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 fermentation cavity is formed in the shell, the two ends of the shell are provided with a feeding port and a discharging port respectively, the feeding port and the discharging port are communicated with the fermentation cavity, the side wall of the fermentation cavity is provided with capillary channels communicated with the fermentation cavity, and the capillary channels are communicated with the fermentation cavity; a heating part is arranged in the side wall of the fermentation chamber, and an air outlet is formed in the top of the fermentation chamber; the stirring and conveying mechanism is arranged in the shell and is used for stirring and conveying materials in the fermentation chamber; the problems of high solid-liquid separation difficulty, complicated operation, high cost and large occupied area in the reduction treatment process of the oily sludge in the prior art are solved.

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] Oil is an important resource and plays a supporting role in the development of the national economy. However, oily sludge is produced during the extraction, transportation and processing of oil. Oily sludge is an emulsified system composed of petroleum hydrocarbons, colloids, asphaltene, mud, sand, water and other organic and inorganic substances, and is classified as hazardous waste. The discharge of oily sludge will cause serious pollution to the soil, atmosphere and water bodies. Oily sludge contains valuable oil resources. Biological treatment of oily sludge and recovery of oil products are important means to protect the environment and achieve resource recovery.

[0003] At present, in order to achieve the purpose of treating pollutants and recovering oil resources, oily sludge treatment devices often require a combination of multiple equipment units, and use high-speed centrifugation as the main means for solid-liquid separation, which has the problems of high energy consumption and complex operation. How to achieve efficient treatment of oily sludge and recovery of high-purity oil products more simply and economically is an important measure to improve the treatment efficiency, effect and economy of oily sludge biological treatment devices.

[0004] Biological aerobic fermentation treatment of oily sludge is a low-cost, environmentally friendly method of treating oily sludge. Microorganisms use the oil in the oily sludge as a carbon source for degradation, destabilizing the oily sludge system and absorbing and degrading pollutants and a portion of oil and water. High-temperature microbial fermentation technology, in particular, has the advantages of short cycle and high efficiency, and can be used in conjunction with demulsifiers to achieve deep reduction treatment of oily sludge.

[0005] In view of the problems of complex operation, difficult oil recovery and high operating cost of existing oily sludge treatment equipment, the high-temperature biological aerobic fermentation coupled with demulsification technology is used to optimize the oily sludge treatment equipment, which can achieve low-cost recovery of high-quality oil products, improve the treatment efficiency of oily sludge and reduce treatment costs.

[0006] CN115504643A discloses a biological-physical combined method for efficiently treating oily sludge. The method proposes to use an air flotation device to form floating flocs containing pollutants and tiny bubbles, and then recover crude oil from the oily scum. Although the method achieves the separation of oil products, the separated oily scum contains a mixture of oil products and pollutants, resulting in low oil purity and increased separation difficulty, which increases the cost of oil recovery.

[0007] CN113816577A discloses a rotary microbial fermentation device for treating oily sludge. The device includes a supporting chassis, a reaction component and a rotating component, etc. The oily sludge is rolled by rotating the turntable, so that the oily sludge and the bacterial liquid are fully mixed, thereby enhancing the fermentation process. However, the oil products cannot be recovered after the oily sludge is treated, and the economic efficiency of the device needs to be further improved.

[0008] 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

[0009] 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.

[0010] In order to achieve the above object, the present invention provides an oily sludge reduction treatment device, which comprises:

[0011] A shell, wherein a fermentation chamber is disposed inside the shell, a feed port and a discharge port connected to the fermentation chamber are disposed at both ends of the shell, a capillary channel connected to the fermentation chamber is opened on the side wall of the fermentation chamber, a heating component is disposed inside the side wall of the fermentation chamber, and an air outlet is disposed on the top of the fermentation chamber;

[0012] A stirring and conveying mechanism is arranged inside the shell and is used for stirring and conveying materials in the fermentation chamber.

[0013] Oily sludge, demulsifier and biological bacteria liquid with the function of fermenting oily sludge can enter the fermentation chamber through the feed port. Under the action of the heating component, the temperature in the fermentation chamber increases, and the oily sludge ferments in the fermentation chamber to produce oil-water mixed liquid, gas and solid products. Under the action of the stirring and conveying mechanism, the material is turned over and transmitted in the direction of the discharge port. The liquid can be collected under the absorption of the capillary pores, and the gas can be discharged through the gas outlet.

[0014] Optionally, a liquid collecting groove connected with the capillary channel is arranged on the outer side of the outer wall of the shell, and a liquid drain port is arranged at the bottom of the liquid collecting groove.

[0015] The liquid collecting tank is used to collect the liquid discharged through the capillary channel, and the liquid collected in the liquid collecting tank can be discharged through the liquid discharge port so as to perform oil-water separation in the next step.

[0016] Optionally, an oil-water separation structure is further included, and the oil-water separation structure is connected to the liquid discharge port through an infusion pipeline.

[0017] The liquid collected in the sump can be separated in the oil-water separation structure, the separated oil can be recycled and reused, and the separated water can be input into the plant wastewater treatment unit for treatment.

[0018] Optionally, the oil-water separation structure comprises:

[0019] An oil-water separation tank, wherein a partition is vertically arranged inside the oil-water separation tank, and the partition divides the inside of the oil-water separation tank into a first space and a second space connected at the bottom;

[0020] An oil storage tank, wherein the oil storage tank is arranged below the oil-water separation tank;

[0021] A floating plate, the floating plate is movably arranged in the second space, the floating plate can float on the oil-water interface, a first limiting portion and a second limiting portion connected to the inner wall of the oil-water separation tank are respectively arranged above and below the floating plate, and the floating plate is provided with a plurality of oil passage ports;

[0022] A hollow fiber bundle, wherein the upper end of the hollow fiber bundle penetrates the floating plate and forms an extension portion above the floating plate, the lower end of the hollow fiber bundle extends into the oil storage tank, and a capillary channel is formed in the hollow fiber bundle;

[0023] A sealing portion is provided between the oil-water separation tank and the oil storage tank so that the oil-water separation tank is communicated with the oil storage tank only through the capillary channel.

[0024] Specifically, the liquid collected in the liquid collecting tank is transported to the first space through the infusion pipeline, and after passing through the first space, enters the second space from the bottom of the oil-water separation tank. As the input amount of the liquid increases, the liquid level in the oil-water separation tank increases, and the water and oil are separated into layers, with the oil above the water. The floating plate in the second space floats on the interface between the oil and water, and the capillary channel formed by the hollow fiber bundle on the floating plate can guide the oil on the upper side into the oil storage tank below the oil-water separation tank, while the water in the oil-water separation tank remains in the second space, thereby achieving oil-water separation.

[0025] In a specific embodiment of the present invention, a plurality of hollow capillary fibers form a capillary fiber bundle, and a capillary channel is disposed in each hollow fiber.

[0026] In another specific embodiment of the present invention, a plurality of hollow capillary fibers form a capillary fiber bundle. Not only is a capillary channel provided in each hollow fiber, but capillary channels are also formed between adjacent capillary fiber bundles. Since the cross-section of the capillary channels formed between adjacent capillary fiber bundles is not circular, the diameter of the capillary channel can be characterized by the average pore size.

[0027] Optionally, an oil drain port is provided at the lower end of the side wall of the oil storage tank, an oil drain valve is provided in the oil drain port, a water drain port is provided at the lower end of the side wall of the oil-water separation tank, a water drain valve is provided in the water drain port, a liquid level gauge is provided in the oil storage tank, and a first position sensor and a second position sensor are respectively provided on the side where the first limit part and the second limit part are close to each other.

[0028] The first limit part and the second limit part limit the position of the float so that the float is between the two. When the float rises to contact the first limit part, the first position sensor is triggered. At this time, the drain valve needs to be opened to discharge some water. When the float drops to contact the second limit part, the second position sensor is triggered. At this time, the input amount of liquid in the liquid collecting tank to the oil-water separation tank needs to be increased. When the liquid level detected by the liquid level meter exceeds the set liquid level height, the oil drain valve needs to be opened to recover and discharge the oil in the oil storage tank.

[0029] The first position sensor and the second position sensor may be a distance sensor, a photoelectric sensor or a position switch.

[0030] Optionally, the density of the floating disk is 0.850-0.950 g / cm 3 .

[0031] The density of the floating disc ensures that it can float at the oil-water interface.

[0032] Optionally, the pore size of the capillary channel is 0.05-4 microns.

