CN116004314A - Method for regenerating waste transformer oil - Google Patents
Method for regenerating waste transformer oil Download PDFInfo
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- CN116004314A CN116004314A CN202310090446.7A CN202310090446A CN116004314A CN 116004314 A CN116004314 A CN 116004314A CN 202310090446 A CN202310090446 A CN 202310090446A CN 116004314 A CN116004314 A CN 116004314A
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- 238000000034 method Methods 0.000 title claims abstract description 46
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- 238000000926 separation method Methods 0.000 claims abstract description 45
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 24
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 claims description 13
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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Abstract
The invention provides a method for regenerating waste transformer oil. The method comprises the following steps: firstly, filtering waste transformer oil by using filter cloth and filter paper respectively, heating, introducing the waste transformer oil into a pre-refining reactor bed layer filled with Y-shaped molecular sieve, cooling the waste transformer oil flowing out of the lower part of the pre-refining reactor, mixing the waste transformer oil with water, entering a static mixer, separating the mixture by using a sedimentation separation tank, mixing the separated waste transformer oil and hydrogen, entering the upper part of a hydrogenation reactor filled with a hydrogenation catalyst for hydrogenation reaction, flowing out of the lower part of the hydrogenation reactor after the reaction is finished, entering a high-pressure separation tank for separation, and then entering a stripping tower for extraction to obtain regenerated transformer oil. The treatment method can reduce the color of the waste transformer oil from No. 3-5 to below 1, the acid value is reduced, the loss tangent value of the medium is also greatly reduced, the oxidation stability is also obviously improved, other aspects are also improved, and the service life of the hydrogenation catalyst is greatly prolonged.
Description
Technical Field
The invention belongs to the field of petroleum refining production, and particularly relates to a method for regenerating waste transformer oil.
Background
The transformer oil mainly plays roles of insulation, cooling, arc extinction and the like in electrical equipment such as a transformer, the transformer oil is subjected to long-term operation in the transformer, and acid sludge is generated by oxidation under the action of metal catalysts such as high temperature, oxygen, copper and the like, so that the acid value of the transformer oil is increased, the dielectric loss factor is increased, the breakdown voltage is reduced, the insulation effect is lost, and the aged transformer oil needs to be replaced in order to ensure the normal operation of the transformer, so that the replaced transformer oil becomes waste transformer oil. According to statistics, 5 ten thousand tons of waste transformer oil produced in China every year can generate larger economic benefit if recycling and regenerating are carried out, and the method also accords with the concept of green, low carbon, circulation and sustainable development advocated in China at present.
At present, the regeneration of the waste transformer oil mainly comprises the following processes, namely, the adsorption and regeneration process of the waste transformer oil, wherein suspended matters and polar compounds in the waste transformer oil are adsorbed by a special adsorbent, so that the color of the waste transformer oil is improved, the dielectric loss factor is reduced, and the breakdown voltage is improved; secondly, an acid-base refining-clay treatment combined process is adopted, and the process can treat the waste transformer oil with serious ageing to reach the standard of new transformer oil, but the process generates a large amount of pollutants such as waste acid and base, waste water, waste clay and the like and is eliminated; thirdly, a process of filtering, solvent refining and clay supplementing refining is adopted, and the process can treat the waste transformer oil with serious ageing to reach the standard of new transformer oil, but generates a lot of waste clay pollutants; therefore, the development of a new transformer oil regeneration process has important significance.
Disclosure of Invention
In order to solve the problems existing in the prior art in the regeneration of the waste transformer oil, the invention provides a method for regenerating the waste transformer oil, and the transformer oil treated by the method reaches the standard of new transformer oil, has the advantages of simple process, no secondary waste generation, low processing cost and the like, and can prolong the service life of a catalyst.
