a feeding port and a discharging port which communicate with the first cavity are formed in the two ends of the shell correspondingly; a capillary pore channel communicated with the first cavity is formed in the side wall of the first cavity, and a heating part is arranged in the side wall of the first cavity; the stirring and conveying mechanism is arranged in the shell and used for stirring and conveying the materials in the first cavity. The device is used for solving the problems of high solid-liquid separation difficulty, high cost and large occupied area in the reduction treatment process of the oily sludge in the prior art.

Description

Technical Field

[0001] The present invention belongs to the technical field of oily sludge treatment, and more specifically, relates to an oily sludge reduction treatment device and method. Background Art

[0002] Oily sludge is widely found in petroleum and petrochemical enterprises. It is a solid waste rich in petroleum components formed in oil refining, chemical processes and sewage treatment units. Oily sludge is black and viscous, and is emulsified from petroleum, crude oil, oil products, mud, sand and water. At present, oily sludge has been included in the "National List of Hazardous Wastes". It contains a variety of toxic and harmful substances, which will have a serious impact on the natural environment. Therefore, the treatment of oily sludge is a necessary requirement for environmental protection of petroleum and petrochemical enterprises. However, with the expansion of the scale of petroleum and petrochemical enterprises and the improvement of production capacity, the content of oily sludge in the plant area is also increasing. Due to the complex composition of oily sludge and the large amount of oily sludge produced, the production and operation costs of petroleum and petrochemical enterprises have been greatly increased.

[0003] For oily sludge, the plant usually needs to spend a lot of money to outsource the treatment. Oily sludge reduction treatment is an important means to reduce the treatment cost of oily sludge and reduce the cost of outsourcing hazardous waste disposal. Oily sludge contains a lot of oil resources, and the recovery of oil resources is also an important means to achieve efficient resource utilization and improve the economic efficiency of oily sludge treatment.

[0004] At present, the oily sludge reduction treatment device separates water and oil from the oily sludge through processes such as demulsification and heating, but solid and liquid separation is still required. For the solid-liquid separation in the oily sludge reduction treatment process, high-speed centrifugal equipment is mostly used to recover liquid resources. High-speed centrifugal treatment requires the reduction device to be equipped with additional centrifugal tanks and centrifugal pumps, which increases the construction cost and the floor space of the device. Moreover, as the amount of oily sludge treated increases, high-speed centrifugal treatment will also cause the cost of oily sludge treatment to increase further. In addition, for oily sludge with high water and oil content, water and oil need to be discharged frequently, and the operating efficiency of the device needs to be improved.

[0005] CN114632789B discloses an integrated separation device for oil sludge mixture for oil fields. It includes an excavation and feeding mechanism, a coarse crushing component, a series crushing component, a conveyor belt and a centrifugal separation component. The device performs solid-liquid separation and volume reduction treatment on the sludge, but requires the use of high-speed centrifugation to complete the solid-liquid separation process, and the overall operating cost of the device is relatively high.

[0006] CN115463462A discloses a centrifugal adjustable sewage oil purification device and a method of use. The system includes an oil purifier and a centrifugal bucket. The system also relies on centrifugal action to achieve solid-liquid separation, and its solid-liquid separation energy consumption is relatively high and needs to be further reduced.

[0007] CN114933400B discloses a device for harmless treatment of oil sludge. It includes an oil sludge inlet, a drum impurity remover, two stirring reactors, a horizontal centrifuge, a dryer, and two disc centrifuges. The device reduces the amount of oil sludge, but requires the use of a horizontal centrifuge and two disc centrifuges to achieve solid-liquid separation by centrifugation. The device has high construction costs, occupies a large area, and has high energy consumption for solid-liquid separation, resulting in high operating costs.

[0008] CN111908743B discloses a system and method for separating and recovering oil sludge by hydrothermal treatment. The system includes a hydrothermal reactor, a flash condenser and an oil-water separator. The system requires high temperature (100-250°C) and high pressure (0.2-4MPa) for the oil sludge, and the system operation cost is high. In addition, the equipment is difficult to operate continuously and can only process the oil sludge intermittently. After the treatment is completed, the hydrothermal reactor is cooled and depressurized and then connected to the flash condenser pipe to discharge the oil sludge. The operation is complicated, and the hydrothermal process is limited to the treatment of low-water content oil sludge, and there is a risk of reactor explosion.

[0009] Therefore, this field urgently needs to optimize the current devices and methods, further enhance the separation and recovery of water and oil in oily sludge, especially the recovery of oil resources, simplify the equipment and reduce the operating cost of the equipment, and further reduce the treatment cost of oily sludge. Summary of the invention

[0010] The purpose of the present invention is to provide an oily sludge reduction treatment device and method to address the deficiencies in the prior art, thereby solving the problems of difficulty in solid-liquid separation, complex operation, high cost and large floor space required in the oily sludge reduction treatment process in the prior art.

[0011] In order to achieve the above object, the present invention provides an oily sludge reduction treatment device, comprising:

[0012] A shell, wherein a first chamber is disposed inside the shell, a feed port and a discharge port communicating with the first chamber are disposed at two ends of the shell, a capillary channel communicating with the first chamber is opened on the side wall of the first chamber, and a heating component is disposed in the side wall of the first chamber;

[0013] A stirring and conveying mechanism is arranged inside the shell and is used to stir and convey the material in the first chamber.

[0014] Optionally, a liquid collecting tank connected to the capillary pores is disposed on the outer side of the outer wall of the shell; at least one drainage port is disposed at the bottom of the liquid collecting tank, which can achieve rapid drainage, maintain sufficient space in the liquid collecting tank, and promote the absorption of oil and water in the first chamber by the capillary pores. In addition, the drainage port can also serve as a backwash port. When the device is shut down for maintenance, air or water is backwashed into the liquid collecting tank through the drainage port, and the capillary pores are backwashed by air or water for a period of time, thereby avoiding blockage of the capillary pores and increasing the service life of the device.

[0015] When the device of the present invention is manufactured, the parameters of the capillary channel can be adjusted, including but not limited to the pore size and volume ratio (ie, the opening ratio).

[0016] According to a preferred embodiment of the present invention, the pore size of the capillary channel is 1-5 microns.

[0017] According to a preferred embodiment of the present invention, the volume of the capillary channel accounts for 0.2-6%, preferably 2-4%, relative to the total volume of the side wall of the first chamber.

[0018] The preferred pore size combined with the preferred volume ratio can achieve a better oil-water separation effect.

[0019] Optionally, the heating component is an electric heating rod, and the temperature in the first chamber can be adjusted by the heating power of the electric heating rod. The temperature in the first chamber is 30-100°C, preferably 60-90°C.

[0020] According to a preferred embodiment of the present invention, a heat-conducting layer is provided on the inner wall of the shell, and the electric heating rod is inserted into the heat-conducting layer. The heat-conducting layer can improve thermal conductivity and heating efficiency.

[0021] Optionally, the stirring and conveying mechanism includes a rotating shaft, the rotating shaft is rotatably arranged in the first chamber, one end of the rotating shaft is connected to a driving motor, and the outer periphery of the rotating shaft is provided with stirring and conveying blades. The rotating shaft of the present invention can be arranged in one or more groups. According to a specific embodiment, the rotating shaft is arranged in two parallel groups to achieve better stirring and conveying effects.

[0022] Optionally, an air intake structure is further included, wherein an output end of the air intake structure is communicated with the first chamber and is used to transport acidic gas into the first chamber.

[0023] Optionally, the air intake structure includes an air intake box, the air intake port of the air intake box is used to communicate with the waste smoke pipeline of the factory area, and the multiple air distribution ports of the air intake box are connected to the first chamber.

[0024] Optionally, the liquid collecting tank is connected to a negative pressure generating structure, and the negative pressure generating structure is used to form a negative pressure environment in the liquid collecting tank.

[0025] Optionally, a second chamber connected to the first chamber is provided inside the shell, the second chamber is provided at one end of the first chamber close to the discharge port, and the second chamber tapers from one end away from the discharge port to one end close to the discharge port, a side wall of the second chamber is provided with an annular recovery groove with an open inner circumference, a liquid outlet is provided at the bottom of the recovery groove, and a filter plate is provided at the open end of the recovery groove.

[0026] Optionally, a squeezing mechanism is provided in the second chamber, and the squeezing mechanism includes a scraper rod rotatably provided in the second chamber, the scraper rod rotates around the cross-sectional center of the second chamber within the cross-section of the second chamber, and a scraper plate is provided at the outer end of the scraper rod, and the scraper plate is in contact with the filter plate.

[0027] The present invention also provides a method for reducing the amount of oily sludge, using the above-mentioned device for reducing the amount of oily sludge, the method comprises:

[0028] Feeding the oily sludge and the optional demulsifier into the first chamber from the feed inlet;

[0029] Heating, stirring and conveying the material in the first chamber;

[0030] discharging at least part of the liquid generated in the first chamber through the capillary channel;

[0031] The solid produced in the first chamber is discharged through the discharge port.

[0032] Optionally, the method further includes backwashing the capillary channels.

[0033] Optionally, when a liquid collecting trough connected to the capillary pores is provided on the outer side of the outer wall of the shell, and a liquid discharge port is provided on the liquid collecting trough, the capillary pores are backwashed with gas or liquid through the liquid discharge port.

[0034] Optionally, the oily sludge reduction treatment device backwashes the capillary channels once every 500-2000 hours of operation.

[0035] In the present invention, the capillary channels can be formed by any method. According to one specific embodiment, the capillary channels are formed by stamping; according to another specific embodiment, the capillary channels are capillary holes with protective sleeves embedded during the equipment processing and forming, which can connect the oily sludge end and the liquid collecting tank end; according to another embodiment, the side wall of the first chamber with the capillary channels is integrally formed using a channel model, for example, it is integrally formed using a channel model during steel rolling; according to another embodiment, the side wall of the first chamber with the capillary channels is made by jet etching, and the device is easy to produce.

[0036] Optionally, the moisture content of the oily sludge is in the range of 10%-80%, preferably in the range of 10%-40%.

[0037] In the present invention, an additional demulsifier can be added to strengthen the demulsification process of the oily sludge, and the demulsifier is selected from at least one of sodium lignin sulfonate, ethylenediamine, propylene glycol, glycerol, nonylphenol polyoxyethylene ether, sodium dodecylbenzene sulfonate, and hexadecyltrimethylammonium bromide.

[0038] The dosage of the demulsifier can be determined as required. Optionally, the amount of the demulsifier added relative to the oily sludge is 0.5-10 g / L, preferably 1-8 g / L, and most preferably 5 g / L.

[0039] In the present invention, it is not necessary to add a demulsifier.

[0040] Without adding demulsifier, the temperature in the first chamber can be increased, and / or the treatment time, that is, the residence time of the oily sludge, can be increased; at this time, the residence time of the oily sludge in the first chamber is 6-24h, preferably 12-16h.

[0041] In the present invention, the power of the heating component is adjustable, and the oily sludge is heated from all sides through the heat-conducting layer. Optionally, the temperature in the first chamber is 30-100°C, preferably 60-90°C. Specifically, 85°C is most preferred when there is no demulsifier, and 75°C is most preferred when a demulsifier is added.

[0042] In the present invention, the solid material discharged from the discharge port can be further subjected to deep treatment, and the deep treatment process can be landfill, tillage, composting, incineration, wet oxidation, etc.

