CN115820298A - Transformer oil production process - Google Patents
Transformer oil production process Download PDFInfo
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- CN115820298A CN115820298A CN202211556233.0A CN202211556233A CN115820298A CN 115820298 A CN115820298 A CN 115820298A CN 202211556233 A CN202211556233 A CN 202211556233A CN 115820298 A CN115820298 A CN 115820298A
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- oil
- transformer oil
- transformer
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- hydrogenation
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 239000003921 oil Substances 0.000 claims abstract description 101
- 238000000034 method Methods 0.000 claims abstract description 36
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 33
- 230000008569 process Effects 0.000 claims abstract description 28
- 239000002199 base oil Substances 0.000 claims abstract description 24
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 19
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000002283 diesel fuel Substances 0.000 claims abstract description 15
- 238000005194 fractionation Methods 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- 239000003963 antioxidant agent Substances 0.000 claims abstract description 6
- 230000003078 antioxidant effect Effects 0.000 claims abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000009835 boiling Methods 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims description 6
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims description 6
- 229910052794 bromium Inorganic materials 0.000 claims description 6
- 239000011261 inert gas Substances 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims 3
- 238000007670 refining Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000004508 fractional distillation Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 13
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 9
- 239000007789 gas Substances 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 241001122767 Theaceae Species 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- -1 benzene series aromatic hydrocarbons Chemical class 0.000 description 1
- CREMABGTGYGIQB-UHFFFAOYSA-N carbon carbon Chemical compound C.C CREMABGTGYGIQB-UHFFFAOYSA-N 0.000 description 1
- 239000011203 carbon fibre reinforced carbon Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002845 discoloration Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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Abstract
The invention discloses a production process of transformer oil, which comprises the following steps: (1) a hydrorefining step: taking hydrocracking diesel oil as a raw material, sending the hydrocracking diesel oil to a hydrogenation reaction unit, mixing with circulating hydrogen after heat exchange and temperature rise, sending to a heating furnace, heating by the heating furnace, and sending to a hydrogenation reactor for hydrorefining to obtain hydrogenation produced oil; (2) fractional distillation stripping procedure: and (3) sending the hydrogenated oil to a fractionation unit, performing heat exchange and temperature rise, then entering a fractionation tower for reduced pressure fractionation, producing base oil of the transformer oil at the bottom of the tower, and adding an antioxidant to produce a qualified transformer oil product. The invention takes the hydrocracking diesel oil as the raw material, obtains the qualified transformer oil base oil through hydrofining and vacuum fractionation, has simple process route and low requirement on the operation condition of hydrogenation reaction, can extend the processing depth of the traditional hydrocracking device, optimizes the product structure of the traditional refinery and improves the oil refining benefit.
Description
Technical Field
The invention relates to the technical field of preparation of transformer oil, in particular to a production process of transformer oil.
Background
The transformer oil is a medium necessary for the operation of the transformer, mainly plays roles of insulation and heat dissipation, and the quality of the transformer oil is directly related to the safe operation of the transformer. The production process of transformer oil develops along with the development of an oil refining process, the existing transformer oil is mainly prepared by taking naphthenic base crude oil or paraffin base crude oil as a raw material through the combination of processes such as reduced pressure distillation, hydrofining, solvent extraction, clay supplement refining and the like, for example, US5167847 relates to a method for producing transformer oil by taking paraffin base oil as a raw material, and the method produces transformer oil components through the processes of hydrocracking, solvent dewaxing and hydrofining; CN1990833A discloses a method for producing extra-high voltage transformer oil, which produces extra-high voltage transformer oil by naphthenic base distillate oil through a two-stage hydrogenation pretreatment process; CN102311785A discloses a method for producing lube base oil by hydrogenation of naphthenic base distillate oil, which uses naphthenic base distillate oil as raw material to produce lube base oil by hydrogenation treatment, hydrogenation pour point depression and hydrogenation refining processes in turn under the condition of high pressure (10-20 MPa); CN106833740A discloses a preparation method of transformer oil base oil, naphthenic base distillate oil is subjected to hydrofining, hydroisomerization and hydrofinishing under the action of a catalyst to obtain three-stage hydrogenation generated oil, and then atmospheric and vacuum fractionation is carried out to obtain the transformer oil base oil.
The above patent methods can prepare qualified transformer oil, but the preparation process is complex, and the prepared transformer oil has a high bromine index, and can be oxidized and yellowed after being stored for a period of time, so that the electrical property is deteriorated.
Disclosure of Invention
In order to solve the technical problems, the invention provides a production process of transformer oil.
The technical scheme adopted by the invention is as follows:
a production process of transformer oil comprises the following steps:
(1) A hydrofining process:
the hydrocracking diesel oil is used as a raw material, the hydrocracking diesel oil is sent to a hydrogenation reaction unit, is mixed with recycle hydrogen after being subjected to heat exchange and temperature rise, and is sent to a heating furnace, and is sent to a hydrogenation reactor after being heated by the heating furnace for hydrogenation refining, so that hydrogenation generated oil is obtained.