In order to achieve the technical effect, the invention provides a method for regenerating waste transformer oil, which is characterized by comprising the following steps:
(1) Filtering the waste transformer oil by using filter cloth and filter paper respectively;
(2) Heating the filtered waste transformer oil to 150-250 ℃, introducing the waste transformer oil into a pre-refining reactor bed layer of the Y-type molecular sieve after filling, entering from the upper part of the pre-refining reactor, and flowing out from the lower part, wherein the airspeed is 0.5-2h -1 ；
(3) Cooling the waste transformer oil flowing out of the lower part of the pre-refining reactor in the step (2) to 80-130 ℃, mixing with water, entering a static mixer, then entering a sedimentation separation tank, flowing out the waste transformer oil from the top of the sedimentation separation tank, and flowing out water from the bottom of the sedimentation separation tank;
(4) Mixing the waste transformer oil and hydrogen flowing out of the top of the sedimentation separation tank in the step (3) and entering the upper part of a hydrogenation reactor filled with a hydrogenation catalyst for hydrogenation reaction, wherein the conditions of the hydrogenation reaction are as follows: airspeed 1-3h -1 The reaction pressure is 2-6MPa, the reaction temperature is 200-300 ℃, and the hydrogen-oil volume ratio is 200-300Nm 3 /m 3 The method comprises the steps of carrying out a first treatment on the surface of the After the reaction is finished, the catalyst flows out from the lower part of the hydrogenation reactor and enters a high-pressure separation tank;
(5) The gas at the top of the high-pressure separation tank returns to the hydrogenation reactor through a circulating hydrogen compressor, transformer oil flowing out from the bottom of the high-pressure separation tank enters the upper part of the stripping tower, and nitrogen is introduced into the lower part of the stripping tower for stripping; the oil flowing out from the bottom of the stripping tower is regenerated transformer oil.
The invention has the preferable technical scheme that: the Y-type molecular sieve filled in the prerefining reactor in the step (2) is a rare earth Y-type molecular sieve or an HY molecular sieve.
The invention has the preferable technical scheme that: the reaction conditions entering the hydrogenation reactor in the step (4) are as follows: space velocity of 2-3h -1 The reaction pressure is 4MPa, and the reaction temperature is 220-280 ℃.
The invention has the preferable technical scheme that: the steps are as follows(4) The middle hydrogenation reactor contains Ni-Mo-W/Al 2 O 3 Is a hydrogenation catalyst of (a).
The invention has the preferable technical scheme that: the hydrogenation catalyst in the step (4) comprises 2-4% of nickel, 6-8% of molybdenum, 3-5% of tungsten and gamma-Al as a carrier 2 O 3 。
The invention has the preferable technical scheme that: : the hydrogenation catalyst in the step (4) is presulfided by adopting diesel oil containing carbon disulfide for 14-16 hours before being used, the presulfiding temperature is 225-235 ℃, and the hydrogen oil volume ratio is 500Nm 3 /m 3 。
The invention has the preferable technical scheme that: the stripping tower in the step (5) is a plate tower, and the volume ratio of the nitrogen for stripping to the waste transformer oil at normal temperature is 5-20Nm 3 /m 3 。
The invention has the preferable technical scheme that: the pre-refining reactor bed fixed bed reactor in the step (2) has the height-diameter ratio of 3-7:1, and the catalyst is spherical or bar-shaped; the sedimentation separation tank in the step (3) and the high-pressure separation tank in the step (4) adopt vertical structures, stainless steel is used as materials, and the volume of the separation tank ensures that the residence time of oil-water in the separation tank exceeds 20 minutes; the hydrogenation reactor in the step (4) is a vertical fixed bed reactor, and hydrogen enters from an inlet at the top of the reactor; the stripping tower in the step (5) adopts a plate tower, a sieve tray or a bubble cap tray is arranged, and a nitrogen inlet is arranged at the bottom.
The purpose of the filtering by using the filter cloth and the filter paper in the invention is to remove particulate matters, rust and the like, and the filter cloth and the filter paper are all conventional filtering devices. The ratio of the water to the waste transformer oil is 0.03-0.2.