[0033] Optionally, a hydrophobic coating is provided on the inner wall of the capillary channel, and the water drop contact angle of the hydrophobic coating is 95-140°.

[0034] The inner wall of the capillary channel in the hollow fiber bundle is coated with a hydrophobic coating, which can accelerate the self-absorption of oil and improve the oil-water separation efficiency.

[0035] Optionally, the pore size of the capillary channel is 0.01-2 microns.

[0036] 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.

[0037] Optionally, relative to the total volume of the side wall of the fermentation chamber, the volume of the capillary channel accounts for 0.5-4%, preferably 2%.

[0038] 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).

[0039] The preferred pore size combined with the preferred volume ratio can achieve a better oil-water separation effect.

[0040] Optionally, the stirring and conveying mechanism comprises a rotating shaft, which is rotatably arranged in the fermentation 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.

[0041] The rotating shaft can be set horizontally or tilted.

[0042] Optionally, the driving motor is a variable frequency motor.

[0043] The output power of the variable frequency motor is adjustable, and the residence time of the oily sludge in the fermentation chamber can be controlled to be 6 to 24 hours, preferably 12 hours, through the rotation speed of the stirring and conveying mechanism; the stirring and conveying mechanism can be divided into three sections of variable frequency output power, namely front, middle and rear, to control the oily sludge to be conveyed at different speeds in the front, middle and rear parts of the fermentation chamber.

[0044] Optionally, an air intake structure is further included, wherein the output end of the air intake structure is connected to the fermentation chamber and is used to transport acidic gas and oxygen into the fermentation chamber.

[0045] The acidic gas reacts with the oily sludge, lowering the pH of the oily sludge, which is beneficial to the demulsification process of the oily sludge, reducing the stability of the emulsification system, and reducing the viscosity of the oily sludge. Oxygen provides oxygen for the fermentation of the oily sludge and promotes the fermentation.

[0046] According to a preferred embodiment of the present invention, the air intake structure delivers dust-removed SO2, CO2, NO x Waste gas from factory areas containing acidic gases such as chlorinated hydrocarbons and oxygen.

[0047] Optionally, the air intake structure comprises:

[0048] An air intake passage, the air intake passage being arranged inside the rotating shaft along the axial direction of the rotating shaft;

[0049] a plurality of air distribution ports, the plurality of air distribution ports being arranged on the rotating shaft along the axial direction of the rotating shaft and connecting the air inlet channel with the fermentation chamber;

[0050] An air inlet is arranged at one end of the rotating shaft close to the driving motor.

[0051] The waste flue gas from the factory enters the air inlet channel through the air inlet, is transported along the air inlet channel and discharged into the fermentation chamber through multiple air distribution ports on the rotating shaft. The waste flue gas from the factory is distributed from the air distribution ports on the rotating shaft. The air distribution position is close to the center of the fermentation chamber and close to the stirring position of the stirring blade conveying impeller, which can make the gas better mixed with the oily sludge; at the same time, the introduction of the waste flue gas from the factory forms a micro-positive pressure environment in the fermentation chamber, which can promote the capillary pores to absorb and recover oil and water liquids.

[0052] Optionally, an opening regulating valve is provided in each of the air distribution ports.

[0053] The air distribution ports can be evenly distributed on the rotating shaft at equal intervals, but the opening regulating valve arranged on each air distribution port can adjust the air distribution volume at each position by adjusting the opening of the air distribution port. Good air distribution volume distribution can form good oxygen content distribution and improve the fermentation effect.

[0054] Optionally, three oxygen content detection instruments are sequentially arranged in the fermentation chamber along the conveying direction of the material, and the three oxygen content detection instruments are used to detect the oxygen concentration in the front, middle and rear parts of the fermentation chamber respectively.

[0055] The three oxygen content detection instruments respectively located at the front, middle and back positions in the fermentation chamber can detect the distribution of oxygen in the fermentation chamber, so as to facilitate its regulation.

[0056] Optionally, a plurality of temperature detection components are sequentially arranged in the fermentation chamber along the conveying direction of the material, and the plurality of temperature detection components are used to detect the temperatures at a plurality of positions in the fermentation chamber.

[0057] The setting of multiple temperature detection components can obtain the temperature conditions at different positions in the fermentation chamber through temperature measurement, which is convenient for regulation. The front part is high-temperature demulsification with a relatively high temperature, and the middle and rear parts are fermented with a relatively low temperature, avoiding excessively high temperature from destroying the activity of the biological bacteria liquid.

[0058] Optionally, the heating component is a segmented variable frequency heating rod arranged along the axial direction of the fermentation chamber, which can heat the material in the fermentation chamber in segments.

[0059] The fermentation chamber is heated in sections by means of the sectioned variable frequency heating rod, and the temperature distribution in the fermentation chamber can be regulated according to the detection result of the temperature detection component.

[0060] 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.

[0061] Specifically, the negative pressure generating structure is connected to the liquid collecting tank through a negative pressure pipe. The negative pressure pipe can be equipped with an air pump to maintain a micro-negative pressure environment in the liquid collecting tank and strengthen the capillary pores to absorb oil and water liquids into the liquid collecting tank.

[0062] Optionally, the discharge port is connected to a material reflux pipe, a variable frequency reflux pump is provided on the material reflux pipe, and the material reflux pipe is connected to the feed port.

[0063] The material reflux pipe is equipped with a variable frequency reflux pump, which can adjust the reflux ratio of the solid product after fermentation.

[0064] 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:

[0065] The oily sludge, demulsifier and biological bacteria liquid capable of fermenting the oily sludge are fed into the fermentation chamber through the feed inlet;

[0066] Heating, stirring and conveying the materials in the fermentation chamber;

[0067] discharging at least a portion of the liquid produced in the fermentation chamber through the capillary channel;

[0068] discharging at least part of the gas generated in the fermentation chamber through the gas outlet;

[0069] The solid product produced in the fermentation chamber is discharged through the discharge port.

[0070] According to a specific embodiment of the present invention, the biological bacterial liquid with the function of fermenting oily sludge is sampled from at least one of oilfield soil, oily sludge in a storage tank and oily wastewater, cultured, enriched and screened at high temperature (70-80°C) in a sterilized crude oil culture medium, and is a bacterial liquid containing at least one of Streptococcus sp., Micrococcus cohnsp. and Planococcus migula sp.

[0071] Optionally, the water content of the oily sludge is higher than 35%, the oil content of the oily sludge is higher than 35%, and the total liquid content of the oily sludge is higher than 80%.

[0072] The water content of the oily sludge is higher than 35%, which ensures that sufficient water is supplied for the growth and fermentation of microorganisms. The oil content of the oily sludge is higher than 35%, which ensures that sufficient oil is provided as a carbon source for the microorganisms.

[0073] Optionally, the method further comprises inputting fermentation-promoting substances into the fermentation chamber through a feed inlet.

[0074] The fermentation effect of microorganisms in the fermentation chamber is enhanced by fermentation-promoting substances.

[0075] Optionally, the fermentation-promoting substance is selected from at least one of sawdust, cow dung and rice straw.

[0076] Optionally, the demulsifier is selected from at least one of sodium lignin sulfonate, tetrasodium ethylenediaminetetraacetate, ethylenediamine, polyquaternary ammonium salt, polyether polyquaternary ammonium salt, glycerol, nonylphenol polyoxyethylene ether, polyacrylate, sodium dodecylbenzene sulfonate, and hexadecyltrimethylammonium bromide.

[0077] Optionally, the demulsifier is added in an amount of 0.5 to 6 g / L relative to the oily sludge.

[0078] The moisture content is adjusted according to the water content and properties of the oily sludge being treated, preferably 2.5 g / L.

[0079] Optionally, the survival temperature of the biological bacterial liquid is 35-95°C, the use temperature of the biological bacterial liquid is 60-80°C, and the preferred use temperature is 70-75°C.

[0080] Optionally, the method further comprises inputting acidic gas and oxygen into the fermentation chamber so that the acidic gas and the oxygen are mixed with the oily sludge.

[0081] Optionally, the acid gas is an acid gas containing SO2, wherein the content of SO2 is in the range of 100-1000 ppm; and the content of oxygen is in the range of 6-20%.

[0082] Optionally, the acid gas and the oxygen are provided by waste flue gas from a factory, and the temperature of the waste flue gas from a factory is 120-300°C, preferably 150-200°C.

[0083] The factory waste gas can be used to provide heat for the fermentation chamber.

