CN117486450A - Demulsification, dehydration and filter pressing integrated process for hydrate oil sludge - Google Patents
Demulsification, dehydration and filter pressing integrated process for hydrate oil sludge Download PDFInfo
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- CN117486450A CN117486450A CN202311449310.7A CN202311449310A CN117486450A CN 117486450 A CN117486450 A CN 117486450A CN 202311449310 A CN202311449310 A CN 202311449310A CN 117486450 A CN117486450 A CN 117486450A
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- 239000010802 sludge Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 45
- 230000008569 process Effects 0.000 title claims abstract description 39
- 238000003825 pressing Methods 0.000 title claims abstract description 29
- 230000018044 dehydration Effects 0.000 title claims abstract description 28
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 112
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 31
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 31
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 13
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 238000003756 stirring Methods 0.000 claims description 22
- 239000012071 phase Substances 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 7
- 238000007789 sealing Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000003921 oil Substances 0.000 abstract description 63
- 239000007789 gas Substances 0.000 abstract description 45
- 239000007787 solid Substances 0.000 abstract description 15
- 238000001035 drying Methods 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 239000003814 drug Substances 0.000 abstract description 4
- 238000004945 emulsification Methods 0.000 abstract description 4
- 238000005191 phase separation Methods 0.000 abstract description 4
- 239000002910 solid waste Substances 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 239000002893 slag Substances 0.000 description 7
- 239000007790 solid phase Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000005189 flocculation Methods 0.000 description 5
- 230000016615 flocculation Effects 0.000 description 5
- 230000006872 improvement Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
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- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000004332 deodorization Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000002441 reversible effect Effects 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 239000013043 chemical agent Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- -1 asphaltene Substances 0.000 description 1
- 239000002734 clay mineral Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
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- 238000011144 upstream manufacturing Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention relates to the technical field of oil sludge treatment, and discloses a hydrate oil sludge demulsification, dehydration and filter pressing integrated process, which comprises the steps of adding oil sludge into a reaction kettle; cooling the reaction kettle, introducing high-pressure carbon dioxide into the reaction kettle, cooling the reaction kettle to 4-6 ℃, raising the pressure to 5MPa, and standing for 50-70 Min until carbon dioxide hydrate is generated; opening a pressure release valve at the bottom of the reaction kettle, self-driving and press-filtering under the pressure in the reaction kettle, discharging oil-water gas and separating; and when the pressure in the reaction kettle is reduced to 1MPa, heating the reaction kettle, and when the pressure in the reaction kettle is increased to normal temperature and is lower than 0.2MPa, decompressing the reaction kettle and taking out the dried oil sludge. According to the invention, a plurality of processes are organically coupled together, the drying of the oil sludge and the separation of oil, water and gas are realized by a single flow, the polarity of carbon dioxide is utilized to destroy the emulsification structure in the oil sludge, the oil, water and solid three-phase separation is promoted, and the overall energy consumption is low; no medicament is added, the total amount of solid waste is reduced, and the solid components of the dehydrated oil sludge are simplified, so that the subsequent treatment is facilitated.
Description
Technical Field
The invention relates to the technical field of oil sludge treatment, in particular to a demulsification, dehydration and filter pressing integrated process for hydrate oil sludge.
Background
The oil sludge has complex components, is a mixture composed of petroleum hydrocarbon, inorganic mineral substances, chemical agents and heavy metals, causes serious environmental pollution due to improper treatment, contains a large amount of residual petroleum components, and has high recycling value. However, the oily sludge has high water content, strong fluidity, easy diffusion, pollution expansion, high energy consumption for treatment and high cost, and is generally called as high-water-content oily sludge. The high water content oil sludge is mainly generated in oil fields and refineries, and is scum, bottom sludge, biochemical sludge and the like which are generated in the processes of upstream exploitation of oil fields, downstream refining of refineries and the like and are not dehydrated yet. The composition is complex, and the multiphase mixture mainly comprises chemical agents such as water, aged crude oil, asphaltene, clay mineral, inorganic salt, surfactant and the like and part of industrial impurities. The complex composition leads to the formation of oil-in-water (O/W) and water-in-oil (W/O) complex emulsion systems, and has the characteristics of small oil and water density difference, strong water holding capacity, high viscosity, difficult sedimentation and dehydration and the like.