[0043] Optionally, the method further includes inputting acid gas into the first chamber to mix the acid gas with the oily sludge.

[0044] Optionally, the acid gas is an acid gas containing SO2 and CO2, wherein the content of SO2 is in the range of 100 to 3000 ppm, and the content of CO2 is in the range of 2% to 40%.

[0045] Optionally, the acidic gas is waste flue gas from a factory, and the temperature of the waste flue gas from the factory is 120-350°C, preferably 200-350°C. Preferably, the waste flue gas from the factory is dust-removed before use. While the waste flue gas can provide heat for the oily sludge, the acidic gases SO2 and CO2 therein can further fine-tune the oily sludge, adjust the pH of the oily sludge to decrease, enhance the demulsification effect, and purify the waste flue gas from the factory to a certain extent.

[0046] Optionally, the volume ratio of the factory waste flue gas input into the first chamber to the oily sludge is 50:1-400:1, preferably 100:1-150:1, and most preferably 120:1.

[0047] According to the present invention, the residence time of the oily sludge in the device can be controlled by the stirring and conveying mechanism. Optionally, when a demulsifier is added, the residence time of the oily sludge in the first chamber is 0.5-8h, preferably 1-3h.

[0048] Optionally, the method further comprises providing a negative pressure environment at one end of the capillary channel away from the first chamber.

[0049] Optionally, when a liquid collecting tank connected to the capillary pores is provided on the outer side of the outer wall of the shell, and a negative pressure tube is provided on the liquid collecting tank, the gas in the liquid collecting tank is extracted and injected into the shell to maintain a slight negative pressure in the liquid collecting tank, specifically, to make the pressure in the liquid collecting tank 0.085-0.095MPa, and the extracted gas is circulated to the air inlet, and the small amount of air circulated to the air inlet and the waste flue gas from the factory area maintain a slight positive pressure at the demulsification point of the oil-containing sludge in the reduction device. Specifically, the pressure in the shell is 0.103-0.125MPa, and the oil and water after demulsification are lifted through the capillary pores by the pressure difference on both sides of the capillary pores to enter the liquid collecting tank through the capillary pores.

[0050] Optionally, when a second chamber connected to the first chamber is provided inside the shell, the second chamber is provided at one end of the first chamber close to the discharge port, and the second chamber tapers from the end away from the discharge port to the end close to the discharge port, the side wall of the second chamber is provided with an annular recovery groove with an open inner circumference, the bottom of the recovery groove is provided with a liquid outlet, and the open end of the recovery groove is provided with a filter plate, it also includes: utilizing the side wall of the second chamber to extrude the material in the second chamber, and performing solid-liquid separation of the material through the filter plate.

[0051] Optionally, when an extrusion mechanism is provided in the second chamber, the extrusion mechanism includes a scraper rod rotatably provided in the second chamber, the scraper rod rotates around the cross-sectional center of the second chamber within the cross-sectional area of ​​the second chamber, and a scraper plate is provided at the outer end of the scraper rod. When the scraper plate contacts the filter plate, it also includes: the material in the second chamber is squeezed between the scraper plate and the filter plate through the extrusion mechanism.

[0052] According to a specific embodiment of the present invention, the method for reducing the amount of oily sludge comprises the following steps:

[0053] S1: Adding oily sludge

[0054] The oily sludge is introduced into the first chamber through the feed port, and a demulsifier can be appropriately added to enhance the demulsification effect of the oily sludge;

[0055] S2: Demulsification of oily sludge

[0056] The oily sludge is demulsified in the first chamber, and the solid-liquid mixture is continuously turned in the first chamber by stirring;

[0057] S3: Discharge of oily sludge

[0058] The demulsified oily sludge is discharged through the discharge port and transported to further deep treatment process;

[0059] S4: Capillary recovery

[0060] After demulsification, the liquid in the first chamber is composed of water and oil, which flows into the liquid collecting tank through the capillary channels on the side wall of the first chamber and is recycled through the drain port.

[0061] According to another specific embodiment of the present invention, a method for reducing the amount of oily sludge using waste flue gas from a plant area comprises the following steps:

[0062] S1: Raw material batching and feeding

[0063] The oily sludge to be treated is mixed with a demulsifier for conditioning, and introduced into the oily sludge reduction treatment device through a pump connected to the feed port, and a proper amount of purified waste flue gas in the plant is introduced into the oily sludge reduction treatment device through the air inlet through a fan;

[0064] S2: Oily sludge reduction

[0065] The oily sludge equipped with demulsifier is heated and heated by the heating component and the heat-conducting layer in the oily sludge reduction treatment device, and is stirred and homogenized by the stirring and conveying mechanism. The waste flue gas heats the oily sludge in the oily sludge reduction treatment device through the gas distribution port. The oily sludge stays in the oily sludge reduction treatment device for a certain period of time to complete the separation of water and oil.

[0066] S3: Separation and recovery

[0067] After demulsification, heating dehydration and deoiling, water and oil are sucked into the liquid collection tank through capillary channels at the bottom of the oily sludge reduction treatment device;

[0068] S4: Material discharge

[0069] The demulsified and heated oily sludge is transported to the discharge port and discharged from the oily sludge reduction treatment device under the stirring and pushing of the stirring and conveying mechanism. A small amount of waste gas generated under high temperature returns to the flue gas treatment unit in the plant area through the gas outlet together with the waste flue gas introduced into the device. Through the above method, the waste flue gas in the plant area introduced into the oily sludge reduction treatment device is purified to a certain extent, and the desulfurization efficiency can reach 5-60%. In addition, a high proportion of waste flue gas will carry a small amount of waste gas generated by the high-temperature demulsification of the oily sludge into the plant area flue gas purification unit, avoiding the generation of waste gas from the oily sludge reduction treatment device.

[0070] Oily sludge is an emulsion system composed of water and oil. Although water and oil are two immiscible liquids, there is a water-in-oil or oil-in-water form in the emulsion system, so that one of the liquids is dispersed in the other liquid in the form of small droplets; due to the existence of the emulsion system, the oily sludge exhibits a large viscosity and poor sedimentation performance. The oil and water system is mixed with suspended particles, which are mostly negatively charged and repel each other and are difficult to aggregate and precipitate; this stable emulsion system of oily sludge results in low efficiency in its reduction treatment, and it is difficult to separate water, oil and suspended particles. To this end, the oily sludge reduction treatment device provided by the present invention can pass the factory waste flue gas into the shell 1, that is, the factory waste flue gas without dust removal can be used, and some particulate matter in the flue gas can be removed by oily sludge, thereby reducing the pressure on the factory dust removal equipment and process, and even the dust removal standard can be achieved by circulating the oily sludge into the oily sludge, thereby eliminating the factory dust removal process unit, and the factory waste flue gas after dust removal can be used to reduce the oily sludge treatment load; the factory waste flue gas contains a large amount of CO2 (2-40%), SO2 (100-3000ppm), NO x (including NO and NO2, 150-2000ppm) and a small amount of SO3 (0-150ppm), and has a relatively high temperature (120-350℃); after the factory waste gas is input into the shell 1 and contacts with the oily sludge for reaction, 1) the temperature of the oily sludge is increased through heat exchange, which accelerates the movement rate of water and oil in the oily sludge, which is conducive to breaking the water-in-oil or oil-in-water emulsion system; 2) CO2, SO2, NO x , SO3 and other acidic gases react with oily sludge, reducing the pH of oily sludge, which is beneficial to the demulsification process of oily sludge, reducing the stability of the emulsification system, and reducing the viscosity of oily sludge; 3) Acidic gases react with oily sludge and are absorbed, providing more positive ions, weakening or breaking the negative charge effect of suspended particles, accelerating the aggregation and deposition of suspended particles and breaking the emulsification system; 4) Acidic gases are absorbed to form HCO3 2- 、SO3 2- 、SO4 2- 、NO3 2- 、NO 2-Plasma combines with metal ions in the solid phase of the oily sludge (such as Ca, Mg, Cu, etc., which originally exist in the form of insoluble oxides, such as CaO, MgO, CuO, or in the form of hydroxides, such as Ca(OH)2, Mg(OH)2), dissolves some metal ions, breaks the stability of the solid phase, reduces viscosity, reduces the difficulty of solid-liquid phase separation, and improves the efficiency and effect of stirring the oily sludge in the first chamber; the above four reasons complete the tempering process of the oily sludge, and the demulsification and treatment effect of the oily sludge is significantly improved through the waste flue gas of the resource-based plant.

[0071] This method has the following technical advantages: (1) It utilizes the waste heat resources of the factory's waste flue gas to synergistically purify the SO2 in the waste flue gas, and utilizes SO2 and CO2 to condition the oily sludge. The waste flue gas also carries the waste gas generated by heating and demulsifying the oily sludge into the factory's flue gas treatment unit, thereby improving the environmental benefits of the oily sludge reduction treatment device and the demulsification effect of the oily sludge.

[0072] (2) By sucking through the negative pressure pipe and blowing the waste flue gas into the oily sludge reduction treatment device, a pressure difference is established, the oil-water recovery efficiency after demulsification is improved, the treatment efficiency of the oily sludge reduction treatment device and the oil-water separation and recovery efficiency are improved, and the economic benefits of the device are improved.

[0073] (3) The device uses capillary self-priming to separate and recover oil and water substances, avoiding the centrifugal equipment of traditional equipment methods, reducing the construction cost and operating cost of the oily sludge reduction treatment device while realizing oil resource recovery and improving economic benefits.

[0074] According to another specific embodiment of the present invention, a method for reducing the amount of oily sludge using waste flue gas from a plant area comprises the following steps:

[0075] S1: Feed

[0076] The oily sludge to be treated is added into the first chamber through the feed port, and the feed port can be used to add a demulsifier to enhance the demulsification effect of the oily sludge in the oily sludge reduction treatment device;

[0077] S2: Demulsification

[0078] The oily sludge in the demulsification bin is continuously stirred and transported by the stirring and conveying mechanism, which strengthens the demulsification process. The temperature of the oily sludge is increased by the heating of the heating component, which strengthens the demulsification effect.

[0079] S3: Separation and recovery

[0080] The demulsified oily sludge is transported to the second chamber driven by the stirring and conveying mechanism. The chamber wall of the second chamber is provided with a recovery tank and a matching extrusion mechanism. The oil and water resources in the oily sludge are recovered through extrusion separation by the extrusion mechanism and the recovery tank, so as to realize solid-liquid separation and achieve the purpose of reducing the amount of oily sludge.

[0081] S4: Discharging

[0082] The oily sludge that stays in the first chamber and the second chamber for a certain period of time is discharged from the discharge port after solid-liquid separation to complete the reduction operation. The waste gas generated during the demulsification process is discharged from the gas outlet and transported to the gas purification unit for purification and discharge.

[0083] The method has the following technical advantages: (1) solid-liquid separation is achieved by squeezing the squeezing mechanism, thus avoiding the high energy consumption caused by using high-speed centrifugal equipment for solid-liquid separation and reducing the operating cost of the oily sludge reduction treatment device;

[0084] (2) The second chamber of the device is equipped with a recovery tank and a filter plate, which has a higher solid-liquid separation efficiency than the traditional extrusion separation method;

[0085] (3) The device is equipped with a scraper. The use of a soft scraper can improve the scraping effect and protect the recovery tank, thereby extending the operating life of the oily sludge reduction treatment device.