[0084] The waste gas generated during the fermentation process enters the factory flue gas purification unit together with the factory waste flue gas through the outlet. The device has no waste gas emissions and can achieve coordinated purification of the factory waste flue gas. The desulfurization rate of the factory waste flue gas can reach 5-50%.

[0085] Optionally, when the biological bacterial liquid having the function of fermenting oily sludge is input into the fermentation chamber from the feed inlet, the process also includes inputting the biological bacterial liquid having the function of degrading H2S gas into the fermentation chamber.

[0086] The biological bacterial liquid includes both the biological bacterial liquid with the function of fermenting oily sludge and the biological bacterial liquid with the function of degrading H2S gas. Therefore, it has both the function of fermenting oily sludge and the function of degrading H2S gas, and can purify the waste flue gas in the factory area.

[0087] According to a specific embodiment of the present invention, the biological bacterial liquid with the function of degrading H2S gas is sampled from at least one of kitchen waste, mineral soil and activated sludge, cultured at high temperature, enriched and screened in a sterilized crude oil culture medium with an H2S atmosphere, and is a bacterial liquid containing at least one of Dietzia sp., Enterobacteriaceae sp. and Lysinibacillus sp.

[0088] Optionally, the volume ratio of the factory waste flue gas input into the fermentation chamber to the oily sludge is 1:1-500:1, preferably 80:1.

[0089] Adjust the appropriate amount of waste gas added from the plant to ensure that the waste gas generated by demulsification and fermentation of the oily sludge can be completely carried out of the outlet, and control the heat of heat exchange between the waste gas and the oily sludge to avoid inactivation of fermentation microorganisms due to excessive temperature, and promote the water generated after demulsification and fermentation to be carried away from the fermentation chamber by the waste gas from the plant in the form of water vapor, thereby improving the purity of oil recovery.

[0090] Optionally, the temperature of the oily sludge in the fermentation chamber is 50-85°C, preferably 70-75°C.

[0091] The heating inside the fermentation chamber is accomplished by the heating components and the waste flue gas from the factory.

[0092] Optionally, the oxygen concentration in the front portion of the fermentation chamber is greater than 15%, and the oxygen concentration in the middle and rear portions of the fermentation chamber is less than 10%.

[0093] Optionally, the residence time of the oily sludge in the fermentation chamber is 6-24 hours, preferably 12 hours.

[0094] Optionally, the method further comprises providing a negative pressure environment at one end of the capillary channel away from the fermentation chamber.

[0095] Optionally, part of the solid product is returned to the fermentation chamber, and the ratio of the flow rate of the solid product returned to the fermentation chamber to the flow rate of the oily sludge input into the fermentation chamber is 1:5-1:50, preferably 1:20.

[0096] Optionally, when a liquid collecting tank 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 tank, the gas in the liquid collecting tank is extracted so that the pressure in the liquid collecting tank is 0.085~0.095MPa, and the pressure in the shell is 0.105~0.13MPa.

[0097] Optionally, the method further includes separating oil and water from the derived liquid.

[0098] Optionally, the biological bacterial liquid capable of fermenting oily sludge includes at least one of the genera Streptococcus, Micrococcus and Moinecoccus.

[0099] Optionally, the concentration of the biological bacterial solution capable of fermenting oily sludge is higher than 5×10 7 / mL, and the added amount of the biological bacteria liquid with the function of fermenting oily sludge is 2-30kg.

[0100] Optionally, the biological bacterial liquid capable of degrading H2S gas includes at least one of the genera Dietzia, Enterobacter, and Lysinibacillus.

[0101] Optionally, the concentration of the biological bacterial solution capable of degrading H2S gas is higher than 10 8 / mL, and the added amount of the biological bacterial liquid with the function of degrading H2S gas is 0.1-3kg.

[0102] According to a specific embodiment of the present invention, the biological bacterial liquid includes a biological bacterial liquid with a function of fermenting oily sludge and a biological bacterial liquid with a function of degrading H2S gas. The weight ratio of the biological bacterial liquid with a function of fermenting oily sludge to the biological bacterial liquid with a function of degrading H2S gas in the biological bacterial liquid is in a range of 5:1-30:1.

[0103] According to a specific embodiment of the present invention, the method for reducing the amount of oily sludge comprises the following steps:

[0104] S1: Feed

[0105] The oily sludge to be treated is mixed with a certain proportion of demulsifier and then fed into the fermentation chamber in the shell through the feed port. The waste flue gas from the plant area after dust removal treatment enters the fermentation chamber through the air inlet, the air inlet channel and the air distribution port. When the device is started for the first time, a certain proportion of biological bacterial liquid with the function of fermenting oily sludge and biological bacterial liquid with the function of degrading H2S gas are mixed into the oily sludge through the feed port.

[0106] S2: Fermentation

[0107] In the fermentation chamber, the oily sludge is stirred and turned by the stirring and conveying mechanism, and the gas distribution port evenly mixes the waste gas from the plant area with the oily sludge to achieve oxygen and heat supply. At the same time, the oily sludge in the fermentation chamber is heated by the heating component to keep the oily sludge at high temperature for biological fermentation. Under the impetus of the stirring and conveying mechanism, the oily sludge is continuously turned in the fermentation chamber and transported in the direction of the discharge port;

[0108] S3: Discharging

[0109] The oily sludge after demulsification and biological fermentation is transported to the discharge port under the stirring and pushing of the stirring and conveying mechanism, and then discharged from the fermentation chamber. The solid product flows back to the feed port in a certain proportion to mix with the oily sludge to be treated and enter the fermentation chamber together. The factory waste gas in the fermentation chamber is discharged from the fermentation chamber through the gas outlet and transported to the factory waste gas treatment unit.

[0110] S4: Separation and recovery

[0111] After demulsification and biological fermentation, water and oil are self-sucked into the liquid collecting tank through capillaries at the bottom of the fermentation chamber, and further enter the oil-water separation tank. The partition is used to ensure that the oil and water enter from the bottom of the oil-water separation tank, and the oil is separated into the oil storage tank through a floating plate with a hollow fiber bundle. The oil is regularly collected through the oil discharge port for reuse, and the water is regularly transported to the factory wastewater treatment unit through the drain port for treatment.

[0112] The method has the following technical advantages: (1) high-temperature demulsification and high-temperature microbial fermentation are combined to achieve efficient treatment and reduction of oily sludge in the integrated structure of the device, thereby improving the treatment efficiency of oily sludge and reducing the treatment cost;

[0113] (2) The waste heat resources of the factory waste gas are utilized to purify SO2 in the waste gas. At the same time, the waste gas generated during the biological fermentation of oily sludge is diluted and purged. The biological bacteria liquid with the function of degrading H2S gas is used to degrade H2S generated during the fermentation of oily sludge, thereby eliminating the pollution of waste gas during the biological treatment of oily sludge and improving the environmental benefits of the device.

[0114] (3) The introduction of waste flue gas from the plant area and the setting of the negative pressure generating structure promote the self-priming separation of the solid phase residue and the liquid phase oil and water after the fermentation of the oily sludge through the capillary channels by constructing a micro-pressure difference, thereby achieving simple operation and low-cost solid-liquid separation and improving the separation efficiency. The oil-water separation structure realizes efficient and low-cost oil-water separation through the hollow fiber bundle, realizes the recovery of high-quality oil products, and improves the economic benefits of the device;

[0115] (4) During the process of reducing the amount of oily sludge, the device can efficiently realize integrated demulsification and biological fermentation in stages through the setting of multiple temperature detection components and segmented variable frequency heating rods, and can be automatically controlled by a PLC control system, so that the device can be easily operated to recover high-quality oil resources, thereby improving the ease of operation of the device.