The traditional sludge dewatering method mainly comprises flocculation dewatering, hot air dewatering, filter pressing dewatering, centrifugal dewatering and the like. The flocculation dehydration technology utilizes the characteristic of negative ions in the oil sludge, and the flocculant is added into the oil sludge to continuously compress the double-layer electricity of the oil sludge colloidal particles and rapidly separate liquid and solid in the slurry. However, the addition of the flocculant not only increases the total amount of solid waste, but also flocculates the dehydrated sludge solid to form gel, which is unfavorable for subsequent treatment. The hot air dehydration refers to drying the oil sludge at high temperature to evaporate the water and achieve the purpose of dehydration. However, the energy consumption of the latent heat of evaporation of water is a decisive factor for the economic viability of the overall process. The latent heat of evaporation of water, due to the effect of hydrogen bonding between water molecules, is as high as 44kJ/mol (25 ℃), the highest of all known solvents. Therefore, hot gas dehydration requires a large amount of energy for evaporating water that is not used, and is liable to cause secondary pollution. The filter pressing dehydration is to put the oil sludge into the filter material, apply pressure to discharge the water from the filter material, and the filter pressing dehydration method has complex operation and complex process flow. The centrifugal dehydration is to separate out water in the oil sludge by utilizing centrifugal force, and the centrifugal dehydration method can only remove a very limited part of water in the oil sludge, mainly gap water, has limited effect on adhesion water and chemical combination water, especially has very limited separation effect because of almost no capability of water in water-in-oil.
Disclosure of Invention
The invention aims to provide a demulsification, dehydration and filter pressing integrated process for hydrate sludge, which aims to solve the problems of limited sludge dehydration and secondary pollution in the traditional method.
In order to achieve the above purpose, the invention adopts the following technical scheme: the integrated process for demulsifying, dehydrating and filter-pressing the hydrate oil sludge comprises the following steps:
step 1: adding the oil sludge into a reaction kettle, and then sealing the reaction kettle;
step 2: starting a heat pump to cool the reaction kettle, introducing high-pressure carbon dioxide into the reaction kettle, cooling the reaction kettle to 4-6 ℃, raising the pressure to 5MPa, and standing for 50-70 Min until carbon dioxide hydrate is generated;
step 3: opening a pressure release valve at the bottom of the reaction kettle, self-driving and pressure-filtering under the pressure in the reaction kettle, enabling oil-water gas to enter a buffer tank, performing gas-liquid separation in the buffer tank, enabling a liquid phase to enter an oil-water separation tank, and standing to separate oil and water;
step 4: when the pressure in the reaction kettle is reduced to 1MPa, switching the cold and hot source inlet and outlet of the heat pump to heat the reaction kettle, when the reaction kettle is raised to normal temperature and the pressure in the reaction kettle is lower than 0.2MPa, opening a pressure release valve at the top of the reaction kettle to release pressure, and taking out the dried oil sludge after releasing the pressure to normal pressure.
Preferably, as an improvement, two groups of reaction kettles are arranged, when one group of reaction kettles is in the cooling time period of step 4, oil sludge is added into the other group of reaction kettles, the steps are repeated, and the temperature of the other group of reaction kettles is controlled to be raised simultaneously in the cooling time period of the one group of reaction kettles. The characteristic that the exothermic synthesis of the carbon dioxide hydrate and the endothermic decomposition reaction of the carbon dioxide hydrate are reversible reactions and the heat absorption and release are completely consistent is utilized, and the heat released by one group of reaction kettles is used for cooling the other group of reaction kettles, so that the energy consumption of the whole treatment process is reduced.
Preferably, as an improvement, in the step 1, the temperature of the reaction kettles is controlled by a heat pump, and the heat pump controls different reaction kettles to heat and cool respectively at the same time. Therefore, heat can be generated when the heat pump is used for refrigerating, so that the two groups of reaction kettles are cooled and heated respectively.
Preferably, as an improvement, in the step 2, the stirring paddle in the reaction kettle is started to stir the oil sludge before introducing the high-pressure carbon dioxide, the stirring speed is 38-45 rpm, and the stirring time is 25-35 min.
Preferably, as a modification, the mixture is kept stand for 60min in the step 2 to generate hydrate.