[0086] The invention provides an oily sludge reduction treatment device and method, and the beneficial effects are as follows: the oily sludge reduction treatment device is provided with a first chamber in a shell, a stirring and conveying mechanism is provided in the first chamber, the oily sludge and the demulsifier can be input into the first chamber through a feed port, under the stirring and conveying action of the stirring and conveying mechanism, the materials are fully contacted, and at the same time, a heating component heats the first chamber to provide a suitable treatment temperature, the demulsifier can break the emulsification system of the oily sludge and reduce the viscosity of the oily sludge, and the water and oil in the oily sludge after sufficient demulsification are absorbed and discharged in a liquid form through capillary channels for collection, and at the same time, the treated solid material can be discharged through a discharge port for further deep treatment; in a preferred embodiment, the acidic gas is input into the first chamber through the air intake structure, the acidic gas can react with the oily sludge, reduce the pH value of the oily sludge, facilitate the demulsification process of the oily sludge, and reduce the stability of the emulsification system, and in addition, the acidic gas can also provide heat for the first chamber to realize the recovery and utilization of heat energy. In another preferred embodiment, a second chamber connected to the first chamber is arranged inside the shell, the second chamber is tapered from one end away from the discharge port to the end close to the discharge port, the side wall of the second chamber is provided with a circular recovery groove with an open inner circumference, the bottom of the recovery groove is provided with a liquid outlet, and the open end of the recovery groove is provided with a filter plate; an extrusion mechanism is arranged in the second chamber, the extrusion mechanism includes a scraper rod rotatably arranged in the second chamber, the scraper rod rotates around the cross-sectional center of the second chamber in the cross-sectional area of ​​the second chamber, and a scraper plate is arranged at the outer end of the scraper rod, and the scraper plate contacts the filter plate; the scraping action of the scraper plate of the extrusion mechanism can further squeeze the material between the scraper plate and the filter plate, promote solid-liquid separation, and improve separation efficiency and separation effect. The oily sludge reduction treatment device has a simple and compact structure, a small footprint, and adopts a new solid-liquid separation method to achieve solid-liquid separation in the process of oily sludge reduction treatment. Compared with the solid-liquid separation method using high-speed centrifugation in the prior art, it not only reduces the separation difficulty and improves the separation efficiency, but also saves costs.

[0087] The present invention aims to solve the problem that the current oily sludge reduction treatment device and method are complex and have high operating costs, and proposes an oily sludge reduction treatment device and method. The solid-liquid separation process of oily sludge reduction is optimized, the traditional high-energy centrifugal method of separating oily sludge and oil-water mixture is avoided, and oil resources are recycled, which improves the economic efficiency of the oily sludge reduction treatment device and reduces the cost of oily sludge treatment. In one embodiment, waste flue gas in the plant area of ​​petroleum and petrochemical enterprises is also recycled, the oil recovery capacity and efficiency in the oily sludge reduction treatment device are enhanced, and the waste gas pollution generated by the oily sludge reduction treatment device is synergistically treated.

[0088] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0089] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention in conjunction with the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0090] Figure 1 A schematic structural diagram of an oily sludge reduction treatment device according to Example 1 of the present invention is shown.

[0091] Figure 2 A schematic cross-sectional structure diagram of a first chamber of an oily sludge reduction treatment device according to Example 1 of the present invention is shown.

[0092] Figure 3 A schematic structural diagram of an oily sludge reduction treatment device according to Example 2 of the present invention is shown.

[0093] Figure 4 A schematic structural diagram of an oily sludge reduction treatment device according to Example 3 of the present invention is shown.

[0094] Figure 5 A schematic cross-sectional structure diagram of a second chamber of an oily sludge reduction treatment device according to Example 3 of the present invention is shown.

[0095] Figure 6 A schematic diagram of the side wall structure of the second chamber of an oily sludge reduction treatment device according to Example 3 of the present invention is shown.

[0096] Figure 7 A schematic structural diagram of an oily sludge reduction treatment device according to Example 4 of the present invention is shown.

[0097] Figure 8 A flow chart of a method for reducing the amount of oily sludge according to Example 5 of the present invention is shown.

[0098] Fig. 9 A flow chart of a method for reducing the amount of oily sludge according to Example 6 of the present invention is shown.

[0099] Fig.10 A flow chart of a method for reducing the amount of oily sludge according to Example 7 of the present invention is shown.

[0100] Fig.11 A flow chart of a method for reducing the amount of oily sludge according to Example 8 of the present invention is shown.

[0101] Description of reference numerals:

[0102] 1. Shell; 2. First chamber; 3. Feed inlet; 4. Discharge outlet; 5. Capillary channel; 6. Heating component; 7. Heat-conducting layer; 8. Liquid collecting tank; 9. Liquid discharge outlet; 10. Rotating shaft; 11. Driving motor; 12. Stirring and conveying blades; 13. Air inlet box; 14. Air inlet; 15. Air distribution port; 16. Air outlet; 17. Negative pressure pipe; 18. Second chamber; 19. Recovery tank; 20. Liquid outlet; 21. Filter plate; 22. Filter hole; 23. Scraper rod; 24. Scraper plate; 25. Sealing component. DETAILED DESCRIPTION

[0103] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. On the contrary, these embodiments are provided to make the present invention more thorough and complete, and to fully convey the scope of the present invention to those skilled in the art.

[0104] Example 1

[0105] like Figure 1 and Figure 2 As shown, this embodiment provides an oily sludge reduction treatment device, comprising:

[0106] A shell 1, wherein a first chamber 2 is disposed inside the shell 1, a feed port 3 and a discharge port 4 communicating with the first chamber 2 are disposed at both ends of the shell 1, a plurality of capillary channels 5 communicating with the first chamber 2 are formed on the side wall of the first chamber 2 by stamping, and a heating component 6 is disposed inside the side wall of the first chamber 2;

[0107] The stirring and conveying mechanism is arranged inside the shell 1 and is used to stir and convey the material in the first chamber 2 .

[0108] A liquid collecting tank 8 connected to the capillary channel 5 is provided on the outside of the outer wall of the shell 1. The liquid collecting tank 8 is connected to the outer wall of the shell 1 to form a liquid collecting space on the outside of the outer wall of the shell 1. The liquid separated from the oily sludge reduction treatment device can be discharged from the first chamber 2 through the capillary channel 5 to the liquid collecting tank 8.

[0109] A plurality of drain ports 9 are provided at the bottom of the liquid collecting tank 8, which can realize rapid drainage, maintain sufficient space in the liquid collecting tank 8, promote the absorption of oil and water by the capillary pores 5, and the drain ports 9 can serve as backwash ports. When the device is shut down for maintenance, air or backwash water is backwashed into the liquid collecting tank 8 through the drain ports 9 and maintained for a period of time. The capillary pores 5 are backwashed by air or backwash water to avoid blockage of the capillary pores 5 and improve the service life of the equipment.

[0110] The heating component 6 is an electric heating rod, and the temperature in the first chamber 2 can be adjusted by the heating power of the electric heating rod.

[0111] In this embodiment, if Figure 2 As shown, a heat-conducting layer 7 is provided on the inner wall of the shell 1, and the electric heating rod is inserted into the heat-conducting layer 7. The heat-conducting layer 7 can improve the thermal conductivity and the heating efficiency. In the present embodiment, the heat-conducting layer 7 is heat-conducting oil, so the shell 1 includes an inner shell and an outer shell, and an interlayer is formed between the inner shell and the outer shell, and the heat-conducting oil is filled in the interlayer. At this time, the capillary pores 5 and the de-oiling capillary pores 7 are opened on the inner shell, and the outer shell is provided with through holes at corresponding positions and the periphery of the through holes is connected to the inner shell through a cylinder, so that the liquid discharged through the capillary pores 5 can flow out.

[0112] The stirring and conveying mechanism comprises a rotating shaft 10 , which is rotatably disposed in the first chamber 2 , one end of the rotating shaft 10 is connected to a driving motor 11 , and a stirring and conveying blade 12 is disposed on the outer periphery of the rotating shaft 10 .

[0113] The stirring and conveying mechanism drives the rotating shaft 10 to drive the stirring and conveying blades 12 to rotate through the driving motor 11. The stirring and conveying blades 12 can stir the material while conveying the material from a position close to the feed port 3 to a position close to the discharge port 4; the stirring and conveying blades 12 can adopt auger blades, and the residence time of the oily sludge in the first chamber 2 can be controlled by controlling the rotation speed of the rotating shaft 10 and the shape of the stirring and conveying blades 12.

[0114] One end of the rotating shaft 10 passes through the side wall of the housing 1 and is connected to the driving motor 11 outside the housing 1 . A sealing component 25 connected to the housing 1 is disposed on the outer periphery of the rotating shaft 10 .

[0115] Example 2

[0116] like Figure 3 As shown, the difference between this embodiment and embodiment 1 is that:

[0117] In this embodiment, an air intake structure is also included. The output end of the air intake structure is connected to the first chamber 2 and is used to transport acid gas into the first chamber 2. The acid gas is factory waste gas.

[0118] The oily sludge reduction treatment device provided in the present embodiment is provided with a first chamber 2 in a shell 1, and a stirring and conveying mechanism is provided in the first chamber 2. The oily sludge and demulsifier can be input into the first chamber 2 through the feed port 3, and the acidic gas can be input into the first chamber 2 through the air intake structure. Under the stirring and conveying action of the stirring and conveying mechanism, the material is fully in contact with the acidic gas. At the same time, the heating component 6 heats the first chamber 2 to provide a suitable treatment temperature. The demulsifier can break the emulsification system of the oily sludge, and the acidic gas can react with the oily sludge to reduce the pH value of the oily sludge, which is beneficial to the demulsification process of the oily sludge, reduces the stability of the emulsification system, and reduces the viscosity of the oily sludge. After sufficient demulsification, the water and oil in the oily sludge are discharged in liquid form through the capillary channel 5 for collection. At the same time, the treated object material can be discharged through the discharge port 4 for further deep treatment.

[0119] In this embodiment, the air intake structure includes an air intake box 13 , an air intake port 14 of the air intake box 13 is used to communicate with the factory waste smoke pipeline, and a plurality of air distribution ports 15 of the air intake box 13 are communicated with the first chamber 2 .

[0120] The air inlet box 13 is connected to the outer wall of the shell 1 and is connected to the first chamber 2 through multiple air distribution ports 15. The air inlet 14 is used to connect to the factory waste flue gas pipeline to input the factory waste flue gas with a higher temperature and containing acidic gas into the first chamber 2, which not only provides acidic gas but also can heat the material, saving the energy consumption of the heating component 6.

[0121] In this embodiment, the factory waste flue gas is directly input into the first chamber 2, and the factory waste flue gas can be purified to a certain extent during the treatment of oily sludge by the device; and an air outlet 16 is provided on the side wall of the shell 1, and the gas in the shell 1 can enter the factory flue gas purification unit through the air outlet 16, so as to avoid the waste gas generated by the device causing environmental pollution.

[0122] In this embodiment, the liquid collecting tank 8 is connected to a negative pressure generating structure, and the negative pressure generating structure is used to form a negative pressure environment in the liquid collecting tank 8 .

[0123] A negative pressure pipe 17 is provided on the liquid collecting tank 8, which is connected to a negative pressure generating structure through the negative pressure pipe 17. The negative pressure generating structure adopts an air pump to extract the air in the liquid collecting tank 8 and circulates it to the air inlet 14 of the air inlet box 13, so as to keep the liquid collecting tank 8 in a negative pressure environment. The small amount of air circulated to the air inlet 14 and the waste smoke from the factory area keep the inside of the shell 1 in a positive pressure environment. The pressure difference on both sides of the capillary channel 5 can improve the efficiency of the liquid entering the liquid collecting tank 8 through the capillary channel 5.