[0116] The present invention provides an oil-containing sludge reduction treatment device and method, and its beneficial effects are: the oil-containing sludge reduction treatment device is provided with a fermentation chamber in a shell, and a stirring and conveying mechanism is provided in the fermentation chamber. The oil-containing sludge, demulsifier and biological bacterial liquid with the function of fermenting the oil-containing sludge can be input into the fermentation chamber through a feed port, and a heating component heats them to provide a suitable fermentation temperature, so that the oil-containing sludge undergoes biological fermentation in the fermentation chamber and moves toward a discharge port under the stirring and conveying action of the stirring and conveying mechanism. The fermentation produces liquid, gas and solid products, the liquid being oil and water, which are absorbed and discharged in liquid form through capillary channels for collection, the solid products can be discharged through the discharge port for further deep treatment and resource utilization, and the gas includes waste gas and water vapor generated during the fermentation process, which are discharged through the gas outlet for further deep treatment, which can not only avoid gas Pollution can be eliminated and water vapor can be discharged in time to improve the purity of oil recovery. In a preferred embodiment, the factory waste gas including acidic gas and oxygen is input into the fermentation chamber through the air intake structure, and a biological bacterial liquid with the function of degrading H2S gas is added. The waste heat in the factory waste gas can be utilized to provide heat for the fermentation environment, save heating energy, and ensure the supply of oxygen. In addition, the factory waste gas can also have a certain desulfurization and purification effect during the fermentation process. In another preferred embodiment, the discharge port on the liquid collecting tank below the shell is also connected to an oil-water separation structure. The liquid in the liquid collecting tank enters the second space at the bottom of the oil-water separation tank after passing through the first space. The floating plate in the second space floats on the oil-water interface. The capillary channel formed by the hollow fiber bundle on the floating plate is used to introduce the upper layer of oil into the oil storage tank below the oil-water separation tank, so as to achieve oil-water separation and ensure the quality of the oil.

[0117] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0118] 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.

[0119] Figure 1 A schematic structural diagram of an oily sludge reduction treatment device according to Example 1 of the present invention is shown.

[0120] Figure 2 Show Figure 1 Schematic diagram of the cross-sectional structure.

[0121] Figure 3 A schematic diagram of the top view of the oil-water separation structure of an oily sludge reduction treatment device according to Example 1 of the present invention is shown.

[0122] Figure 4 A flow chart of a method for reducing the amount of oily sludge according to Example 2 of the present invention is shown.

[0123] Description of reference numerals:

[0124] 1. Shell; 2. Fermentation chamber; 3. Feed inlet; 4. Discharge outlet; 5. Capillary channel; 6. Heating component; 7. Air outlet; 8. Liquid collecting tank; 9. Heat conducting layer; 10. Infusion pipeline; 11. Oil-water separation tank; 12. Partition; 13. Oil storage tank; 14. Float; 15. First limiting part; 16. Second limiting part; 17. Oil passing port; 18. Hollow fiber bundle; 19. Sealing part; 20. Oil discharge port; 21. Oil discharge valve; 22. Drain port; 23. Drain valve; 24. Liquid level gauge; 25. Rotating shaft; 26. Driving motor; 27. Stirring and conveying blades; 28. Sealing component; 29. ​​Air inlet channel; 30. Air inlet; 31. Negative pressure pipe; 32. Material reflux pipe; 33. Exhaust valve; 34. Air distribution port. DETAILED DESCRIPTION

[0125] 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.

[0126] Example 1

[0127] like Figures 1 to 3 As shown, this embodiment provides an oily sludge reduction treatment device, the device comprising:

[0128] A housing 1, wherein a fermentation chamber 2 is disposed inside the housing 1, a feed port 3 and a discharge port 4 communicating with the fermentation chamber 2 are disposed at both ends of the housing 1, a capillary channel 5 communicating with the fermentation chamber 2 is opened on the side wall of the fermentation chamber 2, a heating component 6 is disposed inside the side wall of the fermentation chamber 2, and an air outlet 7 is disposed on the top of the fermentation chamber 2;

[0129] The stirring and conveying mechanism is arranged inside the shell 1 and is used for stirring and conveying the materials in the fermentation chamber 2 .

[0130] A liquid collecting tank 8 connected to the capillary channel 5 is arranged 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 produced by fermentation in the oil-containing sludge reduction treatment device can be discharged from the first chamber to the liquid collecting tank 8 through the capillary channel 5; a liquid discharge port is arranged at the bottom of the liquid collecting tank 8 to realize liquid discharge, maintain sufficient space in the liquid collecting tank 8, promote the absorption of oil and water by the capillary channel 5, and discharge the liquid into the oil-water separation structure to further separate the oil and water.

[0131] In this embodiment, if Figure 2 As shown, a heat-conducting layer 9 is provided on the inner wall of the shell 1, and the heating component 6 is inserted into the heat-conducting layer 9. The heat-conducting layer 9 can improve the thermal conductivity and the heating efficiency. In the present embodiment, the heat-conducting layer 9 includes 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 channel 5 is opened on the inner shell, and the outer shell is provided with a through hole at the corresponding position and the through hole is connected to the inner shell around the through hole through a cylinder, so that the liquid discharged through the capillary channel 5 can flow out.

[0132] In this embodiment, an exhaust valve 33 is provided on the air outlet 7 .

[0133] It also includes an oil-water separation structure, which is connected to the discharge port through the infusion pipeline 10.

[0134] The oil-water separation structure includes:

[0135] An oil-water separation tank 11, wherein a partition 12 is vertically arranged inside the oil-water separation tank 11, and the partition 12 divides the inside of the oil-water separation tank 11 into a first space and a second space which are connected at the bottom;

[0136] An oil storage tank 13, which is arranged below the oil-water separation tank 11;

[0137] The floating plate 14 is movably arranged in the second space. The floating plate 14 can float on the oil-water interface. The upper and lower parts of the floating plate 14 are respectively provided with a first limiting part 15 and a second limiting part 16 connected to the inner wall of the oil-water separation tank 11. The floating plate 14 is provided with a plurality of oil passing ports 17.

[0138] A hollow fiber bundle 18, wherein the upper end of the hollow fiber bundle 18 penetrates the floating plate 14 and forms an extension portion above the floating plate 14, and the lower end of the hollow fiber bundle 18 extends into the oil storage tank 13, and a capillary channel is formed in the hollow fiber bundle 18;

[0139] The sealing part 19 is disposed between the oil-water separation tank 11 and the oil storage tank 13 so that the oil-water separation tank 11 is connected to the oil storage tank 13 only through a capillary channel.

[0140] In this embodiment, if Figure 3 As shown, four oil passages 17 are provided to ensure that the oil flows from the lower part of the floating plate 14 to the upper part of the floating plate 14 through the oil passages 17, and ensure that the floating plate 14 floats smoothly on the interface between water and oil; the first limiting portion 15 and the second limiting portion 16 are structures protruding inward from the inner wall of the oil-water separation tank 11, so that the floating plate 14 can only move up and down between the two.

[0141] An oil drain port 20 is provided at the lower end of the side wall of the oil storage tank 13, and an oil drain valve 21 is provided in the oil drain port 20. A water drain port 22 is provided at the lower end of the side wall of the oil-water separation tank 11, and a water drain valve 23 is provided in the water drain port 22. A liquid level gauge 24 is provided in the oil storage tank 13, and a first position sensor and a second position sensor are respectively provided on the side where the first limit portion 15 and the second limit portion 16 are close to each other.

[0142] In this embodiment, a control system is also included. The control system adopts PLC. When the float 14 rises to contact the first limit part 15, the first position sensor is triggered. At this time, the drain valve 23 needs to be opened to discharge part of the water. When the float 14 drops to contact the second limit part 16, the second position sensor is triggered. At this time, it is necessary to increase the input amount of liquid in the collecting tank 8 to the oil-water separation tank 11. Then, the opening of the flow valve on the infusion pipeline 10 can be controlled. When the liquid level detected by the liquid level meter 24 exceeds the set liquid level height, the oil drain valve 21 needs to be opened to recover and discharge the oil in the oil storage tank 13. The PLC automatically controls the above process.

[0143] The density of the floating disk 14 is 0.850-0.950 g / cm 3 .

[0144] The pore size of the capillary channel is 0.05-4 microns.

[0145] A hydrophobic coating is arranged on the inner wall of the capillary channel, and the water drop contact angle of the hydrophobic coating is 95-140°.

[0146] The pore size of the capillary channel 5 is 0.01-2 microns.

[0147] Relative to the total volume of the side wall of the fermentation chamber 2 , the volume of the capillary channel 5 accounts for 0.5-4%.

[0148] The stirring and conveying mechanism comprises a rotating shaft 25 , which is rotatably disposed in the fermentation chamber 2 , one end of the rotating shaft 25 is connected to a driving motor 26 , and a stirring and conveying blade 27 is disposed on the periphery of the rotating shaft 25 .

[0149] The stirring and conveying mechanism drives the rotating shaft 25 through the driving motor 26 to drive the stirring and conveying blades 27 to rotate. The stirring and conveying blades 27 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 27 can adopt auger blades, and the residence time of the oily sludge in the first chamber can be controlled by controlling the rotation speed of the rotating shaft 25 and the shape of the stirring and conveying blades 27.

[0150] One end of the rotating shaft 25 passes through the side wall of the housing 1 and is connected to a driving motor 26 outside the housing 1 . A sealing component 28 connected to the housing 1 is disposed on the outer periphery of the rotating shaft 25 .