Preferably, as an improvement, the method further comprises the step of compressing and injecting the gas phase separated from the buffer tank in the step 3 into a high-pressure gas tank for standby.
Preferably, as a modification, the gas phase separated in the step 3 is first subjected to impurity removal and then injected into the high-pressure gas tank.
Preferably, in the step 2, high-pressure carbon dioxide is introduced into the reaction kettle through an air supply pipe, and the air supply pipe is positioned at the bottom of the reaction kettle.
Preferably, as an improvement, be provided with the filter plate in the reation kettle of step 1, the fatlute tilizes on the filter plate, in step 3, when self-driven filter pressing efficiency reduces, close reation kettle bottom relief valve, pulse lets in high-pressure carbon dioxide in the filter plate below space of reation kettle simultaneously, stirs filter plate upper portion material simultaneously, stops stirring after the stirring preset time, closes carbon dioxide and reopens reation kettle bottom relief valve. After the clearance between the filter plate and the hydrate is blocked, the filtering efficiency of oil water and gas is reduced, and at the moment, the high-pressure carbon dioxide fed from the lower part of the filter plate in a pulse mode can dredge the filter holes of the filter plate, meanwhile, the solid hydrate is turned upwards, the self-driving pressure is further improved, in addition, the effect and the efficiency of turning are improved due to the intervention of the stirring device, and therefore, a new round of high-efficiency self-driving filter pressing is restarted.
The scheme has the advantages that:
(1) According to the invention, a plurality of processes are organically coupled together, the drying of the oil sludge and the separation of oil, water and gas are realized by a single flow, the polarity of carbon dioxide is utilized to destroy the emulsification structure in the oil sludge and promote the oil, water and solid three-phase separation, and compared with the traditional steam drying, the drying system has no phase change, avoids the high energy consumption of the phase change stage of the water phase and has low overall energy consumption; compared with the traditional flocculation drying, the invention has no medicament addition, reduces the total amount of solid phase waste, simplifies the solid phase components of the dehydrated oil sludge, and is beneficial to subsequent treatment.
(2) The carbon dioxide inert gas is used in the whole process, and the purity of the carbon dioxide gas is not particularly required, so that the gas can be an anaerobic fermentation byproduct, the cost is basically avoided, the sealing degree of the whole process is high, the odor component in the oil sludge can not escape, the gas is recycled for a plurality of times and then is subjected to centralized deodorization treatment, and compared with the traditional steam drying odor escape problem, the problem of the gas is effectively controlled.
(3) The method skillfully utilizes the characteristics that the exothermic synthesis reaction of the carbon dioxide hydrate and the endothermic decomposition reaction of the carbon dioxide hydrate are reversible reactions, and the heat absorption and the heat release are consistent, adopts a mode of combining a heat pump with a plurality of kettles, uses the released heat of one group of kettles to cool the other group of kettles, and reduces the energy consumption; meanwhile, the pressure of carbon dioxide in the kettle is fully utilized to realize in-situ filter pressing in the kettle, so that the process flow is shortened, and the energy consumption of the whole process is reduced.
Drawings
Fig. 1 is a schematic flow chart of a process integrating demulsification, dehydration and filter pressing of hydrate sludge according to an embodiment of the invention.
Fig. 2 is a schematic structural diagram of a device integrating demulsification, dehydration and filter pressing of hydrate sludge according to an embodiment of the invention.
Detailed Description
The following is a further detailed description of the embodiments:
reference numerals in the drawings of the specification include: a reaction kettle 1, a heat pump 2, a high-pressure gas tank 3, a buffer tank 4, an oil-water separation tank 5, an oil tank 6 and a water tank 7.
The examples are shown:
as shown in fig. 1, this embodiment takes 50kg of sludge with water content of 80% as an example, and illustrates a process for demulsification, dehydration and filter-pressing integrated process for hydrate sludge, which specifically includes the following steps:
step 1: the oil sludge is added into the reaction kettle 1, and then the reaction kettle 1 is closed.
Specifically, the lower part in the reaction kettle is provided with a filter plate, 50kg of oil sludge is pumped into the reaction kettle 1 and spread on the filter plate, and the upper flange of the reaction kettle 1 is tightly covered and sealed with the reaction kettle 1.