[0124] Example 3

[0125] like Figures 4 to 6 As shown, the difference between this embodiment and embodiment 1 is that:

[0126] In this embodiment, a second chamber 18 connected to the first chamber 2 is provided inside the shell 1. The second chamber 18 is provided at one end of the first chamber 2 close to the discharge port 4, and the second chamber 18 is gradually tapered from the end away from the discharge port 4 to the end close to the discharge port 4. The side wall of the second chamber 18 is provided with an annular recovery groove 19 with an open inner circumference, the bottom of the recovery groove 19 is provided with a liquid outlet 20, and the open end of the recovery groove 19 is provided with a filter plate 21.

[0127] The first chamber 2 is connected to the discharge port 4 through the second chamber 18. The second chamber 18 is a tapered structure. Under the transmission action of the stirring and conveying mechanism, the material passes through the first chamber 2 and enters the second chamber 18, and is squeezed in the second chamber 18, which promotes the solid-liquid separation of the material in the second chamber 18. The setting of the recovery tank 19 and the filter plate 21 can make the solid material remain in the second chamber 18 and be discharged through the discharge port 4, and the liquid flows into the recovery tank 19 through the filter holes 22 on the filter plate 21, and can flow out through the liquid outlet 20.

[0128] The liquid outlet 20 is communicated with the liquid collecting tank 8, and can introduce the liquid into the liquid collecting tank 8 for collection.

[0129] The filter holes 22 on the filter plate 21 are also capillary channels 5 .

[0130] In this embodiment, an extrusion mechanism is provided in the second chamber 18, and the extrusion mechanism includes a scraper rod 23 rotatably arranged in the second chamber 18. The scraper rod 23 rotates around the cross-sectional center of the second chamber 18 in the cross-section of the second chamber 18. A scraper plate 24 is provided at the outer end of the scraper rod 23, and the scraper plate 24 is in contact with the filter plate 21.

[0131] The scraper rod 23 of the extrusion mechanism rotates around the cross-sectional center of the second chamber 18 in a plane parallel to the cross-sectional plane of the second chamber 18, driving the scraper plate 24 at its outer end to come into contact with the filter plate 21 and move relative to it. The scraping effect of the scraper plate 24 can further squeeze the material between the scraper plate 24 and the filter plate 21, thereby promoting solid-liquid separation and improving separation efficiency and separation effect.

[0132] The scraper blade 24 is made of a rubber sheet.

[0133] The use of soft scraper blades can improve the scraping effect and protect the recovery tank, thereby extending the operating life of the oily sludge reduction treatment device.

[0134] In this embodiment, if Figure 3 and Figure 4As shown, a plurality of scraper rods 23 are provided, and the scraper rods 23 are connected to the outer periphery of the rotating shaft 10 of the stirring and conveying mechanism. The filter holes 22 on the filter plate 21 are arranged in groups, and each group of filter holes 22 has a plurality of filter holes. The plurality of groups of filter holes 22 are evenly distributed on the filter plate 21 along the circumference of the second chamber 18 .

[0135] Example 4

[0136] like Figure 7 As shown, the difference between this embodiment and embodiment 2 is that:

[0137] In this embodiment, a second chamber 18 connected to the first chamber 2 is provided inside the shell 1. The second chamber 18 is provided at one end of the first chamber 2 close to the discharge port 4, and the second chamber 18 is gradually tapered from the end away from the discharge port 4 to the end close to the discharge port 4. The side wall of the second chamber 18 is provided with an annular recovery groove 19 with an open inner circumference, the bottom of the recovery groove 19 is provided with a liquid outlet 20, and the open end of the recovery groove 19 is provided with a filter plate 21.

[0138] In this embodiment, an extrusion mechanism is provided in the second chamber 18, and the extrusion mechanism includes a scraper rod 23 rotatably arranged in the second chamber 18. The scraper rod 23 rotates around the cross-sectional center of the second chamber 18 in the cross-section of the second chamber 18. A scraper plate 24 is provided at the outer end of the scraper rod 23, and the scraper plate 24 is in contact with the filter plate 21.

[0139] Under the transmission action of the stirring and conveying mechanism, the material first passes through the first chamber 2, where the material is fully mixed with the waste flue gas from the factory area, and is not only heated by the waste flue gas from the factory area, but also tempered by the waste flue gas from the factory area, and part of the liquid is discharged from the capillary channel 5 to the liquid collecting tank 8; then the material enters the second chamber 18, and is squeezed in the second chamber 18 to promote the solid-liquid separation of the material in the second chamber 18, and at the same time, the scraper rod 23 of the squeezing mechanism rotates around the cross-sectional center of the second chamber 18 in a plane parallel to the cross-sectional plane of the second chamber 18, driving the scraper plate 24 at its outer end to contact with the filter plate 21 and generate The scraping action of the scraper plate 24 can further squeeze the material between the scraper plate 24 and the filter plate 21, thereby promoting solid-liquid separation and improving separation efficiency and effect. The setting of the recovery tank 19 and the filter plate 21 can make the solid material remain in the second chamber 18 and be discharged through the discharge port 4, and the liquid flows into the recovery tank 19 through the filter holes 22 on the filter plate 21, and can flow into the collecting tank through the liquid outlet hole 20 for collection; in this way, the oily sludge undergoes two solid-liquid separations when passing through the first chamber 2 and the second chamber 18 in sequence, which can further improve the separation effect and efficiency.

[0140] Examples 5A-5S and Comparative Example 1

[0141] The oily sludge reduction treatment device of Example 1 is used to reduce the oily sludge, and the steps are as follows: Figure 8 shown.

[0142] Example 5A

[0143] The oily sludge to be treated has a water content of 33%, a solid content of 6% and an oil content of 61%. The treatment method is as follows:

[0144] S1: Adding oily sludge

[0145] The oily sludge to be treated is introduced into the first chamber 2 through the feed port 3 at a flow rate of 8 kg / h, and 16 g / h of demulsifier (sodium lignin sulfonate) is added;

[0146] S2: Demulsification of oily sludge

[0147] The temperature of the material in the first chamber 2 is maintained at 72°C, and the material is continuously stirred and conveyed under the action of the stirring and conveying mechanism;

[0148] S3: Discharge of oily sludge

[0149] The material which has been in the first chamber 2 for 3 hours is discharged from the first chamber 2 through the discharge port 4. The composition of the material discharged from the first chamber 2 is as follows: water content 13%, solid content 72%, oil content 15%, and the oily sludge is reduced by 92%;

[0150] S4: Capillary recovery

[0151] The chamber wall of the first chamber 2 has capillary channels with an average pore size of 2.2 μm, accounting for 3.1% of the volume. The oil and water in the first chamber 2 are absorbed into the collecting tank 8 through the capillary channels 5. During the continuous operation of the device, about 0.31 L of water and about 0.61 L of oil are obtained after each kg of oil-containing sludge is treated, which are further separated by gravity for recycling.

[0152] S5: Every 1000 hours, air is back-blown through the drain port to the capillary channel.

[0153] The device of the present invention is compared with a conventional oily sludge reduction treatment device of the same volume. The conventional oily sludge reduction treatment device is not equipped with capillary channels, but uses a conventional high-speed centrifugal method to achieve solid-liquid separation. By comparison, the conventional device costs about 268 yuan per ton of oily sludge, while the oily sludge reduction treatment device used in this embodiment saves high-speed centrifugal equipment, realizes solid-liquid separation and recovery at a low cost, and the cost of treating one ton of oily sludge is about 196 yuan, which has significant economic advantages.

[0154] Example 5B

[0155] The oily sludge to be treated has a water content of 52%, a solid content of 5% and an oil content of 43%. The treatment method is as follows:

[0156] S1: Adding oily sludge

[0157] The oily sludge to be treated is introduced into the first chamber 2 through the feed port 3 at a flow rate of 10 kg / h;

[0158] S2: Demulsification of oily sludge

[0159] The temperature of the material in the first chamber 2 is maintained at 85°C, and the material is continuously stirred and conveyed under the action of the stirring and conveying mechanism;

[0160] S3: Discharge of oily sludge

[0161] The material which has been in the first chamber 2 for 14 hours is discharged from the first chamber 2 through the discharge port 4. The composition of the material discharged from the first chamber 2 is as follows: water content 10%, solid content 83%, oil content 7%, and the oily sludge is reduced by 94%;

[0162] S4: Capillary recovery

[0163] The chamber wall of the first chamber 2 has capillary channels with an average pore size of 2.8 μm, accounting for 2.4% of the volume. The oil and water in the first chamber 2 are absorbed into the collecting tank 8 through the capillary channels 5. During the continuous operation of the device, about 0.50 L of water and about 0.46 L of oil are obtained after each kg of oil-containing sludge is treated, which are further separated by gravity for recycling.

[0164] S5: Every 1000 hours, air is back-blown through the drain port to the capillary channel.

[0165] Comparative Example 1

[0166] The device with the same structure as that of Example 5A is used, but the side wall of the first chamber 2 is not provided with capillary channels. After the treated oily sludge is discharged through the discharge port 4, a high-speed centrifuge is used to separate the oily sludge after demulsification into solid and liquid. The overall cost of treating the oily sludge is about 277 yuan / ton, and about 0.32L of water and 0.61L of oil products are obtained after each kg of oily sludge is treated. However, the cost of treating the oily sludge by using the device and method described in Example 1A is about 196 yuan / ton, and about 0.3L of water and 0.62L of oil products are obtained after each kg of oily sludge is treated. It can be seen that the device of the present invention has higher economic benefits and can achieve solid-liquid separation at low cost.

[0167] Examples 5C-5N

[0168] The same structure as in Example 5A was used, but the capillary pore size was different to carry out the oily sludge reduction treatment. The results of the amount of oil and water resources recovered from the oily sludge after treatment with different capillary pore sizes are shown in Table 1 below:

[0169] Table 1

[0170]

[0171] By comparison, it was found that when the average pore size of the capillary channels is 1-5μm, the oil-water separation ability is strong, and more than 0.25L of water and more than 0.55L of oil can be recovered per kg of oily sludge. When the average pore size of the capillary channels is greater than 5μm, the capillary siphon effect is weakened, and the water and oil recovery capacity decreases. When the capillary channel volume accounts for 0.2-6%, the oil-water separation ability is strong, and more than 0.25L of water and more than 0.55L of oil can be recovered per kg of oily sludge. When the capillary channel volume accounts for less than 0.2%, the capillary channels are insufficient and the oil and water recovery capacity decreases. When the capillary channel volume accounts for more, the excessively large wall openings will weaken the siphon effect, resulting in a decrease in the oil and water recovery capacity.

[0172] Examples 50-5S

[0173] The same device and method as in Example 5A were used to treat the oily sludge. In Example 5A, air backwashing was performed on the capillary channel through the discharge port every 1000 hours, which ensured that the oily sludge reduction rate was still above 90% when the device was operated for 16000 hours. In Examples 5I-5M, the backwashing frequency was changed, and the corresponding oily sludge reduction rate change results are shown in Table 2 below:

[0174] Table 2

[0175]

[0176]

[0177] By comparison, it is found that regular back-flushing of the capillary channels can ensure the stability of the device and ensure efficient oil-water separation efficiency, and controlling the reasonable back-flushing frequency can achieve low-cost separation and recovery of oil and water resources. Controlling the back-flushing time interval within 500-2000h can ensure that the equipment maintains an oily sludge reduction rate of more than 90.5% when it is running for 4000h, an oily sludge reduction rate of more than 90% when it is running for 8000h, and an oily sludge reduction rate of more than 88% when it is running for 16000h.