[0151] The driving motor 26 is a variable frequency motor.

[0152] It also includes an air intake structure, the output end of which is connected to the fermentation chamber 2 and is used to transport acidic gas and oxygen into the fermentation chamber 2.

[0153] The air intake structure includes:

[0154] An air inlet passage 29, the air inlet passage 29 is arranged inside the rotating shaft 25 along the axial direction of the rotating shaft 25;

[0155] A plurality of air distribution ports 34 are provided on the rotating shaft 25 along the axial direction of the rotating shaft 25 and connect the air inlet channel 29 with the fermentation chamber 2;

[0156] The air inlet 30 is disposed at one end of the rotating shaft 25 close to the driving motor 26 .

[0157] Each air distribution port 34 is provided with an opening regulating valve.

[0158] In this embodiment, the opening regulating valve is connected to the PLC to achieve automatic regulation.

[0159] Three oxygen content detection instruments are sequentially arranged in the fermentation chamber 2 along the material conveying direction. The three oxygen content detection instruments are used to detect the oxygen concentration in the front, middle and rear parts of the fermentation chamber 2 respectively.

[0160] A plurality of temperature detection components are sequentially arranged in the fermentation chamber 2 along the conveying direction of the material, and the plurality of temperature detection components are used to detect the temperature at a plurality of positions in the fermentation chamber 2 .

[0161] The heating component 6 is a segmented variable frequency heating rod arranged along the axial direction of the fermentation chamber 2 , and can heat the material in the fermentation chamber 2 in segments.

[0162] 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 .

[0163] In this embodiment, the negative pressure generating structure includes a negative pressure tube 31 , on which an air pump is provided, and the negative pressure tube 31 is connected to the infusion pipeline 10 .

[0164] The discharge port 4 is connected to a material reflux pipe 32 , a variable frequency reflux pump is provided on the material reflux pipe 32 , and the material reflux pipe 32 is connected to the feed port 3 .

[0165] Examples 2A-2H and Comparative Example 1

[0166] The oily sludge reduction treatment device of Example 1 is used to reduce the oily sludge, and the steps are as follows: Figure 4 shown.

[0167] Example 2A

[0168] The oily sludge to be treated has a water content of 40%, an oil content of 46%, a solid content of 14%, a total liquid content of 86%, a pH of 7.6, and a temperature of the waste gas in the plant area after dust removal treatment of 162°C, and a SO2 content of 236ppm; the treatment method is as follows:

[0169] S1: Feed

[0170] The oily sludge to be treated is added into the fermentation chamber 2 through the feed port 3 at a flow rate of 5 kg / h. When the device is started for the first time, 5 kg of biological bacterial solution is added at a flow rate of 0.5 kg / h. The biological bacterial solution includes a biological bacterial solution with the function of fermenting oily sludge and a biological bacterial solution with the function of degrading H2S gas. The weight ratio of the two is 9:1, and the concentrations of the two are higher than 5*10 7 / mL and 10 8 / mL, the fermentation-promoting substance is sawdust, which is added into the fermentation chamber 2 through the feed port 3 at a flow rate of 0.3kg / h, the demulsifier is polyether polyquaternary ammonium salt and sodium dodecylbenzene sulfonate, the ratio is 2:1, and the addition flow rate is 2.2g demulsifier per liter of oily sludge, and the waste gas in the plant is 0.6m 3 / h flow rate is input into the fermentation chamber 2 through the air inlet 30;

[0171] S2: Fermentation

[0172] In the fermentation chamber 2, the material in the fermentation chamber 2 is heated by the heating component 6 and the waste flue gas from the factory area, and the two temperature detection positions at the front of the fermentation chamber 2 are maintained at 85°C, and the other four temperature detection positions in the rear fermentation chamber 2 are maintained at 72°C. The PLC control system controls the opening of the opening regulating valve on the air distribution port 34, and controls the detection results of the oxygen content detection instrument at the front, middle and rear of the fermentation chamber 2 to be 8%, 17% and 9% respectively. Driven by the stirring and conveying mechanism, the solid material continues to move from front to back in the fermentation chamber 2, and completes the heating and demulsification link in the high-temperature and low-oxygen area, which lasts for 2 hours, and completes the biological fermentation link in the subsequent medium-high-temperature and high-oxygen area and the medium-high-temperature and low-oxygen area, which lasts for 8 hours;

[0173] S3: Discharging

[0174] The treated solid product is discharged from the fermentation chamber 2 through the discharge port, and flows back to the feed port 3 at a flow rate of 0.26 kg / h through the material reflux pipe 32, and re-enters the fermentation chamber 2 together with the oily sludge to be treated. The waste gas generated by the fermentation in the fermentation chamber 2 is discharged from the factory waste flue gas through the outlet pipe on the outlet port 7 to the factory flue gas treatment unit for treatment. The solid product discharged from the fermentation chamber 2 has a moisture content of 18%, an oil content of 4%, a solid content of 78%, a reduction rate of 82%, a pH of 7.2, and a temperature of 134°C, a SO2 content of 122ppm, a H2S content of 12ppm, and a VOCs content of 33ppm.

[0175] S4: Separation and recovery

[0176] The waste flue gas from the factory enters the fermentation chamber 2 through the air distribution port 34 and provides a slight positive pressure of 0.116MPa. The negative pressure pipe 31 is evacuated by an air pump, so that the liquid collecting tank 8 presents a slight negative pressure of 0.091MPa. A capillary channel 5 is provided at the bottom of the fermentation chamber 2. The average pore size of the capillary channel 5 is 1.16 microns. The capillary channel 5 accounts for 2.1% of the volume of the bottom of the fermentation chamber 2. The self-priming recovery of the oily sludge demulsification and the oil-water mixture separated after fermentation enters the liquid collecting tank 8 through the slight pressure difference on both sides of the capillary channel 5. Most of the demulsified water is absorbed by microorganisms and evaporated at high temperature to form water vapor. The oil-water mixture in the liquid collecting tank 8 enters the oil-water separation tank 11 from the bottom through the partition 12. The density of the floating plate 14 in the oil-water separation tank 11 is 0.882g / cm 3The floating plate 14 floats at the oil-water interface. The floating plate 14 is provided with a capillary hollow fiber bundle 18, wherein the capillary channel pore size is 2.68 microns, and the capillary hollow fiber bundle 18 occupies 10% of the area of ​​the floating plate 14. In addition, there are 4 oil-passing ports 17 on the floating plate 14, which occupy 25% of the area of ​​the floating plate 14. The inner wall of the capillary channel in the capillary hollow fiber bundle 18 is coated with a hydrophobic coating, and the water drop contact angle is 106°. The extension of the hollow fiber bundle 18 is 16 mm higher than the upper surface of the floating plate 14, and is provided with The protective cover recycles the oil in the oil-water separation tank 11 to the oil storage tank 13 through the capillary hollow fiber bundle 18. The purity of the recovered oil is >99.75%. The liquid level meter 24 and the PLC system automatically control the oil drain valve 21 to discharge high-quality oil into the factory for reuse. When the float 14 reaches the first limit part 15 in the oil-water separation tank 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separation tank 11 into the factory wastewater treatment system for purification.

[0177] Example 2B

[0178] The oily sludge to be treated has a water content of 59%, an oil content of 36%, a solid content of 5%, a total liquid content of 95%, and a pH of 7.5. The temperature of the factory waste gas used by the device is 183°C and the SO2 content is 238ppm. The treatment method is as follows:

[0179] S1: Feed

[0180] The oily sludge to be treated is added to the fermentation chamber 2 through the feed port 3 at a flow rate of 30 kg / h. When the device is started for the first time, 20 kg of high-temperature biological bacterial liquid is added at a flow rate of 0.5 kg / h. The biological bacterial liquid includes a biological bacterial liquid with the function of fermenting oily sludge and a biological bacterial liquid with the function of degrading H2S gas. The weight ratio of the two is 19:1, and the concentrations of the two are higher than 5*10 7 / mL and 10 8 / mL, the fermentation promoting substances are sawdust and cow dung, the ratio of the two is 2:1, and they are added into the fermentation chamber 2 through the feed port 3 at a flow rate of 0.9kg / h, and the demulsifier is nonylphenol polyoxyethylene ether, the addition flow rate is 2g per liter of oily sludge, and the waste gas in the plant is 3.3m 3 / h flow rate is input into the fermentation chamber 2 through the air inlet 30;