Step 2: and (3) starting the heat pump 2 to cool the reaction kettle 1, introducing high-pressure carbon dioxide into the reaction kettle 1, and standing for 50-70 Min until hydrate is generated after the reaction kettle 1 is cooled to 4-6 ℃ and the pressure is increased to 5 MPa.
Preferably, when the reaction kettle 1 is cooled to 5 ℃ and the pressure is increased to 5MPa, the reaction kettle is kept stand for 60 minutes to generate hydrate.
Wherein, before introducing carbon dioxide, stirring the sludge by starting a stirring paddle in the reaction kettle 1 at a stirring speed of 38-45 rpm for 25-35 min, in this embodiment at a stirring speed of 40rpm for 30 min to homogenize the sludge.
Continuously stirring at the current speed in the process of introducing carbon dioxide until the reaction kettle 1 is cooled to 5 ℃, and stopping stirring when the pressure is increased to 5MPa, so that substances in the reaction kettle 1 are uniformly stirred, the subsequent reaction speed is increased, and the reaction is more thorough.
Step 3: opening a pressure release valve at the bottom of the reaction kettle 1, self-driving and pressure-filtering under the pressure in the reaction kettle 1, enabling oil-water gas to enter a buffer tank 4, performing gas-liquid separation in the buffer tank 4, enabling liquid phase to enter an oil-water separation tank 5, and separating oil and water after standing.
The gas phase separated in the buffer tank 4 in this step is injected into the high-pressure gas tank 3 for standby. The separated gas phase is purified and compressed before being injected into the high pressure gas tank 3.
In this step, when filter-pressing efficiency reduces, close the bottom relief valve earlier to let in high-pressure carbon dioxide gas to reation kettle 1's filter plate below space, adopt pulse mode air feed, stir filter plate upper portion material simultaneously, stop stirring after the stirring preset time 5min, stop letting in high-pressure carbon dioxide, open reation kettle 1 bottom relief valve and carry out self-driven filter-pressing again simultaneously. In the use process of the filter plate, the filter holes are easy to be blocked by solid slag, and the filtering effect is affected; the mode dredges the filtering holes of the filter plate and increases the self-driven pressure, so that the filtering efficiency is improved, and the process can be adjusted for multiple times according to the actual production condition.
The carbon dioxide inert gas is used in the whole process, and the purity of the carbon dioxide gas is not particularly required, so that the gas can be an anaerobic fermentation byproduct, the cost is basically avoided, the sealing degree of the whole process is high, the odor component in the oil sludge can not escape, the gas is recycled for a plurality of times and then is subjected to centralized deodorization treatment, and compared with the traditional steam drying odor escape problem, the problem of the gas is effectively controlled.
Step 4: when the pressure in the reaction kettle 1 is reduced to 1MPa, switching cold and hot source inlets and outlets of the heat pump 2 to heat the reaction kettle 1, when the reaction kettle 1 is raised to normal temperature and the pressure in the reaction kettle 1 is lower than 0.2MPa, opening a pressure relief valve at the top of the reaction kettle 1 to relieve pressure, and taking out the dried oil sludge after the pressure is relieved to normal pressure.
In the step, the refrigeration in the kettle is switched into heating by switching the cold and heat source inlet and outlet of the heat pump 2 through a tee joint.
The moisture content of the dried sludge in this step can be reduced to 35%.
The number of the reaction kettles 1 is the same, when one group of reaction kettles 1 is in the cooling time period of the step 4, the steps are repeated by adding the oil sludge into the other group of reaction kettles 1, the heat pump 2 controls the other group of reaction kettles 1 to heat in the cooling time period of the one group of reaction kettles 1, and the heat pump 2 controls the different reaction kettles 1 to heat and cool respectively. The characteristics that the exothermic synthesis of the carbon dioxide hydrate and the endothermic decomposition reaction of the carbon dioxide hydrate are reversible reactions, the heat absorption and the heat release in the two reaction processes are completely consistent are utilized, a heat pump 2 and multiple kettles are combined, the released heat of one kettle is used for cooling the other kettle, the refrigeration coefficient of the heat pump 2 is 2.5, and the energy consumption of the heat pump 2 is 30 kW.h/ton of oil sludge (the water content is 80%) and is far lower than that of heat drying 200-300 kW.h/ton of oil sludge. Meanwhile, the pressure of carbon dioxide in the kettle is fully utilized to realize in-situ filter pressing in the kettle, so that the process flow is shortened, and the energy consumption of the whole process is reduced.