[0178] Compared with CN114632789B and CN115463462A, this embodiment greatly simplifies the difficulty of solid-liquid separation and reduces the cost of solid-liquid separation by setting capillary channels on the side wall of the first chamber without increasing the difficulty of manufacturing the device, thereby significantly improving the cost of the oily sludge reduction process and having higher economic performance.

[0179] Examples 6A-6Z and Comparative Examples 2-4

[0180] The oily sludge reduction treatment device of Example 2 is used to reduce the oily sludge, and the steps are as follows: Fig. 9 shown.

[0181] Example 6A

[0182] The oily sludge to be treated has a water content of 36%, a solid content of 3%, an oil content of 61%, and a pH of 8.2. At the same time, there is flue gas emission from the production process and heating boilers in the plant area. After dust removal, the waste flue gas in the plant area has a flue gas temperature of 215°C, a SO2 content of 600ppm, and a CO2 content of 27%. The treatment method is as follows:

[0183] S1: Material feeding

[0184] Sodium lignin sulfonate and sodium dodecylbenzene sulfonate were selected as two demulsifiers and mixed with oily sludge. The ratio of the two demulsifiers was 1:1. The amount of demulsifier added was 3g demulsifier / L oily sludge. The oily sludge continuously entered the first chamber 2 through the feed port 3. The feed rate was 25kg / h. The waste gas from the plant was heated at 3m 3 / h of feed volume continuously enters the first chamber 2 through the air inlet 14;

[0185] S2: Oily sludge reduction

[0186] In the first chamber 2, the oily sludge is heated by the heating component 6 and the waste flue gas from the plant area, and the temperature of the oily sludge reaches 75°C. The waste flue gas from the plant area is evenly contacted with the oily sludge through the air distribution port 15. The oily sludge absorbs SO2 and CO2 in the waste flue gas from the plant area, so that the pH value of the oily sludge is adjusted to 7.7, and the demulsifier effect is enhanced. The stirring and conveying mechanism stirs and pushes the oily sludge, and the residence time of the oily sludge in the shell 1 is maintained for 1 hour, so that the oily sludge is demulsified to form solid oily sludge and liquid water and oil.

[0187] S3: Separation and recovery

[0188] The negative pressure environment is created by evacuating the liquid collecting tank 8 through the negative pressure pipe 17. The pressure in the liquid collecting tank 8 is 0.092Mpa. The evacuated air is introduced into the air inlet 14 and enters the first chamber 2 together with the waste gas from the factory area, so that a slight positive pressure of 0.111Mpa is formed in the first chamber 2. The average pore size of the capillary channel 5 is 0.86 microns, and the volume of the capillary channel 5 accounts for 1.36% of the bottom of the shell. After the oily sludge is demulsified, the separated water and oil enter the liquid collecting tank 8 through the capillary channel 5 in a self-priming manner;

[0189] S4: Material discharge

[0190] The oily sludge after demulsification is driven by the stirring and conveying mechanism for 1 hour and is continuously discharged from the device through the discharge port 4. The volume of the oily sludge after reduction treatment is reduced by 90%, the water content of the oily sludge is 25%, the oil content is 37%, and the solid content is 38%; the flue gas in the shell 1 and the gas generated during the reaction process are discharged through the outlet 16, the temperature of the discharged gas is 179°C, the SO2 content is 336ppm, the CO2 content is 26.9%, the H2S content is 1.2ppm, and the VOCs content is 8ppm; the discharged gas can be returned to the factory flue gas treatment unit for purification, the water and oil collected in the liquid collecting tank 8 are used as the oil-water interface as the judgment basis, and the water and oil can be recovered separately through the discharge port 9, the recovered water is transported to the factory wastewater treatment unit, and the recovered oil is returned to the oil storage tank for reuse.

[0191] Example 6B

[0192] The oily sludge to be treated has a water content of 38%, a solid content of 16%, an oil content of 46%, and a pH of 8.6; after dust removal, the waste flue gas from the production process and heating boilers in the plant has a flue gas temperature of 238°C, a SO2 content of 350ppm, and a CO2 content of 32%. The treatment method is as follows:

[0193] S1: Material feeding

[0194] Propylene glycol and nonylphenol polyoxyethylene ether are used as two demulsifiers to mix with oily sludge. The ratio of the two demulsifiers is 1:3. The amount of demulsifier added is 3g demulsifier / L oily sludge. The oily sludge continuously enters the first chamber 2 through the feed port 3. The feed rate is 18kg / h. The waste gas in the plant is 1.9m 3 / h of feed volume continuously enters the first chamber 2 through the air inlet 14;

[0195] S2: Oily sludge reduction

[0196] In the first chamber 2, the oily sludge is heated by the heating component and the waste flue gas from the plant area, and the temperature of the oily sludge reaches 80°C. The waste flue gas from the plant area is evenly contacted with the oily sludge through the air distribution port 15. The oily sludge absorbs SO2 and CO2 in the waste flue gas from the plant area, so that the pH value of the oily sludge is adjusted to 8.1, and the demulsifier effect is enhanced. The stirring and conveying mechanism stirs and pushes the oily sludge, and the residence time of the oily sludge in the shell 1 is maintained for 80 minutes, so that the oily sludge is demulsified to form solid oily sludge and liquid water and oil.

[0197] S3: Separation and recovery

[0198] The negative pressure environment is created by evacuating the liquid collecting tank 8 through the negative pressure pipe 17. The pressure in the liquid collecting tank 8 is 0.095Mpa. The evacuated air is introduced into the air inlet 14 and enters the first chamber 2 together with the waste gas from the factory area, so that a slight positive pressure of 0.114Mpa is formed in the first chamber 2. The average pore size of the capillary channel 5 is 1.26 microns, and the volume of the capillary channel 5 accounts for 1.48% of the bottom of the shell. After the oily sludge is demulsified, the separated water and oil enter the liquid collecting tank 8 through the capillary channel 5 in a self-priming manner;

[0199] S4: Material discharge

[0200] After demulsification, the oily sludge is continuously discharged from the device through the discharge port 4 driven by the stirring and conveying mechanism. The volume of the oily sludge after reduction treatment is reduced by 76%, the water content of the oily sludge is 13%, the oil content is 21%, and the solid content is 66%; the flue gas in the shell 1 and the gas generated during the reaction are discharged through the gas outlet 16. The temperature of the discharged gas is 148°C, the SO2 content is 227ppm, the CO2 content is 21.8%, the H2S content is 0.8ppm, and the VOCs content is 4ppm. The discharged gas returns to the factory flue gas treatment unit for purification.

[0201] Example 6C

[0202] The oily sludge to be treated has a water content of 76%, a solid content of 6%, an oil content of 18%, and a pH of 7.3; the waste flue gas from the production process and heating boilers in the plant area has a flue gas temperature of 179°C, a SO2 content of 468ppm, and a CO2 content of 22% after dust removal. The treatment method is as follows:

[0203] S1: Material feeding

[0204] Sodium dodecylbenzene sulfonate demulsifier is selected to mix with oily sludge, and the demulsifier addition amount is 4g demulsifier / L oily sludge. The oily sludge continuously enters the first chamber 2 through the feed port 3, and the feed rate is 29kg / h. The waste gas in the plant area is 2.8m 3 / h of feed volume continuously enters the first chamber 2 through the air inlet 14;

[0205] S2: Oily sludge reduction

[0206] In the first chamber 2, the oily sludge is heated by the heating component and the waste flue gas from the plant area, and the temperature of the oily sludge reaches 75°C. The waste flue gas from the plant area is evenly contacted with the oily sludge through the air distribution port 15, and the oily sludge absorbs SO2 and CO2 in the waste flue gas, so that the pH value of the oily sludge is adjusted to 7.0, and the demulsifier effect is enhanced. The stirring and conveying mechanism stirs and pushes the oily sludge, and the residence time of the oily sludge in the shell 1 is maintained for 1 hour, and the oily sludge is demulsified to form solid oily sludge and liquid water and oil;

[0207] S3: Separation and recovery

[0208] The negative pressure environment is created by evacuating the liquid collecting tank 8 through the negative pressure pipe 17. The pressure in the liquid collecting tank 8 is 0.088Mpa. The evacuated air is introduced into the air inlet 14 and enters the first chamber 2 together with the waste gas from the factory area, so that a slight positive pressure of 0.119Mpa is formed in the first chamber 2. The average pore size of the capillary channel 5 is 1.52 microns, and the volume of the capillary channel 5 accounts for 1.76% of the bottom of the shell. After the oily sludge is demulsified, the separated water and oil enter the liquid collecting tank 8 through the capillary channel 5 in a self-priming manner;

[0209] S4: Material discharge

[0210] After demulsification, the oily sludge is continuously discharged from the device through the discharge port 4 driven by the stirring and conveying mechanism. The volume of the oily sludge after reduction treatment is reduced by 88%, the water content of the oily sludge is 38%, the oil content is 12%, and the solid content is 50%; the flue gas in the shell 1 and the gas generated during the reaction are discharged through the gas outlet 16. The temperature of the discharged gas is 122°C, the SO2 content is 402ppm, the CO2 content is 22%, the H2S content is 2.2ppm, and the VOCs content is 12.6ppm. The discharged gas returns to the factory flue gas treatment unit for purification.

[0211] Comparative Example 2

[0212] The same device as in Example 6A was used, but the intake air was changed from factory waste gas to air, and the air parameters were 23°C, SO2 content was 0 ppm, and CO2 content was 0.03%.

[0213] Without the heating and conditioning effects of the factory's waste gas, at the same power, the temperature of the oily sludge in the oily sludge reduction treatment device dropped to 43°C, the pH was 8.2, and the volume reduction rate of the oily sludge after demulsification was 63%, the water content was 33%, the solid content was 8%, and the oil content was 59%. The oily sludge reduction effect was significantly reduced, and the factory's waste gas purification was not achieved.

[0214] Comparative Example 3

[0215] A device with the same structure as in Example 6A is used, but no micro-pressure difference is constructed in the device, that is, the pressure in the device and the collection tank are both at normal pressure.

[0216] Without the setting of micro-pressure difference, the oil and water recovery capacity of the capillary channels is reduced. The reduction rate of oily sludge discharged from the device is 83%, the water content is 29%, the solid content is 18%, and the oil content is 53%. The separation capacity of the oily sludge is reduced and the reduction effect is reduced.

[0217] Examples 6D-6G

[0218] Using a device with the same structure as Example 6B, the content of oily sludge components before and after the operation of the device was compared with or without positive and negative pressure differences and with or without factory waste flue gas conditioning. The comparison results are shown in Table 3 below:

[0219] Table 3

[0220]

[0221] By comparison, it was found that the positive and negative pressure difference can improve the separation and recovery of oil and water in the capillary channel 5, and the waste flue gas in the factory area can effectively enhance the demulsification effect of the device on oily sludge. The use of flue gas conditioning or positive and negative pressure difference to promote recovery can achieve a reduction rate of >68%, and when used together, a reduction rate of more than 75% can be achieved. However, without using flue gas conditioning and positive and negative pressure difference to promote recovery, only a 60% reduction rate of oily sludge can be achieved.