The application provides a hydrogenation regeneration process of waste transformer oil, which removes polar compounds in the waste transformer oil through hydrogenation reaction under the action of a catalyst to reach the standard of new transformer oil, and has the advantages of simple process, no secondary waste generation, low processing cost and the like. In the hydrogenation process, impurities in the raw materials have a great influence on the hydrogenation catalyst of the transformer oil, for example, when the waste transformer oil contains metal ions such as copper ions, iron ions and the like, the pores of the hydrogenation catalyst are blocked, so that the deactivation is caused, and the service life of the catalyst is shortened; some waste transformer oil contains chlorides, such as polychlorinated biphenyl, which corrode hydrogenation equipment and also affect a hydrogenation catalyst, so that a small amount of chlorides and metal ions are removed by a pre-refining method, and the chlorides can be decomposed and adsorbed on the molecular sieve by the Y molecular sieve in the pre-refining reactor, and meanwhile, the metal ions are adsorbed on the molecular sieve, so that the service life of the catalyst can be prolonged.
The treatment method can reduce the color of the waste transformer oil from 3-5 to below 1, the acid value from more than 0.5mgKOH/g to less than 0.01mgKOH/g, the dielectric loss tangent (dielectric loss for short) can be greatly reduced, the oxidation stability is obviously improved, other aspects are improved, and the service life of the hydrogenation catalyst is greatly prolonged.
Drawings
Fig. 1 is a process flow diagram of the present application.
In the figure: 1. a raw material oil tank; 2. a high pressure oil pump; 3. a heater; 4. a pre-refining reactor; 5. a static mixer; 6. a sedimentation separation tank; 7. a hydrogenation reactor; 8. a high pressure separator tank; 9. a recycle hydrogen compressor; 10. a valve; 11. a stripping column; 12. a cooler; 13. a bottom oil pump; 14. a light oil tank.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The specific process of the present invention will be described below with reference to examples. The hydrogenation reactor of the following example was filled with a catalyst containing Ni-Mo-W/Al 2 O 3 The weight of nickel in the hydrogenation catalyst is 2-4%, the weight of molybdenum is 6-8%, and the weight of tungsten is 3-5%The carrier is gamma-Al 2 O 3 . The stripping tower is a plate-type tower, and the volume ratio of nitrogen for stripping to waste transformer oil at normal temperature is 5-20Nm 3 /m 3 . The process flow is specifically shown in fig. 1, the pre-refining reactor 4 in fig. 1 is a fixed bed reactor, the height-diameter ratio is generally 3-7:1, and the catalyst can be spherical or bar-shaped. The sedimentation separation tank 6 and the high-pressure separation tank 8 are both of vertical structures, 316L stainless steel is used as a material, and the volume of the separation tank is generally used for ensuring that the residence time of oil and water in the separation tank exceeds 20 minutes. The hydrogenation reactor 7 is generally a vertical fixed bed reactor, and has low reaction heat because of low hydrogen consumption, and the hydrogen only needs to enter from the inlet at the top of the reactor without setting middle section cold hydrogen to enter. The stripping tower 11 adopts a plate tower, a sieve tray can be adopted, a bubble cap tray can also be adopted, a nitrogen inlet is arranged at the bottom, and nitrogen stripping is adopted.