The dehydration kettle can adopt a quick-dismantling mode, and all other supporting facilities such as the heat pump 2, the gas pressurizing device, the oil-water separating device and the like except the kettle are public, so that the turnover rate of equipment is high, the investment of unit treatment capacity cost is low, and the treatment scale can be easily amplified by utilizing multiple kettles and multiple interfaces.
According to the invention, a plurality of processes are coupled together, the drying of the oil sludge and the separation of oil, water and gas are realized by a single flow, the polarity of carbon dioxide is utilized, the emulsification structure in the oil sludge can be destroyed, and the oil, water and solid three-phase separation is promoted; compared with the traditional flocculation drying, the invention has no medicament addition, reduces the total amount of solid phase waste, simplifies the solid phase components of the dehydrated oil sludge, and is beneficial to subsequent treatment.
The scheme also provides a hydrate oil sludge demulsification, dehydration and filter pressing integrated device, as shown in figure 2, specifically comprising: a reaction kettle 1, a heat pump 2, a high-pressure gas tank 3, a buffer tank 4, an oil-water separation tank 5, an oil tank 6 and a water tank 7.
The reaction kettle 1, the buffer tank 4 and the oil-water separation tank 5 are sequentially communicated, the oil tank 6 and the water tank 7 are communicated with the oil-water separation tank 5, and carbon dioxide is filled in the high-pressure gas tank 3.
The multiple processes are coupled together, the drying of the oil sludge and the separation of oil and water and gas are realized by a single flow, the polarity of carbon dioxide is utilized, the emulsification structure in the oil sludge can be destroyed, and the oil-water-solid three-phase separation is promoted. Compared with the traditional flocculation drying, the invention has no medicament addition, reduces the total amount of solid phase waste, simplifies the solid phase components of the dehydrated oil sludge, and is beneficial to subsequent treatment.
The top of the reaction kettle 1 is provided with a flange cover for sealing the reaction kettle 1, so that the high-pressure reaction kettle 1 can be controlled to be formed. The reaction kettle 1 is internally provided with a stirring paddle which is used for uniformly stirring substances in the reaction kettle 1. The stirring paddles are arranged to stir the substances in the reaction kettle 1 uniformly, so that the subsequent reaction speed is accelerated and the reaction is more thorough. The inside bottom of reation kettle 1 is equipped with the filter plate, is equipped with a plurality of filtration pore on the filter plate. The high-pressure gas tank 3 is communicated with the reaction kettle 1, a bottom pressure relief valve is arranged at the bottom of the reaction kettle 1 and used for controlling substances in the reaction kettle 1 to be discharged into the buffer tank 4, and a top pressure relief valve is arranged at the top of the reaction kettle 1. And a regulating valve can be further arranged for regulating and controlling the pressure relief quantity of the pressure relief valve.
The high-pressure gas tank 3 is communicated with the reaction kettle 1 through a gas supply pipe, one end of the gas supply pipe is positioned at the bottom of the reaction kettle 1, and the gas supply pipe is specifically positioned below the filter plate. So that the carbon dioxide is contacted with the oil sludge quickly, and the generation speed of the hydrate is increased. The buffer tank 4 is communicated with the high-pressure gas tank 3, and the communication part of the high-pressure gas tank 3 and the buffer tank 4 is positioned at the top of the buffer tank 4. The carbon dioxide inert gas is used in the whole process, and the purity of the carbon dioxide gas is not particularly required, so that the gas can be an anaerobic fermentation byproduct, the cost is basically avoided, the sealing degree of the whole process is high, the odor component in the oil sludge can not escape, the gas is recycled for a plurality of times and then is subjected to centralized deodorization treatment, and compared with the traditional steam drying odor escape problem, the problem of the gas is effectively controlled.