[0222] Examples 6H-6K

[0223] The same structure as in Example 6A was used, but the micro-pressure difference in the housing 1 was changed. The results of the content of the components of the oily sludge after treatment corresponding to different micro-pressure differences are shown in Table 4 below:

[0224] Table 4

[0225]

[0226]

[0227] The comparison shows that the construction of micro-pressure difference affects the solid-liquid separation and recovery effect, and the reasonable setting of micro-pressure difference can improve the oily sludge reduction treatment effect. After constructing a reasonable micro-pressure difference, the oily sludge reduction rate can reach more than 85%.

[0228] Examples 6L-6Y

[0229] The device with the same structure as in Example 6A was used, but the capillary channel size and volume ratio on the device were different. The results of the amount of oil and water resources recovered from the treated oily sludge with different capillary channel sizes and volume ratios are shown in Table 5 below:

[0230] Table 5

[0231]

[0232]

[0233] By comparison, it was found that under fixed temperature and micro-pressure difference, controlling the size and volume proportion of capillary channels can promote solid-liquid separation and improve the reduction effect of the device on oily sludge. When the pore size is 0.05-3.5μm, the reduction rate of oily sludge can be maintained at more than 80%. When the pore size is too small, the resistance to oil and water recovery is large, and when the pore size is too large, the capillary siphon effect is weakened, which will lead to poor oil and water recovery effect and reduced oily sludge reduction rate. When the volume proportion of capillary channels is 0.2-2%, the alkali effect of oily sludge is better, and the reduction rate is more than 85%. When the volume proportion of capillary channels is relatively small (<0.2%), the capillary channels are insufficient and the oil and water recovery effect is poor. When the volume proportion of capillary channels is large (>2%), excessively large wall openings will weaken the siphon effect, resulting in a decrease in oil and water recovery capacity.

[0234] Embodiment 6Z1-6Z 19

[0235] The same structure as that of Example 6A was used, but the feed amount of the waste flue gas was adjusted. The properties of the oily sludge after conditioning and the reduction rate corresponding to different waste flue gas feed amounts are shown in Table 6 below:

[0236] Table 6

[0237]

[0238]

[0239] The treated oily sludge has a water content of 36%, a solid content of 3%, an oil content of 61%, and a density of 0.9987 kg / L. This embodiment uses 1 kg / L for calculation. When the waste gas feed rate ranges from 2.5 to 3.75 m 3 / h (this range corresponds to the waste flue gas and oily sludge volume ratio range of 100:1 ~ 150:1), the pH of the oily sludge after conditioning is in the range of 7.5-8.0, and the temperature is 70-80℃, which is suitable for the demulsifier to play a role, maintain the oily sludge demulsification effect, and the oily sludge reduction rate is more than 85%, especially when the waste flue gas feed volume is 3m 3 / h (the corresponding waste flue gas to oily sludge volume ratio is 120:1 at this time), the effect is best, the temperature of the oily sludge after conditioning reaches the optimal temperature of 75°C for the demulsifier to work, and the oily sludge achieves a 90% reduction rate. 3 / h (at this time, the volume ratio of waste flue gas to oily sludge is higher than 150:1), the temperature of the oily sludge after conditioning is higher than 80℃, the demulsification effect of the demulsifier decreases, resulting in the oily sludge reduction rate being lower than 85%; when the waste flue gas feed rate is further increased, the waste flue gas feed rate is greater than 10m 3 / h (the corresponding waste flue gas to oily sludge volume ratio is higher than 400:1), the pH of the oily sludge after conditioning is less than 7, and the demulsification effect of the demulsifier decreases, resulting in an oily sludge reduction rate of less than 70%. 3 / h (at this time, the volume ratio of waste flue gas to oily sludge is less than 100:1), the temperature of the oily sludge after conditioning is lower than 70°C, and the pH is higher than 8.0, the demulsification effect of the demulsifier decreases, resulting in an oily sludge reduction rate of less than 85%; when the waste flue gas feed rate is further reduced, the waste flue gas feed rate is less than 1.25m 3 / h (at this time, the volume ratio of waste flue gas to oily sludge is less than 50:1), the temperature of the oily sludge after conditioning is lower than 60°C, and the demulsification effect of the demulsifier is significantly reduced, resulting in an oily sludge reduction rate of less than 75%.

[0240] Compared with CN114933400B and CN111908743B, this embodiment utilizes the waste flue gas resources in the plant area to heat and temper the oily sludge to enhance the demulsification effect of the device, and realizes the demulsification of the oily sludge and the recovery of oil and water in an integrated manner. The operation is simple and the device can realize continuous demulsification of the oily sludge. The operation is simple and the work efficiency is high. The capillary self-priming method is used to realize the low-cost recovery of oil and water resources, significantly improve the economic benefits of the oily sludge reduction treatment device and coordinate the treatment of the waste flue gas in the plant area, with high environmental benefits. This embodiment adopts micro-positive pressure and micro-negative pressure, there is no high-pressure explosion risk, and it is highly safe. The cost of the device to achieve the treatment of oily sludge by capillary self-priming is about 157 yuan / ton, and the cost of treating oily sludge by the oily sludge reduction treatment device equipped with a high-speed centrifuge is about 268 yuan / ton. The cost advantage of recovering oil and water resources in this embodiment is significant.

[0241] Examples 7A-7J and Comparative Examples 5-6

[0242] The oily sludge reduction treatment device of Example 3 is used to reduce the oily sludge, and the steps are as follows: Fig.10 shown.

[0243] Example 7A

[0244] The oily sludge to be treated has a water content of 56%, a solid content of 7%, and an oil content of 37%. The treatment method is as follows:

[0245] S1: Feed

[0246] Add the oily sludge and demulsifier into the first chamber 2 through the feed port 3, the feed flow rate of the oily sludge is 15 kg / h, and sodium lignin sulfonate is added as a demulsifier, and the feed rate of the demulsifier is 90 g / h;

[0247] S2: Demulsification

[0248] In the first chamber 2, the material is continuously stirred and slowly pushed by the stirring and conveying mechanism. The residence time of the oily sludge in the first chamber 2 is 3 hours. The temperature of the oily sludge in the first chamber 2 is increased by the heating component, and the temperature of the oily sludge is maintained at 73°C.

[0249] S3: Separation and recovery

[0250] The demulsified oily sludge enters the second chamber 18. The second chamber 18 is not equipped with a heating component. The oily sludge itself is kept warm to an average temperature of 42°C. The second chamber 18 is provided with three recovery tanks 19 and a corresponding scraper mechanism. The scraper rod 23 of the scraper mechanism contacts the filter plate 21 through a scraper plate 24 made of synthetic rubber. The extrusion of the scraper plate 24 and the filter plate 21 promotes solid-liquid separation and allows the liquid phase oil and water to enter the collecting tank 8 through the liquid outlet 20 on the bottom of the recovery tank 19. The filter plate 21 effectively blocks solids from entering the recovery tank 19. The purity of the liquid phase entering the recovery tank 19 is as high as 99.92%. It further enters the collecting tank 8 through the liquid outlet 20 for oil-water stratification separation and recovery;

[0251] S4: Discharging

[0252] While achieving solid-liquid separation in the second chamber 18, the oil and water in the liquid phase are recovered, and the oil-containing sludge reduction rate reaches 88%. Due to the reduction in the content of the oil-containing sludge, the space occupied by the oil-containing sludge in the second chamber 18 is reduced, and the residence time in the second chamber 18 is extended from 2 hours to 3.5 hours, further improving the solid-liquid separation efficiency and the oil-water recovery efficiency. The solid material discharged through the discharge port 4 has a composition of 19% water content, 70% solid content, and 11% oil content, achieving an oil-containing sludge reduction rate of 90%. The waste gas generated in the demulsification process can be discharged from the outlet 16 to the gas purification unit for purification and discharge.

[0253] Example 7B

[0254] The oily sludge to be treated has a water content of 55%, a solid content of 3%, and an oil content of 42%. The treatment method is as follows:

[0255] S1: Feed

[0256] Add the oily sludge and demulsifier into the first chamber 2 through the feed port 3, the feed flow rate of the oily sludge is 10 kg / h, and no demulsifier is added;

[0257] S2: Demulsification

[0258] In the first chamber 2, the material is continuously stirred and slowly pushed by the stirring and conveying mechanism. The residence time of the oily sludge in the first chamber 2 is 12 hours. The temperature of the oily sludge in the first chamber 2 is increased by the heating component, and the temperature of the oily sludge is maintained at 86°C.

[0259] S3: Separation and recovery

[0260] The oily sludge after heating and demulsification enters the second chamber 18. The second chamber 18 is not equipped with a heating component. The oily sludge itself is kept warm to an average temperature of 48°C. The second chamber 18 is provided with 6 recovery tanks 19 and a corresponding scraper mechanism. The scraper rod 23 of the scraper mechanism contacts the filter plate 21 through a scraper plate 24 made of synthetic rubber. The extrusion of the scraper plate 24 and the filter plate 21 promotes solid-liquid separation and allows the liquid phase oil and water to enter the collecting tank 8 through the liquid outlet 20 on the bottom of the recovery tank 19. The filter plate 21 effectively blocks solids from entering the recovery tank 19. The purity of the liquid phase entering the recovery tank 19 is as high as 99.94%. It further enters the collecting tank 8 through the liquid outlet 20 for oil-water stratification separation and recovery;

[0261] S4: Discharging

[0262] While achieving solid-liquid separation in the second chamber 18, the oil and water in the liquid phase are recovered, and the oil-containing sludge reduction rate reaches 88%. Due to the reduction in the content of the oil-containing sludge, the space occupied by the oil-containing sludge in the second chamber 18 is reduced, and the residence time of the second chamber 18 is extended from 6 hours to 10.8 hours, further improving the solid-liquid separation efficiency and the oil-water recovery efficiency. The composition of the solid phase material discharged through the discharge port 4 is: water content 23%, solid content 62%, oil content 15%, and the oil-containing sludge reduction rate reaches 95%. The waste gas generated in the demulsification process can be discharged from the outlet 16 to the gas purification unit for purification and discharge.

[0263] Comparative Example 5

[0264] The device with the same structure as that of Example 7A is adopted, but the scraper plate 24 is not provided, and the scraper rod 23 is an integrated steel scraper rod 23. After long-term operation comparison, the filter plate 22 in Example 7A is less worn and the service life reaches 2700 hours, while the integrated steel scraper rod 23 wears the filter plate 22 more, and the oily sludge reduction rate of the filter plate 22 is less than 70% after the service life of the filter plate 22 reaches 962 hours, and the filter plate 22 needs to be replaced.

[0265] Comparative Example 6

[0266] The device adopts the same structure as that of Example 7A, but the scraper blade 24 is made of brush material. Compared with the scraper blade 24 made of synthetic rubber in Example 7A, the oily sludge reduction rate achieved in Example 7A reaches 88%. After adopting the scraper blade 24 made of brush material, the oily sludge reduction rate is reduced to 83%. It can be seen that the synthetic rubber scraper blade 24 can improve the solid-liquid separation efficiency.