The method for regenerating the waste transformer oil provided in the embodiment 1 specifically aims at a certain waste transformer oil, wherein the transformer oil has been used for 12 years, the color number is 2, the metal content is 4 mug/g, the dielectric loss is 0.038, the breakdown voltage is 45kV, and the chlorine content is 12 mug/g. The process flow is shown in figure 1. In laboratory, HY molecular sieve column is used as pre-refining reactor with height of 20cm and diameter of 20mm and the hydrogenation catalyst contains Ni-Mo-W/Al 2 O 3 The hydrogenation catalyst of (1) contains 2% by weight of nickel, 8% by weight of molybdenum and 3% by weight of tungsten, and the carrier is gamma-Al 2 O 3 The hydrogenation catalyst was charged into a micro hydrogenation reactor and then presulfided with carbon disulphide-containing diesel fuel for 15 hours at a presulfiding temperature of 230 ℃ and a hydrogen to oil volume ratio of 500Nm 3 /m 3 . After pre-vulcanization, the waste transformer oil is used as raw oil for feeding, and the method comprises the following steps:
(1) Filtering the waste transformer oil by using filter cloth and filter paper respectively;
(2) Heating the filtered waste transformer oil to 150 ℃, introducing the waste transformer oil into a bed layer of a pre-refining reactor filled with HY molecular sieve columns, entering from the upper part of the pre-refining reactor, flowing out from the lower part, and having a space velocity of 0.5h -1 ；
(3) Cooling the waste transformer oil flowing out of the bottom of the pre-refining reactor in the step (2) to 80-130 ℃, mixing with water, entering a static mixer, then entering a sedimentation separation tank, flowing out of the top of the sedimentation separation tank into waste transformer oil, and flowing out of the bottom of the sedimentation separation tank into water, wherein the chlorine content in the flowing-out waste transformer oil is measured to be 2 mug/g, and the metal content is measured to be 1 mug/g;
(4) Mixing the waste transformer oil and hydrogen gas which are discharged from the step (3) according to the volume ratio of 500Nm of hydrogen oil 3 /m 3 Airspeed of 3h -1 Entering the upper part of a hydrogenation reactor, flowing out from the lower part of the hydrogenation reactor, entering a high-pressure separation tank, and enabling the temperature of the hydrogenation reactor to be 200 ℃;
(5) The gas at the top of the separation tank returns to the hydrogenation reactor through a circulating hydrogen compressor;
(6) The materials at the bottom of the separating tank enter the upper part of a stripping tower, the temperature of the stripping tower is 150 ℃, and nitrogen is introduced into the lower part of the stripping tower;
(7) The oil flowing out from the bottom of the stripping tower is regenerated transformer oil.
The regenerated transformer oil has the color of No. 0.5, the metal content of 0.1 mug/g, the dielectric loss of 0.0014, the breakdown voltage of 44kV, the chlorine content of 0 mug/g, the flash point of 145 ℃, and the oxidation stability of qualified, and meets the standard requirements of the transformer oil.
The method for regenerating the waste transformer oil provided in example 2 is the same as that of example 1, a Rare Earth Y (REY) molecular sieve column is adopted as a pre-refining reactor in a laboratory, and a hydrogenation catalyst comprises Ni-Mo-W/Al 2 O 3 The hydrogenation catalyst of (1) contains nickel 4 wt%, molybdenum 6 wt%, tungsten 5 wt%, and gamma-Al as carrier 2 O 3 The hydrogenation catalyst was charged into a micro hydrogenation reactor and then presulfided with carbon disulphide-containing diesel fuel for 15 hours at a presulfiding temperature of 230 ℃ and a hydrogen to oil volume ratio of 500Nm 3 /m 3 . After pre-vulcanization, the waste transformer oil is used as raw oil for feeding, and the method comprises the following steps:
(1) Filtering the waste transformer oil by using filter cloth and filter paper respectively;
(2) Heating the filtered waste transformer oil to 250 ℃, introducing the waste transformer oil into a pre-refining reactor bed filled with REY molecular sieve, entering from the upper part of the pre-refining reactor, and flowing out from the lower part, wherein the airspeed is 1.5h -1 ；
(3) Cooling the waste transformer oil flowing out of the bottom of the pre-refining reactor in the step (2) to 80-130 ℃ and mixing with water, then entering a sedimentation separation tank, wherein the waste transformer oil flowing out of the top of the sedimentation separation tank flows out of the bottom of the sedimentation separation tank, and the chlorine content in the discharged waste transformer oil is 1.5 mug/g and the metal content is 1.1 mug/g;
(4) Mixing the discharged waste transformer oil with hydrogen gas according to the volume ratio of 500Nm 3 /m 3 Airspeed of 2h -1 Entering the upper part of a hydrogenation reactor, flowing out from the lower part of the hydrogenation reactor, entering a high-pressure separation tank, and enabling the temperature of the hydrogenation reactor to be 300 ℃;
(5) The gas at the top of the separation tank returns to the hydrogenation reactor through a circulating hydrogen compressor;
(6) The materials at the bottom of the separating tank enter the upper part of a stripping tower, the temperature of the stripping tower is 150 ℃, and nitrogen is introduced into the lower part of the stripping tower;
(7) The oil flowing out from the bottom of the stripping tower is regenerated transformer oil.