[0181] S2: Fermentation

[0182] In the fermentation chamber 2, the material in the fermentation chamber 2 is heated by the heating component 6 and the waste flue gas from the plant area, and the two temperature detection positions at the front of the fermentation chamber 2 are maintained at 82°C, and the other four temperature detection positions in the rear fermentation chamber 2 are maintained at 73°C. The opening of the air distribution port 34 is regulated by the PLC control system, and the detection results of the oxygen content detection instruments at the front, middle and rear parts of the fermentation chamber 2 are controlled to be 6%, 20% and 16% respectively. Driven by the stirring and conveying mechanism, the solid material continues to move from front to back in the fermentation chamber 2, and the heating and demulsification link is completed in the high-temperature and low-oxygen area, which lasts for 1 hour, and the biological fermentation link is completed in the subsequent medium-high-temperature and high-oxygen area and the medium-high-temperature and low-oxygen area, which lasts for 9 hours;

[0183] S3: Discharging

[0184] The treated solid phase product is discharged from the fermentation chamber 2 through the discharge port, and refluxed to the feed port 3 at a flow rate of 0.7 kg / h through the material reflux pipe 32, and re-enters the fermentation chamber 2 together with the oily sludge to be treated. The waste gas generated by the fermentation in the fermentation chamber 2 is discharged from the factory waste flue gas through the outlet pipe on the outlet port 7 to the factory flue gas treatment unit for treatment. The solid phase product discharged from the fermentation chamber 2 has a moisture content of 17%, an oil content of 5%, a solid content of 78%, a reduction rate of 94%, a pH of 7.0, and a temperature of 128°C, a SO2 content of 173ppm, a H2S content of 12ppm, and a VOCs content of 35ppm.

[0185] S4: Separation and recovery

[0186] The waste flue gas from the factory enters the fermentation chamber 2 through the air distribution port 34 and provides a slight positive pressure of 0.116MPa. The negative pressure pipe 31 is evacuated by an air pump, so that the liquid collecting tank 8 presents a slight negative pressure of 0.086MPa. A capillary channel 5 is provided at the bottom of the fermentation chamber 2. The average pore size of the capillary channel 5 is 0.95 microns. The capillary channel 5 accounts for 2.8% of the volume of the bottom of the fermentation chamber 2. The self-priming recovery of the oily sludge demulsification and the oil-water mixture separated after fermentation enters the liquid collecting tank 8 through the slight pressure difference on both sides of the capillary channel 5. The density of the floating plate 14 in the oil-water separation tank 11 is 0.912g / cm 3The floating plate 14 floats at the oil-water interface. The floating plate 14 is provided with a capillary hollow fiber bundle 18, wherein the aperture of the capillary channel is 1.35 microns. The capillary hollow fiber bundle 18 occupies 16% of the area of ​​the floating plate 14. In addition, the floating plate 14 contains 4 oil-passing ports 17, which occupy 24% of the area of ​​the floating plate 14. The inner wall of the capillary channel in the capillary hollow fiber bundle 18 is coated with a hydrophobic coating, and the water drop contact angle is 102°. The extension of the hollow fiber bundle 18 is 10 mm higher than the floating plate 14. The oil in the oil-water separation tank 11 is recovered to the oil storage tank 13 through the capillary hollow fiber bundle 18. The purity of the recovered oil is >99.30%. The high-quality oil is discharged into the factory for reuse through the automatic control of the oil drain valve 21 by the liquid level meter 24 and the PLC system. When the float 14 reaches the first limit part 15 in the oil-water separation tank 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separation tank 11 into the factory wastewater treatment system for purification.

[0187] Example 2C

[0188] The oily sludge to be treated has a water content of 39%, an oil content of 52%, a solid content of 9%, a total liquid content of 91%, and a pH of 7.9. The temperature of the factory waste gas used by the device is 178°C and the SO2 content is 268ppm. The treatment method is as follows:

[0189] S1: Feed

[0190] The oily sludge to be treated is added to the fermentation chamber 2 through the feed port 3 at a flow rate of 6 kg / h. When the device is started for the first time, 10 kg of high-temperature biological bacterial solution is added at a flow rate of 0.5 kg / h. The biological bacterial solution includes a biological bacterial solution with the function of fermenting oily sludge and a biological bacterial solution with the function of degrading H2S gas. The weight ratio of the two is 9:1, and the concentrations of the two are higher than 5*10 7 / mL and 10 8 / mL, sawdust was selected as the fermentation promoting substance, and was added into the fermentation chamber 2 through the feed port 3 at a flow rate of 0.5kg / h. Tetrasodium ethylenediaminetetraacetic acid and sodium lignin sulfonate were selected as demulsifiers, with a ratio of 1:5 and an addition flow rate of 2.6g per liter of oily sludge. The waste gas from the plant was added at a flow rate of 0.8m 3 / h flow rate is input into the fermentation chamber 2 through the air inlet 30;

[0191] S2: Fermentation

[0192] In the fermentation chamber 2, the material in the fermentation chamber 2 is heated by the heating component 6 and the waste flue gas from the plant area, and the temperature detection positions of the first two parts of the fermentation chamber 2 are maintained at 86°C, and the remaining four temperature detection positions in the rear fermentation chamber 2 are maintained at 75°C. The opening of the air distribution port 34 is regulated by the PLC control system, and the detection results of the oxygen content detection instrument at the front, middle and rear of the fermentation chamber 2 are controlled to be 5%, 18% and 10% respectively. Driven by the stirring and conveying mechanism, the solid material continues to move from front to back in the fermentation chamber 2, and the heating and demulsification link is completed in the high-temperature and low-oxygen area, which lasts for 2 hours, and the biological fermentation link is completed in the subsequent medium-high-temperature and high-oxygen area and the medium-high-temperature and low-oxygen area, which lasts for 10 hours;

[0193] S3: Discharging

[0194] The treated solid phase product is discharged from the fermentation chamber 2 through the discharge port, and refluxed to the feed port 3 at a flow rate of 0.2 kg / h through the material reflux pipe 32, and re-enters the fermentation chamber 2 together with the oily sludge to be treated. The waste gas generated by the fermentation in the fermentation chamber 2 is discharged from the factory waste flue gas through the outlet pipe on the outlet port 7 to the factory flue gas treatment unit for treatment. The solid phase product discharged from the fermentation chamber 2 has a moisture content of 11%, an oil content of 7%, a solid content of 82%, a reduction rate of 89%, a pH of 7.3, and a temperature of 129°C, a SO2 content of 153ppm, a H2S content of 19ppm, and a VOCs content of 38ppm.

[0195] S4: Separation and recovery

[0196] The waste flue gas from the factory enters the fermentation chamber 2 through the air distribution port 34 and provides a slight positive pressure of 0.121 MPa. The negative pressure pipe 31 is evacuated by an air pump, so that the liquid collecting tank 8 presents a slight negative pressure of 0.088 MPa. A capillary channel 5 is provided at the bottom of the fermentation chamber 2. The average pore size of the capillary channel 5 is 0.98 microns. The capillary channel 5 accounts for 2.3% of the volume of the bottom of the fermentation chamber 2. The self-priming recovery of the oily sludge demulsification and the oil-water mixture separated after fermentation enters the liquid collecting tank 8 through the slight pressure difference on both sides of the capillary channel 5. Most of the demulsified water is absorbed by microorganisms and evaporated at high temperature to form water vapor. The oil-water mixture in the liquid collecting tank 8 enters the oil-water separation tank 11 from the bottom through the partition 12. The density of the floating plate 14 in the oil-water separation tank 11 is 0.893g / cm 3The floating plate 14 floats at the oil-water interface. The floating plate 14 is provided with a capillary hollow fiber bundle 18, wherein the capillary channel pore size is 1.62 microns, and the capillary hollow fiber bundle 18 occupies 12.5% ​​of the area of ​​the floating plate 14. In addition, the floating plate 14 contains 4 oil-passing ports 17, which occupy 28% of the area of ​​the floating plate 14. The inner wall of the capillary channel 5 in the capillary hollow fiber bundle 18 is coated with a hydrophobic coating, and the water drop contact angle is 113°. The extension of the hollow fiber bundle 18 is 10° higher than the floating plate 14. mm, the oil in the oil-water separation tank 11 is recovered to the oil storage tank 13 through the capillary hollow fiber bundle 18, the purity of the recovered oil is>99.80%, and the high-quality oil is collected into the factory for reuse through the level meter 24 and the PLC system to control the oil drain valve 21. When the float 14 reaches the first limit part 15 in the oil-water separation tank 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separation tank 11 into the factory wastewater treatment system for purification.