[0267] Examples 7C-7F

[0268] The same structure as that of Example 7A is used, but the number of recovery slots 19 on the inner wall of the second chamber 18 is different. The different numbers of recovery slots 19 and the parameters of the treated oily sludge are shown in Table 6 below:

[0269] Table 6

[0270] serial number Number of recycling tanks Moisture content / % Solid content / % Oil content / % Reduction rate / % Example 7A 3 19 70 11 90 Example 7C 2 26 55 19 87 Example 7D 1 33 40 27 83 Example 7E 5 17 72 11 90 Example 7F 0 55 8 37 13

[0271] By comparison, it is found that optimizing the number of recovery tanks 19 can control and achieve efficient oily sludge reduction treatment at low cost.

[0272] Examples 7G-7J

[0273] The same structure as that of Example 7A is used, but the number of scraper rods 23 in the second chamber 18 is different. The parameters of the treated oily sludge corresponding to the different numbers of scraper rods 23 are shown in Table 7 below:

[0274] Table 7

[0275]

[0276] By comparison, it is found that the number of scraper rods 23 produces different scraping frequencies during operation, which can affect the reduction treatment effect of oily sludge.

[0277] Compared with the traditional method of using a high-speed centrifuge to achieve solid-liquid separation, this embodiment uses the scraping effect of the scraper plate 24 of the extrusion mechanism to further squeeze the material between the scraper plate 24 and the filter plate 21, promote solid-liquid separation, and improve separation efficiency and separation effect. The cost of the device for achieving solid-liquid separation by a high-speed centrifuge is about 257 yuan / ton for reducing oily sludge, while the cost of processing oily sludge by extrusion separation in this embodiment is reduced to about 192 yuan / ton, indicating that this embodiment can significantly reduce the cost of solid-liquid separation in the process of reducing oily sludge.

[0278] Examples 8A-8H and Comparative Examples 7-8

[0279] The oily sludge reduction treatment device of Example 4 is used to reduce the oily sludge, and the steps are as follows: Fig.11 shown.

[0280] Example 8A

[0281] The oily sludge to be treated has a water content of 26%, a solid content of 21% and an oil content of 53%, a pH of 8.3, and a temperature of 263°C, a SO2 content of 832ppm, and a CO2 content of 28% after dust removal. The treatment method is as follows:

[0282] S1: Material feeding

[0283] The oily sludge and demulsifier are added into the first chamber 2 through the feed port 3. The feed rate of the oily sludge is 22 kg / h. The demulsifier is selected from nonylphenol polyoxyethylene ether, hexadecyl trimethyl ammonium bromide and ethylenediamine in a ratio of 2:1:1. The demulsifier addition rate is 12 g / h. The waste gas from the plant is heated at 2 m 3 / h of feed volume continuously enters the first chamber 2 through the air inlet 14;

[0284] S2: Oily sludge reduction

[0285] In the first chamber 2, the oily sludge is heated by the heating component 6 and the waste flue gas from the plant area, and the temperature of the oily sludge reaches 73°C. The waste flue gas from the plant area is evenly contacted with the oily sludge through the air distribution port 15. The oily sludge absorbs SO2 and CO2 in the waste flue gas from the plant area, so that the pH value of the oily sludge is adjusted to 7.6, which can enhance the demulsification effect of the demulsifier on the oily sludge. The stirring and conveying mechanism stirs and pushes the oily sludge, and the residence time of the oily sludge in the shell 1 is kept for 1.5 hours, so that the oily sludge is demulsified to form solid oily sludge and liquid water and oil.

[0286] The material is continuously stirred and slowly pushed by the stirring and conveying mechanism, and the waste gas from the plant area directly enters the first chamber 2 through the multiple air distribution ports 15 in the air intake structure, and the waste gas is fully in contact with the oily sludge in the first chamber 2. The waste gas after contact is continuously discharged from the first chamber 2 through the air outlet 16. In the process of contact between the waste gas and the oily sludge, the waste gas will heat up the oily sludge, saving the energy consumption of the heating component 6. At the same time, SO2 and CO2 in the waste gas are absorbed and processed by the oily sludge, and the heat energy is also utilized as a resource;

[0287] S3: Separation and recovery

[0288] The chamber wall in the first chamber 2 is provided with capillary channels with an average pore size of 1.02μm, and the volume of the capillary channels accounts for 1.0%. The negative pressure environment is created by evacuating the liquid collecting tank 8 through the negative pressure pipe 17. The pressure in the liquid collecting tank 8 is 0.093Mpa. The extracted air is introduced into the air inlet 14 and enters the first chamber 2 together with the waste smoke from the factory area, so that a slight positive pressure of 0.117Mpa is formed in the first chamber 2. Under the promotion of the slight pressure difference, the free oil and water separated by demulsification in the first chamber 2 can be easily absorbed into the liquid collecting tank 8 through the capillary channels 5. During the continuous operation of the device, about 0.16L of water and about 0.43L of oil resources can be recovered through the capillary channels on the wall of the first chamber 2 for every 1kg of oily sludge treated; the demulsified oily sludge enters the second chamber 18 from the first chamber 2 under the drive of mechanical stirring. The second chamber 18 is not equipped with a heating component, and the oily sludge The sludge itself is kept warm to an average temperature of 44°C. The second chamber 18 is provided with three recovery tanks 19 and a corresponding scraper mechanism. The scraper rod 23 of the scraper mechanism contacts the filter plate 21 through a scraper plate 24 made of synthetic rubber. The extrusion of the scraper plate 24 and the filter plate 21 promotes solid-liquid separation and allows the liquid phase oil and water to enter the liquid collecting tank 8 through the liquid outlet 20 on the bottom of the recovery tank 19. For every 1kg of oily sludge processed, about 0.09L of water and 0.08L of oil resources can be recovered through the capillary channels in the second chamber 18; since most of the free water and oil have been separated in the first chamber 2, the second chamber 18 only needs to recover the water and oil with low recovery efficiency due to micro-pressure difference caused by capillary adsorption between solid phases through the extrusion device, which greatly shortens the residence time of the oily sludge in the second chamber 18, and the residence time of the oily sludge in the second chamber 18 is controlled to be 0.7h. The overall residence time of the oily sludge in the device is 2.2 hours, and the device of the present invention has a very high oily sludge treatment efficiency;

[0289] S4: Discharging

[0290] After further deep recovery of water and oil products in the second chamber 18, the oily sludge reduction rate reached 77%, and the solid material discharged through the discharge port 4 had a water content of 4%, a solid content of 92%, and an oil content of 4%. The flue gas and the gas generated during the reaction were discharged through the gas outlet 16. The temperature of the discharged gas was 175°C, the SO2 content was 457ppm, the CO2 content was 27.8%, the H2S content was 1.4ppm, and the VOCs content was 9ppm. The discharged gas returned to the factory flue gas treatment unit for purification.

[0291] Example 8B

[0292] The oily sludge to be treated has a water content of 36%, a solid content of 5% and an oil content of 59%, a pH of 8.1, and a temperature of 237°C, a SO2 content of 426ppm and a CO2 content of 22% after dust removal in the factory area. The treatment method is as follows:

[0293] S1: Material feeding

[0294] The oily sludge is added into the first chamber 2 through the feed port 3. The feed rate of the oily sludge is 20 kg / h. The waste gas from the plant is heated at a rate of 4 m 3 / h of feed volume continuously enters the first chamber 2 through the air inlet 14;

[0295] S2: Oily sludge reduction

[0296] In the first chamber 2, the oily sludge is heated by the heating component 6 and the waste flue gas from the plant area, and the temperature of the oily sludge reaches 85°C. The waste flue gas from the plant area is evenly contacted with the oily sludge through the air distribution port 15. The oily sludge absorbs SO2 and CO2 in the waste flue gas from the plant area, so that the pH value of the oily sludge is adjusted to 7.5, which can enhance the demulsification effect of the demulsifier on the oily sludge. The stirring and conveying mechanism stirs and pushes the oily sludge, and the residence time of the oily sludge in the shell 1 is maintained for 12 hours, so that the oily sludge is demulsified to form solid oily sludge and liquid water and oil.

[0297] The material is continuously stirred and slowly pushed by the stirring and conveying mechanism, and the waste gas from the plant area continuously enters the first chamber 2 directly through the multiple air distribution ports 15 in the air intake structure, and the waste gas fully contacts the oily sludge in the first chamber 2, and the waste gas after contact is continuously discharged from the first chamber 2 through the air outlet 16. In the process of contact between the waste gas and the oily sludge, the waste gas will heat up the oily sludge, saving the energy consumption of the heating component 6, and at the same time, the SO2 and CO2 in the waste gas are absorbed and processed by the oily sludge, and the heat energy is also utilized as a resource;

[0298] S3: Separation and recovery

[0299] The chamber wall in the first chamber 2 is provided with capillary channels with an average pore size of 0.86μm, and the volume of the capillary channels accounts for 1.7%. The negative pressure environment is created by evacuating the liquid collecting tank 8 through the negative pressure pipe 17. The pressure in the liquid collecting tank 8 is 0.091Mpa. The evacuated air is introduced into the air inlet 14 and enters the first chamber 2 together with the waste smoke from the factory area, so that a slight positive pressure of 0.121Mpa is formed in the first chamber 2. Under the promotion of the slight pressure difference, the free oil and water separated by demulsification in the first chamber 2 can be easily absorbed into the liquid collecting tank 8 through the capillary channels 5. During the continuous operation of the device, about 0.29L of water and about 0.51L of oil resources can be recovered through the capillary channels on the wall of the first chamber 2 for every 1kg of oily sludge treated; the demulsified oily sludge enters the second chamber 18 from the first chamber 2 under the drive of mechanical stirring. The second chamber 18 is not equipped with a heating component, and the oily sludge The sludge itself is kept warm to an average temperature of 48°C. The second chamber 18 is provided with two recovery tanks 19 and a corresponding scraper mechanism. The scraper rod 23 of the scraper mechanism contacts the filter plate 21 through a scraper plate 24 made of synthetic rubber. The extrusion of the scraper plate 24 and the filter plate 21 promotes solid-liquid separation and allows the liquid phase oil and water to enter the liquid collecting tank 8 through the liquid outlet 20 on the bottom of the recovery tank 19. For every 1kg of oily sludge treated, about 0.05L of water and 0.07L of oil resources can be recovered through the capillary channels in the second chamber 18; since most of the free water and oil have been separated in the first chamber 2, the second chamber 18 only needs to recover the water and oil with low recovery efficiency due to micro-pressure difference caused by capillary adsorption between solid phases through the extrusion device, which greatly shortens the residence time of the oily sludge in the second chamber 18, and the residence time of the oily sludge in the second chamber 18 is controlled to be 0.5h;

[0300] S4: Discharging

[0301] After further deep recovery of water and oil products in the second chamber 18, the oily sludge reduction rate reached 93%, and the solid material discharged through the discharge port 4 had a water content of 12%, a solid content of 74%, and an oil content of 14%. The flue gas and the gas generated during the reaction were discharged through the gas outlet 16. The temperature of the discharged gas was 168°C, the SO2 content was 212ppm, the CO2 content was 21.7%, the H2S content was 0.7ppm, and the VOCs content was 5ppm. The discharged gas returned to the factory flue gas treatment unit for purification.