The regenerated transformer oil has the color of No. 0.6, the metal content of 0.1 mug/g, the dielectric loss of 0.0016, the breakdown voltage of 45kV, the chlorine content of 0 mug/g, the flash point of 147 ℃, and the oxidation stability of qualified, and meets the standard requirements of the transformer oil.
The method for regenerating the waste transformer oil provided in example 3 is specifically the same as in example 1, wherein an HY molecular sieve column is used as a pre-refining reactor in a laboratory, and a hydrogenation catalyst comprises Ni-Mo-W/Al 2 O 3 The hydrogenation catalyst of (1) contains nickel 5 wt%, molybdenum 7 wt%, tungsten 4 wt%, and gamma-Al as carrier 2 O 3 Loading hydrogenation catalyst into micro hydrogenation reactor, presulfiding with diesel oil containing carbon bisulfide for 15 hr at presulfiding temperature of 230deg.C, and hydrogen oil volumeAt a ratio of 500Nm 3 /m 3 . After pre-vulcanization, the waste transformer oil is used as raw oil for feeding, and the method comprises the following steps:
(1) Filtering the waste transformer oil by using filter cloth and filter paper respectively;
(2) Heating the filtered waste transformer oil to 200 ℃, introducing the waste transformer oil into a bed layer of a prerefining reactor containing HY type molecular sieve, entering from the upper part of the prerefining reactor, and flowing out from the lower part of the prerefining reactor, wherein the airspeed is 2.0h -1 ；
(3) Cooling the waste transformer oil flowing out of the bottom of the pre-refining reactor in the step (2) to 80-130 ℃, mixing with water, entering a static mixer, then entering a sedimentation separation tank, flowing out of the top of the sedimentation separation tank into waste transformer oil, and flowing out of the bottom of the sedimentation separation tank into water, wherein the chlorine content in the flowing-out waste transformer oil is 1 mug/g and the metal content is 0.7 mug/g;
(4) Mixing the waste transformer oil and hydrogen gas which are discharged from the step (3) according to the volume ratio of 500Nm of hydrogen oil 3 /m 3 Airspeed 1h -1 Entering the upper part of a hydrogenation reactor, flowing out from the lower part of the hydrogenation reactor, entering a separation tank, and controlling the temperature of the hydrogenation reactor to 240 ℃;
(5) The gas at the top of the separation tank returns to the hydrogenation reactor through a circulating hydrogen compressor;
(6) The materials at the bottom of the separating tank enter the upper part of a stripping tower, the temperature of the stripping tower is 150 ℃, and nitrogen is introduced into the lower part of the stripping tower;
(7) The oil flowing out from the bottom of the stripping tower is regenerated transformer oil.
The regenerated transformer oil has the color of No. 0.5, the metal content of 0 mug/g, the dielectric loss of 0.0015, the breakdown voltage of 45kV, the chlorine content of 0 mug/g, the flash point of 148 ℃, and the oxidation stability of qualified, and meets the standard requirements of the transformer oil.