[0197] Comparative Example 1

[0198] The same device as in Example 2A is used, but instead of using the factory waste gas, air is used, and the output power of the heating component 6 is kept consistent with that in Example 2A. In order to keep the oxygen concentration in the fermentation chamber 2 consistent when using air, the air flow rate is changed to 0.03m 3 / h.

[0199] In the S1 feed condition, except that the factory waste flue gas was replaced by air, the other feed conditions were the same as those in Example 2A;

[0200] During the fermentation process of S2, the temperature of the two temperature monitoring positions at the front of the fermentation chamber 2 was 78°C, and the temperature of the other four temperature monitoring positions at the middle and rear of the fermentation chamber 2 was 65°C;

[0201] During the S3 discharge process, the solid product discharged from the fermentation chamber 2 has a moisture content of 23%, an oil content of 30%, a solid content of 47%, a reduction rate of 70%, a pH of 7.6, a temperature of the gas discharged from the fermentation chamber 2 of 28°C, a SO2 content of 1ppm, a H2S content of 166ppm, and a VOCs content of 382ppm;

[0202] During the S4 separation and recovery process, there is a lack of waste flue gas entering the fermentation chamber 2. After the air is replaced, in order to keep the oxygen concentration in the fermentation chamber 2 consistent with that in Example 2A, the air flow rate is reduced compared to the waste flue gas flow rate in the plant area, and the micro-positive pressure in the fermentation chamber 2 is reduced to 0.103 MPa. Due to the pressure drop, the volume of the recovered oil-water mixture after treatment is reduced by 23% compared to Example 2A.

[0203] By comparison with Example 2A, it was found that after the factory waste flue gas was replaced with air, the temperature in the fermentation chamber 2 decreased, the pH value of the oily sludge was higher, and the overall oily sludge reduction effect was reduced; due to the reduction in air flow, the micro-positive pressure in the fermentation chamber 2 decreased, resulting in a reduction in the amount of oil and water recovered; the pollutants such as H2S and VOCs generated during the demulsification and fermentation process of the oily sludge had a high concentration when they were carried out by the air, so that the used air needed to be purified before it could be discharged after being discharged from the fermentation chamber 2, and the environmental protection performance was reduced.

[0204] Examples 2D1-2D19

[0205] The same device and method as in Example 2A were used, but the components of the waste flue gas used were different. The parameters of the oily sludge after treatment corresponding to the components of the waste flue gas were shown in Table 1 below:

[0206] Table 1

[0207]

[0208] By comparison, it was found that when the device was used to reduce the amount of oily sludge, it used waste flue gas from the factory area with a certain temperature and SO2. During the treatment process, it could not only synergistically control SO2, but also regulate the pH of the oily sludge, thereby enhancing the demulsification and biological treatment effects of the oily sludge and enhancing the reduction effect of the oily sludge.

[0209] When the flue gas temperature is between 120-300°C, the oily sludge reduction effect is better, and the reduction rate is higher than 75%, especially when the flue gas temperature is between 150-200°C, the reduction rate is higher than 80%; when the SO2 content is above 100ppm, the oily sludge can be regulated to have a lower and appropriate pH, and the oily sludge reduction effect is better, and the reduction rate is higher than 75%. When SO2 is less than 100ppm, the pH of the oily sludge is higher, the reduction effect becomes worse, and the reduction rate is lower than 75%.

[0210] Examples 2E1-2E7

[0211] The same device and method as in Example 2C were used, but the temperature distribution and oxygen content in the front, middle and rear parts of the fermentation chamber 2 were different during the treatment process. The parameters of the treated oily sludge corresponding to the different temperature and oxygen content distributions are shown in Table 2 below:

[0212] Table 2

[0213]

[0214] By comparison, it is found that the demulsification and fermentation treatment effects of the oily sludge can be improved by regulating the temperature and oxygen content in the front, middle and rear parts of the fermentation chamber 2.

[0215] When the temperature and oxygen concentration in the fermentation chamber 2 are controlled by zones (Example 2C), the oily sludge reduction rate can be as high as 89%; when only the oxygen concentration is controlled by zones (Examples 2E1-2E3), even if the temperature parameters are optimized, the maximum reduction rate is only 87%; when only the temperature is controlled by zones (Examples 2E6 and 2E7), the reduction rate can only reach 87%; when the temperature and oxygen concentration are not controlled by zones (Examples 2E4 and 2E5), the oily sludge reduction effect is significantly worse, with reduction rates of 75% and 83%.

[0216] Examples 2F1-2F17

[0217] The same device and method as in Example 2A are used, but the amount of biological liquid added to the fermentation chamber 2, the flow rate of the fermentation-promoting substance added, and the sludge return rate are changed. The corresponding parameters of the treated oily sludge are shown in Table 3 below:

[0218] Table 3

[0219]

[0220]

[0221] By comparison, it was found that the appropriate amount of high-temperature biological liquid added, sawdust added flow rate and sludge return flow rate can achieve a high oily sludge reduction rate. Keeping the amount of biological liquid added in the range of 2-30kg can maintain an oily sludge reduction rate of more than 80%. At the same time, maintaining a sawdust addition of 0.3kg / h and a sludge return flow of 0.26kg / h can maintain a high oily sludge treatment effect.

[0222] Examples 2G1-2G17

[0223] The same device and method as in Example 2A were used, but the size of the capillary channel 5, the volume percentage of the capillary channel 5 and the micro-pressure difference were different. The oily sludge reduction rate after treatment corresponding to different capillary channel 5 sizes, capillary channel 5 volume percentages and micro-pressure difference parameters are shown in Table 4 below:

[0224] Table 4

[0225]

[0226]

[0227] By comparison, it was found that maintaining the pore size of capillary channel 5 below 2 μm would achieve better oily sludge reduction effect, and the capillary channel 5 needs to have a certain volume share. When the volume share is above 0.5-4.0%, the oily sludge reduction rate is relatively high, maintained above 75%. The presence of micro-pressure difference also significantly affects the oily sludge reduction effect. Within the micro-pressure difference range of ≤0.045, the larger the micro-pressure difference, the better the oily sludge treatment effect.

[0228] Examples 2H1-2H15

[0229] The same device and method as in Example 2A are used, but the capillary channel pore size, capillary channel area ratio, oil port 17 area ratio, and hydrophilicity of the hydrophobic coating on the inner wall of the capillary channel of the hollow fiber bundle 18 in the oil-water separation tank 11 are different. The corresponding results of the oil purity after treatment are shown in Table 5 below:

[0230] Table 5

[0231]

[0232]

[0233] By comparison, it was found that controlling the capillary channel pore size at 4 μm can obtain better oil recovery purity, and regulating the appropriate area ratio of the hollow fiber bundle 18 and the oil passage 17 is beneficial to improving the purity of the recovered oil. When the water droplet contact angle of the hydrophobic coating is above 90°, high-purity oil resources can be recovered.

[0234] Compared with CN115504643A and CN113816577A, this embodiment adopts an integrated fermentation chamber 2 to achieve efficient demulsification and biological fermentation of oily sludge, and utilizes waste flue gas in the factory area through porous air distribution, thereby enhancing the heating and demulsification effect of oily sludge, and realizes self-priming recovery of oil and water resources through the capillary channel 5 by constructing a micro-pressure difference, and realizes oil-water separation by designing a floating plate 14 with a hollow fiber bundle 18 to realize self-priming, thereby realizing high-quality oil product (>98.5%) resource recovery. The device is equipped with a PLC control system, which can automatically control the temperature and oxygen distribution, and optimize the demulsification and fermentation effect of oily sludge. The PLC control system can simplify the operation of the device and realize automatic opening and closing of the device valve, thereby improving the operability and economy of the device biological treatment of oily sludge.

[0235] 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 fermentation chamber is disposed inside the shell, a feed port and a discharge port connected to the fermentation chamber are disposed at both ends of the shell, a capillary channel connected to the fermentation chamber is opened on the side wall of the fermentation chamber, a heating component is disposed inside the side wall of the fermentation chamber, and an air outlet is disposed on the top of the fermentation chamber; A stirring and conveying mechanism is arranged inside the shell and is used for stirring and conveying materials in the fermentation chamber.

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

3. The oily sludge reduction treatment device according to claim 2 is characterized in that: It also includes an oil-water separation structure, which is connected to the liquid discharge port through a liquid infusion pipeline.