[0302] Comparative Example 7

[0303] The device with the same structure as Example 8A is used, but the waste flue gas from the factory is not used. For every 1kg of oily sludge treated, about 0.12L of water is recovered, about 0.36L of oil products are recovered, the water content of the output solid material is 27%, the solid content is 40%, the oil content is 33%, and the oily sludge reduction rate is 48%. The treatment effect of the oily sludge deteriorates, which is less than the 77% reduction rate of Example 8A, and the oil and water recovery is reduced. In Comparative Example 7, the residence time of the oily sludge in the first chamber and the second chamber is regulated, and the oil and water recovery in the first chamber and the second chamber are kept the same as in Example 8A. The residence time of the oily sludge in the first chamber in Comparative Example 7 is 2.1h, and the residence time in the second chamber is 1.1h. The overall treatment time of Comparative Example 7 is 3.2h, which is 45% longer than the overall treatment time of 2.2h in Example 8A, and the treatment efficiency is significantly reduced.

[0304] Comparative Example 8 uses a device with the same structure as Example 8A, but does not provide a scraper plate 24 or a scraper rod 23. For every 1 kg of oily sludge treated, about 0.16 L of water is recovered, about 0.44 L of oil products are recovered, the water content of the output solid material is 25%, the solid content is 53%, the oil content is 23%, and the oily sludge reduction rate is 60%. The treatment effect of the oily sludge deteriorates, which is less than the 77% reduction rate of Example 8A, and the oil and water recovery is reduced. In Comparative Example 7, the residence time of the oily sludge in the first chamber and the second chamber is regulated, and the oil and water recovery in the first chamber and the second chamber are kept the same as in Example 8A. In Comparative Example 7, the residence time of the oily sludge in the first chamber is 3.5 h, and the residence time in the second chamber is 0.2 h. The overall treatment time of Comparative Example 7 is 3.7 h, which is 68% longer than the overall treatment time of 2.2 h in Example 8A, and the treatment efficiency is significantly reduced.

[0305] Examples 8C-8S

[0306] The device with the same structure as that of Example 8A was used, but the waste flue gas feed amount was different, resulting in a different ratio of oily sludge to flue gas in the first chamber 2. The waste flue gas feed amount was adjusted, and the corresponding oily sludge parameters were shown in Table 8 below;

[0307] Table 8

[0308]

[0309]

[0310] The treated oily sludge has a water content of 26%, a solid content of 21%, an oil content of 53%, and a density of 1.097 kg / L (1.1 kg / L in this embodiment). 3 / h (this range corresponds to the waste flue gas and oily sludge volume ratio range of 100:1 ~ 150:1), the temperature of the oily sludge after conditioning is in the range of 70-80℃, which is suitable for the added demulsifier to play a role, maintain the oily sludge demulsification effect, and the oily sludge reduction rate is more than 75%, especially when the waste flue gas feed amount is 2.4m 3 / h (the volume ratio of waste flue gas to oily sludge is 120:1), the effect is best, and the oily sludge can achieve a 78% reduction rate. 3 / h (the corresponding waste flue gas to oily sludge volume ratio range is 150:1 ~ 400:1), the oily sludge reduction efficiency is good, maintaining a reduction rate of more than 70%; when the waste flue gas feed rate is further increased, the waste flue gas feed rate is greater than 8m 3 / h (the corresponding waste flue gas to oily sludge volume ratio is higher than 400:1), the pH of the oily sludge after conditioning is too low and the temperature is too high, the demulsifier demulsification effect decreases, resulting in an oily sludge reduction rate of less than 70%. When the waste flue gas feed rate is 1-2m 3 / h (the corresponding waste flue gas to oily sludge volume ratio range is 50:1-100:1), the oily sludge reduction efficiency is good, maintaining a reduction rate of more than 70%; when the waste flue gas feed rate is further reduced, the waste flue gas feed rate is less than 1m 3 / h (at this time, the volume ratio of waste flue gas to oily sludge is less than 50:1), the temperature of the oily sludge after conditioning is too low and the pH is too high, and the demulsification effect of the demulsifier is significantly reduced, resulting in an oily sludge reduction rate of less than 70%.

[0311] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A device for reducing the amount of oily sludge, characterized in that: The device includes: A shell, wherein a first chamber is disposed inside the shell, a feed port and a discharge port communicating with the first chamber are disposed at two ends of the shell, a capillary channel communicating with the first chamber is opened on the side wall of the first chamber, and a heating component is disposed in the side wall of the first chamber; A stirring and conveying mechanism is arranged inside the shell and is used to stir and convey the material in the first chamber.

2. The oily sludge reduction treatment device according to claim 1 is characterized in that: A liquid collecting groove connected with the capillary channel is arranged on the outer side of the outer wall of the shell; and at least one liquid discharge port is arranged at the bottom of the liquid collecting groove.

3. The oily sludge reduction treatment device according to claim 1 is characterized in that: The pore size of the capillary channel is 1-5 microns.

4. The oily sludge reduction treatment device according to claim 1 is characterized in that: The pore size of the capillary channel is 0.05-3.5 microns.

5. The oily sludge reduction treatment device according to claim 1 is characterized in that: The pore size of the capillary channel is 0.02-0.3 microns.

6. The oily sludge reduction treatment device according to claim 1 is characterized in that: Relative to the total volume of the side wall of the first chamber, the volume of the capillary channel accounts for 0.2-6%.

7. The oily sludge reduction treatment device according to claim 6 is characterized in that: Relative to the total volume of the side wall of the first chamber, the volume of the capillary channel accounts for 0.2-2%.

8. The oily sludge reduction treatment device according to claim 6 is characterized in that: Relative to the total volume of the side wall of the first chamber, the volume of the capillary channel accounts for 1-5%.

9. The oily sludge reduction treatment device according to claim 1, characterized in that: The stirring and conveying mechanism comprises a rotating shaft, which is rotatably arranged in the first chamber, one end of the rotating shaft is connected to a driving motor, and the outer periphery of the rotating shaft is provided with stirring and conveying blades.

10. The oily sludge reduction treatment device according to claim 1, characterized in that: It also includes an air intake structure, the output end of which is in communication with the first chamber and is used to transport acidic gas into the first chamber.

11. The oily sludge reduction treatment device according to claim 10, characterized in that: The air intake structure includes an air intake box, the air intake port of the air intake box is used to communicate with the waste smoke pipeline in the factory area, and the multiple air distribution ports of the air intake box are connected to the first chamber.

12. The oily sludge reduction treatment device according to claim 2, characterized in that: The liquid collecting tank is connected to a negative pressure generating structure, and the negative pressure generating structure is used to form a negative pressure environment in the liquid collecting tank.

13. The oily sludge reduction treatment device according to any one of claims 1 to 12, characterized in that: A second chamber connected to the first chamber is provided inside the shell, the second chamber is provided at one end of the first chamber close to the discharge port, and the second chamber tapers from one end away from the discharge port to one end close to the discharge port, a side wall of the second chamber is provided with an annular recovery groove with an open inner circumference, a liquid outlet hole is provided at the bottom of the recovery groove, and a filter plate is provided at the open end of the recovery groove.

14. The oily sludge reduction treatment device according to claim 13, characterized in that: The second chamber is provided with an extrusion mechanism, which includes a scraper rod rotatably arranged in the second chamber, the scraper rod rotates around the cross-sectional center of the second chamber in the cross-sectional area of ​​the second chamber, and a scraper plate is provided at the outer end of the scraper rod, and the scraper plate contacts the filter plate.

15. A method for reducing the amount of oily sludge, using the device for reducing the amount of oily sludge according to any one of claims 1 to 14, characterized in that: The method includes: Feeding the oily sludge and the optional demulsifier into the first chamber from the feed inlet; Heating, stirring and conveying the material in the first chamber; discharging at least part of the liquid generated in the first chamber through the capillary channel; The solid produced in the first chamber is discharged through the discharge port.

16. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The method also includes backwashing the capillary channels.

17. The method for reducing the amount of oily sludge according to claim 16, characterized in that: When a liquid collecting groove connected with the capillary pores is arranged on the outer side of the outer wall of the shell, and a liquid discharge port is arranged on the liquid collecting groove, the capillary pores are backwashed with gas or liquid through the liquid discharge port.

18. The method for reducing the amount of oily sludge according to claim 16, characterized in that: The oily sludge reduction treatment device backwashes the capillary channels once every 500-2000 hours of operation.

19. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The capillary channel is formed by stamping; or, the capillary channel is a capillary hole with a protective cover embedded during the equipment processing and molding; or, the side wall of the first chamber with the capillary channel is integrally formed using a channel model; or, the side wall of the first chamber with the capillary channel is manufactured by jet etching.

20. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The moisture content of the oily sludge is in the range of 10%-80%, preferably in the range of 10%-40%.

21. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The demulsifier is selected from at least one of sodium lignin sulfonate, ethylenediamine, propylene glycol, glycerol, nonylphenol polyoxyethylene ether, sodium dodecylbenzene sulfonate, and hexadecyltrimethylammonium bromide.

22. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The amount of the demulsifier added relative to the oily sludge is 0.5 to 10 g / L, preferably 1 to 8 g / L.

23. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The temperature in the first chamber is 30-100°C, preferably 60-90°C.

24. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The method further includes inputting acid gas into the first chamber so that the acid gas is mixed with the oily sludge.

25. The method for reducing the amount of oily sludge according to claim 24, characterized in that: The acid gas is an acid gas containing SO2 and CO2, wherein the content of SO2 is in the range of 100 to 3000 ppm, and the content of CO2 is in the range of 2% to 40%.

26. The method for reducing the amount of oily sludge according to claim 24, characterized in that: The acid gas is factory waste flue gas, and the temperature of the factory waste flue gas is 120-350°C, preferably 200-350°C.

27. The method for reducing the amount of oily sludge according to claim 26, characterized in that: The volume ratio of the factory waste flue gas input into the first chamber to the oily sludge is 50:1-400:1, preferably 100:1-150:

1.

28. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The residence time of the oily sludge in the first chamber is 0.5-8 hours, preferably 1-3 hours.

29. The method for reducing the amount of oily sludge according to claim 15, characterized in that: The method also includes providing a negative pressure environment at one end of the capillary channel away from the first chamber.

30. The method for reducing the amount of oily sludge according to claim 29, characterized in that: When a liquid collecting groove connected to the capillary channel is provided on the outer side of the outer wall of the shell, and a negative pressure tube is provided on the liquid collecting groove, the gas in the liquid collecting groove is extracted and injected into the shell, so that the pressure in the liquid collecting groove is 0.085-0.095MPa, and the pressure in the shell is 0.103-0.125MPa.

31. The method for reducing the amount of oily sludge according to claim 15, characterized in that: When a second chamber connected to the first chamber is provided inside the shell, the second chamber is provided at one end of the first chamber close to the discharge port, and the second chamber tapers from the end away from the discharge port to the end close to the discharge port, a side wall of the second chamber is provided with an annular recovery groove with an open inner circumference, a liquid outlet is provided at the bottom of the recovery groove, and a filter plate is provided at the open end of the recovery groove, it also includes: using the side wall of the second chamber to extrude the material in the second chamber, and performing solid-liquid separation of the material through the filter plate.

32. The method for reducing the amount of oily sludge according to claim 31, characterized in that: When an extrusion mechanism is provided in the second chamber, the extrusion mechanism includes a scraper rod rotatably provided in the second chamber, the scraper rod rotates around the cross-sectional center of the second chamber in the cross-sectional area of ​​the second chamber, and a scraper plate is provided at the outer end of the scraper rod. When the scraper plate contacts the filter plate, it also includes: the material in the second chamber is squeezed between the scraper plate and the filter plate through the extrusion mechanism.

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