The inventors of the present application also conducted the following experimental studies on the conditions of hydrogenation reaction in the above-described method:
test one: influence of reaction pressure; at a constant reaction temperature of 220 ℃ and a space velocity of 3h -1 The effect of the reaction pressure at 1MPa, 2MPa, 4MPa and 6MPa was examined, and the results are shown in Table 1:
TABLE 1 influence of reaction pressure on treatment of pressure-swing oils
As can be seen from Table 1, the chromaticity of the hydrogenated transformer oil is reduced from 3 to below 1, and after the reaction pressure reaches 4MPa, the color is basically water white, which indicates that the reaction pressure is 1-6MPa, and the hydrofining effect can be realized; in view of the complexity of the processing of the feedstock, and the service life of the industrial catalyst, it is recommended that the reaction pressure for industrial hydrogenation is 3-4MPa.
And (2) testing II: the reaction temperature influence; at a constant reaction pressure of 4MPa and a space velocity of 3h -1 Hydrogen to oil ratio 500Nm 3 /m 3 The effect of the reaction temperature was examined and the results are shown in Table 2.
TABLE 2 influence of reaction temperature on treatment of pressure-swing oil
As can be seen from Table 2, the hydrogenated oil had a hue of less than 1 at temperatures up to 200℃with a hue of less than 260 ℃.
And (3) test III: at a constant reaction pressure of 4MPa, a reaction temperature of 220 ℃ and a hydrogen-oil ratio of 500Nm 3 /m 3 The effect of reaction space velocity was examined and the results are shown in Table 3:
TABLE 3 influence of reaction space velocity on pressure swing oil treatment
As can be seen from Table 3, at a space velocity of 1-4h -1 The reaction pressure is 4MPa, the reaction temperature is 220 ℃, and the hydrogen-oil ratio is 500Nm 3 /m 3 The color of the hydrogenated oil is basically below 1.0, and the space velocity is considered to be 2-3h in consideration of the service life of the catalyst and the size of the reactor -1 Is suitable.
And (3) testing four: the influence of the hydrogen-oil ratio was examined to determine the hydrogen-oil ratio of 200, 300, 500Nm 3 /m 3 The results are shown in Table 4.
TABLE 4 Hydrogen to oil ratio versus pressure swing oil treatment effect
As can be seen from Table 4, the hydrogen/oil ratio was 200, 300, 500Nm 3 /m 3 The hydrogenated oil has a color of less than 1, and the hydrogen-oil ratio is 500Nm 3 /m 3 The chromaticity is smaller, and the hydrogen-oil ratio is selected to be 200-300Nm in view of the increase in energy consumption caused by the larger hydrogen-oil ratio 3 /m 3 。
As can be seen from the above study, the optimal hydrogenation reaction conditions are: space velocity of 2-3h -1 The reaction pressure is 4MPa, the reaction temperature is 220-280 ℃, and the hydrogen-oil ratio is 200-300Nm 3 /m 3 。
The inventors of the present application have found that under optimal reaction conditions: airspeed of 3h -1 The reaction pressure was 4MPa, the reaction temperature was 220℃and the hydrogen-to-oil ratio was 300Nm 3 /m 3 5L of hydrogenated oil was prepared, and the hydrogenated oil was subjected to property and yield analysis, and the results are shown in Table 5:
TABLE 5 hydrogenated oil mass to mass ratio
As can be seen from table 5, the properties of the hydrogenated oil are substantially capable of meeting the requirements of GB 2536-2011.
From the above examples and test data, it can be seen that the waste transformer oil treated by the method of the invention can basically meet the transformer oil standard requirements and can be reused.
The foregoing description is, of course, merely one embodiment of the invention, and it should be noted that modifications and adaptations of the invention will occur to one skilled in the art and are intended to be comprehended within the scope of the invention as defined in the following claims.