4. The oily sludge reduction treatment device according to claim 3 is characterized in that: The oil-water separation structure comprises: An oil-water separation tank, wherein a partition is vertically arranged inside the oil-water separation tank, and the partition divides the inside of the oil-water separation tank into a first space and a second space connected at the bottom; An oil storage tank, wherein the oil storage tank is arranged below the oil-water separation tank; A floating plate, the floating plate is movably arranged in the second space, the floating plate can float on the oil-water interface, a first limiting portion and a second limiting portion connected to the inner wall of the oil-water separation tank are respectively arranged above and below the floating plate, and the floating plate is provided with a plurality of oil passage ports; A hollow fiber bundle, wherein the upper end of the hollow fiber bundle penetrates the floating plate and forms an extension portion above the floating plate, the lower end of the hollow fiber bundle extends into the oil storage tank, and a capillary channel is formed in the hollow fiber bundle; A sealing portion is provided between the oil-water separation tank and the oil storage tank so that the oil-water separation tank is communicated with the oil storage tank only through the capillary channel.

5. The oily sludge reduction treatment device according to claim 4 is characterized in that: An oil drain port is provided at the lower end of the side wall of the oil storage tank, and an oil drain valve is provided in the oil drain port. A water drain port is provided at the lower end of the side wall of the oil-water separation tank, and a water drain valve is provided in the water drain port. A liquid level gauge is provided in the oil storage tank, and a first position sensor and a second position sensor are respectively provided on the side where the first limit part and the second limit part are close to each other.

6. The oily sludge reduction treatment device according to claim 4 is characterized in that: The density of the floating disk is 0.850-0.950 g / cm 3 .

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

8. The oily sludge reduction treatment device according to claim 4 is characterized in that: A hydrophobic coating is arranged on the inner wall of the capillary channel, and the water drop contact angle of the hydrophobic coating is 95-140°.

9. The oily sludge reduction treatment device according to claim 1, characterized in that: The pore size of the capillary channel is 0.01-2 microns.

10. The oily sludge reduction treatment device according to claim 1, characterized in that: Relative to the total volume of the side wall of the fermentation chamber, the volume of the capillary channel accounts for 0.5-4%.

11. 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 fermentation 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.

12. The oily sludge reduction treatment device according to claim 11, characterized in that: The driving motor is a variable frequency motor.

13. The oily sludge reduction treatment device according to claim 11, characterized in that: It also includes an air intake structure, the output end of which is communicated with the fermentation chamber and is used to transport acidic gas and oxygen into the fermentation chamber.

14. The oily sludge reduction treatment device according to claim 13, characterized in that: The air intake structure comprises: An air intake passage, the air intake passage being arranged inside the rotating shaft along the axial direction of the rotating shaft; a plurality of air distribution ports, the plurality of air distribution ports being arranged on the rotating shaft along the axial direction of the rotating shaft and connecting the air inlet channel with the fermentation chamber; An air inlet is arranged at one end of the rotating shaft close to the driving motor.

15. The oily sludge reduction treatment device according to claim 14, characterized in that: An opening regulating valve is arranged in each of the air distribution ports.

16. The oily sludge reduction treatment device according to claim 1, characterized in that: Three oxygen content detection instruments are sequentially arranged in the fermentation chamber along the conveying direction of the material, and the three oxygen content detection instruments are used to detect the oxygen concentration in the front, middle and rear parts of the fermentation chamber respectively.

17. The oily sludge reduction treatment device according to claim 1, characterized in that: A plurality of temperature detection components are sequentially arranged in the fermentation chamber along the conveying direction of the material, and the plurality of temperature detection components are used to detect the temperature of a plurality of positions in the fermentation chamber.

18. The oily sludge reduction treatment device according to claim 17, characterized in that: The heating component is a segmented variable frequency heating rod arranged along the axial direction of the fermentation chamber, which can heat the material in the fermentation chamber in segments.

19. 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.

20. The oily sludge reduction treatment device according to claim 1, characterized in that: The discharge port is connected to a material reflux pipe, a variable frequency reflux pump is arranged on the material reflux pipe, and the material reflux pipe is connected to the feed port.

21. 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 20, characterized in that: The method includes: The oily sludge, demulsifier and biological bacteria liquid capable of fermenting the oily sludge are fed into the fermentation chamber through the feed inlet; Heating, stirring and conveying the materials in the fermentation chamber; discharging at least a portion of the liquid produced in the fermentation chamber through the capillary channel; discharging at least part of the gas generated in the fermentation chamber through the gas outlet; The solid product produced in the fermentation chamber is discharged through the discharge port.

22. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The water content of the oily sludge is higher than 35%, the oil content of the oily sludge is higher than 35%, and the total liquid content of the oily sludge is higher than 80%.

23. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The method also includes inputting fermentation-promoting substances into the fermentation chamber through a feed inlet.

24. The method for reducing the amount of oily sludge according to claim 23, characterized in that: The fermentation-promoting substance is selected from at least one of sawdust, cow dung and rice straw.

25. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The demulsifier is selected from at least one of sodium lignin sulfonate, tetrasodium ethylenediaminetetraacetate, ethylenediamine, polyquaternary ammonium salt, polyether polyquaternary ammonium salt, glycerol, nonylphenol polyoxyethylene ether, polyacrylate, sodium dodecylbenzene sulfonate, and hexadecyltrimethylammonium bromide.

26. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The amount of the demulsifier added relative to the oily sludge is 0.5 to 6 g / L.

27. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The survival temperature of the biological bacterial liquid is 35-95°C, the use temperature of the biological bacterial liquid is 60-80°C, and the preferred use temperature is 70-75°C.

28. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The method further includes inputting acidic gas and oxygen into the fermentation chamber so that the acidic gas and the oxygen are mixed with the oily sludge.

29. The method for reducing the amount of oily sludge according to claim 28, characterized in that: The acid gas is an acid gas containing SO2, wherein the content of SO2 is in the range of 100-1000 ppm; the content of oxygen is in the range of 6-20%.

30. The method for reducing the amount of oily sludge according to claim 29, characterized in that: The acid gas and the oxygen are provided by using waste flue gas from a factory, and the temperature of the waste flue gas from a factory is 120-300°C, preferably 150-200°C.

31. The method for reducing the amount of oily sludge according to claim 30, characterized in that: When the biological bacterial liquid with the function of fermenting oily sludge is input into the fermentation chamber from the feed inlet, the biological bacterial liquid with the function of degrading H2S gas is also input into the fermentation chamber.

32. The method for reducing the amount of oily sludge according to claim 29, characterized in that: The volume ratio of the factory waste flue gas input into the fermentation chamber to the oily sludge is 1:1-500:

1.

33. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The temperature of the oily sludge in the fermentation chamber is 50-85°C, preferably 70-75°C.

34. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The oxygen concentration in the front part of the fermentation chamber is greater than 15%, and the oxygen concentration in the middle and rear parts of the fermentation chamber is less than 10%.

35. 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 fermentation chamber is 6-24 hours.

36. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The method also includes providing a negative pressure environment at one end of the capillary channel away from the fermentation chamber.

37. The method for reducing the amount of oily sludge according to claim 21, characterized in that: A portion of the solid product is returned to the fermentation chamber, and the ratio of the flow rate of the solid product returned to the fermentation chamber to the flow rate of the oily sludge input into the fermentation chamber is 1:5-1:

50.

38. The method for reducing the amount of oily sludge according to claim 21, 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 so that the pressure in the liquid collecting groove is 0.085-0.095MPa, and the pressure in the shell is 0.105-0.13MPa.

39. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The method also includes separating oil and water from the derived liquid.

40. The method for reducing the amount of oily sludge according to claim 21, characterized in that: The biological bacterial liquid capable of fermenting oily sludge comprises at least one of the genera Streptococcus, Micrococcus and Moinecoccus.

41. The method for reducing the amount of oily sludge according to claim 40, characterized in that: The concentration of the biological bacterial solution capable of fermenting oily sludge is higher than 5×10 7 / mL, and the added amount of the biological bacteria liquid with the function of fermenting oily sludge is 2-30kg.

42. The method for reducing the amount of oily sludge according to claim 31, characterized in that: The biological bacterial liquid capable of degrading H2S gas includes at least one of Dietzia, Enterobacter, and Lysinibacillus.

43. The method for reducing the amount of oily sludge according to claim 42, characterized in that: The concentration of the biological bacterial solution having the function of degrading H2S gas is higher than 10 8 / mL, and the added amount of the biological bacterial liquid with the function of degrading H2S gas is 0.1-3kg.

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