The device also comprises a gas compressor and a impurity removing device for absorbing impurities in gas, wherein the buffer tank 4, the impurity removing device, the compressor and the high-pressure gas tank 3 are sequentially communicated. The recycled gas is subjected to impurity removal and pressurization, and impurities are reduced from entering the high-pressure gas tank 3 while maintaining the high pressure of carbon dioxide. In addition, a temperature detector and a pressure detector are arranged, wherein the temperature detector is used for detecting the temperature in the reaction kettle 1, and the pressure detector is used for detecting the pressure in the reaction kettle 1. The pressure and temperature data of the reaction kettle 1 are conveniently obtained through a temperature detector and a pressure check meter.
The oil-water separation tank 5 is provided with a solid slag outlet, partial solid slag is inevitably carried and discharged when the reaction kettle 1 filters, and finally the solid slag enters the oil-water separation tank 5, after the oil-water separation tank 5 separates oil from water by utilizing different densities, the solid slag can be settled at the bottom of the oil-water separation tank 5, and the solid slag can be cleaned regularly through the solid slag outlet arranged on the oil-water separation tank 5, so that the continuous and stable operation of the whole device is ensured.
The foregoing is merely exemplary of the present invention, and specific technical solutions and/or features that are well known in the art have not been described in detail herein. It should be noted that, for those skilled in the art, several variations and modifications can be made without departing from the technical solution of the present invention, and in the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "fixed," etc. are to be construed broadly, and may be either a fixed connection, a removable connection, or an integral connection, for example; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances. The protection scope of the present application shall be subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims.
Claims (9)
1. The integrated process for demulsifying, dehydrating and filter-pressing the hydrate oil sludge is characterized by comprising the following steps of:
step 1: adding the oil sludge into a reaction kettle, and then sealing the reaction kettle;
step 2: cooling the reaction kettle, introducing high-pressure carbon dioxide into the reaction kettle, cooling the reaction kettle to 4-6 ℃, raising the pressure to 5MPa, and standing for 50-70 Min until carbon dioxide hydrate is generated;
step 3: opening a pressure release valve at the bottom of the reaction kettle, self-driving and pressure-filtering under the pressure in the reaction kettle, enabling oil-water gas to enter a buffer tank, performing gas-liquid separation in the buffer tank, enabling a liquid phase to enter an oil-water separation tank, and standing to separate oil and water;
step 4: and when the pressure in the reaction kettle is reduced to 1MPa, heating the reaction kettle, when the reaction kettle is raised to normal temperature and the pressure in the reaction kettle is lower than 0.2MPa, opening a pressure relief valve at the top of the reaction kettle for pressure relief, and taking out the dried oil sludge after the pressure is reduced to normal pressure.
2. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: and (3) setting two groups of reaction kettles, adding oil sludge into the other group of reaction kettles when the one group of reaction kettles are in the cooling time period of the step (4), repeating the steps, and controlling the other group of reaction kettles to heat simultaneously in the cooling time period of the one group of reaction kettles.
3. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 2, which is characterized in that: in the step 1, the temperature of the reaction kettles is controlled by a heat pump, and the heat pump controls different reaction kettles to simultaneously and respectively heat and cool.
4. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: in the step 2, the oil sludge is stirred before high-pressure carbon dioxide is introduced.
5. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: and (3) standing for 60min in the step (2) to generate a hydrate.
6. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: and (3) compressing and injecting the gas phase separated from the buffer tank in the step (3) into a high-pressure gas tank for standby.
7. The integrated process for demulsification, dehydration and filter pressing of the hydrate sludge according to claim 6, which is characterized in that: the gas phase separated in the step 3 is firstly subjected to impurity removal and then is injected into a high-pressure gas tank.
8. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: in the step 2, high-pressure carbon dioxide is introduced into the reaction kettle through an air supply pipe, and the air supply pipe is positioned at the bottom of the reaction kettle.
9. The integrated process for demulsification, dehydration and filter pressing of hydrate sludge according to claim 1, which is characterized in that: the reaction kettle of the step 1 is internally provided with a filter plate, the oil sludge is flatly paved on the filter plate, in the step 3, when the self-driven filter pressing efficiency is reduced, the pressure release valve at the bottom of the reaction kettle is closed, high-pressure carbon dioxide is simultaneously introduced into the space below the filter plate of the reaction kettle in a pulse mode, substances on the upper portion of the filter plate are simultaneously stirred, stirring is stopped after the preset time is reached, and the pressure release valve at the bottom of the reaction kettle is closed and opened again.
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