Claims (8)
1. A method for regenerating waste transformer oil, the method comprising the steps of:
(1) Filtering the waste transformer oil by using filter cloth and filter paper respectively;
(2) Heating the filtered waste transformer oil to 150-250 ℃, introducing the waste transformer oil into a pre-refining reactor bed layer of the Y-type molecular sieve after filling, entering from the upper part of the pre-refining reactor, and flowing out from the lower part, wherein the airspeed is 0.5-2h -1 ；
(3) Cooling the waste transformer oil flowing out of the lower part of the pre-refining reactor in the step (2) to 80-130 ℃, mixing with water, entering a static mixer, then entering a sedimentation separation tank, flowing out the waste transformer oil from the top of the sedimentation separation tank, and flowing out water from the bottom of the sedimentation separation tank;
(4) Mixing the waste transformer oil and hydrogen flowing out of the top of the sedimentation separation tank in the step (3) and entering the upper part of a hydrogenation reactor filled with a hydrogenation catalyst for hydrogenation reaction, wherein the conditions of the hydrogenation reaction are as follows: airspeed 1-3h -1 The reaction pressure is 2-6MPa, the reaction temperature is 200-300 ℃, and the hydrogen-oil volume ratio is 200-300Nm 3 /m 3 The method comprises the steps of carrying out a first treatment on the surface of the After the reaction is finished, the catalyst flows out from the lower part of the hydrogenation reactor and enters a high-pressure separation tank;
(5) The gas at the top of the high-pressure separation tank returns to the hydrogenation reactor through a circulating hydrogen compressor, transformer oil flowing out from the bottom of the high-pressure separation tank enters the upper part of the stripping tower, and nitrogen is introduced into the lower part of the stripping tower for stripping; the oil flowing out from the bottom of the stripping tower is regenerated transformer oil.
2. The method for regenerating a waste transformer oil according to claim 1, wherein: the Y-type molecular sieve filled in the prerefining reactor in the step (2) is a rare earth Y-type molecular sieve or an HY molecular sieve.
3. The method for regenerating a waste transformer oil according to claim 1, wherein: the reaction conditions entering the hydrogenation reactor in the step (4) are as follows: space velocity of 2-3h -1 The reaction pressure is 4MPa, and the reaction temperature is 220-280 ℃.
4. The method for regenerating a waste transformer oil according to claim 1, wherein: the hydrogenation reactor in the step (4) contains Ni-Mo-W/Al 2 O 3 Is a hydrogenation catalyst of (a).
5. The method for regenerating a waste transformer oil according to claim 1, wherein: the hydrogenation catalyst in the step (4) comprises 2-4% of nickel, 6-8% of molybdenum, 3-5% of tungsten and gamma-Al as a carrier 2 O 3 。
6. The method for regenerating a waste transformer oil according to claim 1, wherein: the hydrogenation catalyst in the step (4) is presulfided by adopting diesel oil containing carbon disulfide for 14-16 hours before being used, the presulfiding temperature is 225-235 ℃, and the hydrogen oil volume ratio is 500Nm 3 /m 3 。
7. The method for regenerating a waste transformer oil according to claim 1, wherein: the stripping tower in the step (5) is a plate tower, and the volume ratio of the nitrogen for stripping to the waste transformer oil at normal temperature is 5-20Nm 3 /m 3 。
8. The method for regenerating a waste transformer oil according to claim 1, wherein: the pre-refining reactor bed fixed bed reactor in the step (2) has the height-diameter ratio of 3-7:1, and the catalyst is spherical or bar-shaped; the sedimentation separation tank in the step (3) and the high-pressure separation tank in the step (4) adopt vertical structures, stainless steel is used as materials, and the volume of the separation tank ensures that the residence time of oil-water in the separation tank exceeds 20 minutes; the hydrogenation reactor in the step (4) is a vertical fixed bed reactor, and hydrogen enters from an inlet at the top of the reactor; the stripping tower in the step (5) adopts a plate tower, a sieve tray or a bubble cap tray is arranged, and a nitrogen inlet is arranged at the bottom.
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