(2) A fractionation and stripping process:
and (3) sending the hydrogenated oil to a fractionation unit, performing heat exchange and temperature rise, then entering a fractionating tower for reduced pressure fractionation, producing the transformer oil base oil at the bottom of the tower, and adding an antioxidant to produce a qualified transformer oil product.
The method comprises the steps of taking hydrocracking diesel as a raw material, and removing olefin, sulfide, aromatic hydrocarbon and the like in the raw material oil through hydrofining reaction; and (3) fractionating and stripping the reaction product after hydrorefining to obtain the transformer oil base oil, and adding an antioxidant to obtain a qualified transformer oil product. In addition, the qualified 7# industrial white oil product can be produced by optimizing the operating parameters of the hydrogenation reaction system according to market demands and controlling the aromatic hydrocarbon content of the product to be not more than 5%.
Further preferably, the hydrocracking diesel oil is produced by hydrocracking the normal and vacuum wax oil serving as the raw material.
Further preferably, the bromine index of the hydrocracking diesel oil is 480-900 mgBr/100g, the initial boiling point is 280-290 ℃, the dry point is 360-370 ℃, and the flash point is more than 141 ℃.
Further preferably, the inlet temperature of the hydrogenation reactor is 150-280 ℃, the total temperature rise of the bed layer is not more than 50 ℃, the reaction pressure is 2.3-3.1 MPa, and the hydrogen-oil ratio is 284-426.
By adopting the process, on one hand, the effects of removing olefin, aromatic hydrocarbon and reducing bromine index of a hydrogenation reaction system are ensured, so that the purpose of preventing the transformer oil base oil from oxidative discoloration is achieved, and on the other hand, the yield of a target product and the reasonable service life of the catalyst are also ensured.
More preferably, the inlet temperature of the hydrogenation reactor is 170-280 ℃, the reaction pressure is 2.5-3.1 MPa, and the hydrogen-oil ratio is 325-980.
By adopting the process, the content of aromatic hydrocarbon in the target product is not more than 5 percent, thereby producing the qualified 7# industrial white oil product.
Further preferably, the bottom of the fractionating tower is heated by a heater to control the temperature at the bottom of the fractionating tower to not more than 320 ℃, and the pressure at the top of the fractionating tower to not more than 0.1MPa.
By adopting the process, light components (the initial boiling point is more than 280 ℃) in the transformer oil can be effectively removed to ensure that the initial boiling point and the flash point are qualified; and can prevent the overlarge separation and the overlarge loss of the transformer oil, so that the yield of the base oil of the transformer oil is reduced.
Further preferably, introducing inert gas to the bottom of the fractionating tower to strip the produced transformer oil base oil, and removing light hydrocarbon components and water vapor in the transformer oil base oil; to ensure that the flash point is acceptable.
Further preferably, the inert gas is nitrogen.
The invention has the beneficial effects that: if the transformer oil contains olefin or polycyclic aromatic hydrocarbon, the carbon-carbon unsaturated bond in the transformer oil can seriously affect the stability of the transformer oil and is easy to discolor. But the aromatic hydrocarbon can dissolve oil sludge and gas in the transformer oil and is a natural antioxidant, and the proper aromatic hydrocarbon content and aromatic hydrocarbon type are important guarantees of the transformer oil. The hydrogenation treatment can effectively remove heterocyclic compounds and saturated polycyclic aromatic hydrocarbons, reduce the chroma and improve the oxidation stability of oil products, but can also saturate part of benzene series aromatic hydrocarbons and tea series aromatic hydrocarbons to cause the gas evolution performance of the transformer oil to exceed the standard. Therefore, the method selects proper raw materials, ensures proper aromatic hydrocarbon content and high yield of the product according to the properties of the raw oil and the quality requirements of the product, and is the key point for producing the transformer oil. According to the method, the hydrocracking diesel oil is used as a raw material, the qualified transformer oil base oil is obtained through hydrofining and vacuum fractionation, the process route is simple, the operating condition requirement of hydrogenation reaction is not high, the processing depth of a traditional hydrocracking device can be extended, the product structure of a traditional refinery is optimized, and the oil refining benefit is improved.
Drawings
FIG. 1 is a schematic flow diagram of a process for producing transformer oil according to the present invention.
Detailed Description
The invention is further described below with reference to specific examples to facilitate the understanding of the invention, but the invention is not limited thereby.
Referring to fig. 1, fig. 1 illustrates a process flow of the transformer oil production process of the present invention, but the process flow of the transformer oil production process of the present invention is not limited thereto, the number of hydrogenation reactors of the hydrogenation reaction unit may be one or more, a plurality of hydrogenation reactors may be used in parallel or in series, and when a plurality of hydrogenation reactors are used in series or in parallel, the hydrorefining effect of the present invention can be achieved as long as the inlet temperature of each hydrogenation reactor is controlled to be 150 to 280 ℃, the total bed temperature rise is not more than 50 ℃, the reaction pressure is 2.3 to 3.1MPa, and the hydrogen-oil ratio is 284 to 980. In the process shown in FIG. 1, the number of the hydrogenation heat exchangers and the fractionation heat exchangers and the heat exchange method are set to save energy, and are not related to the hydrorefining effect of the present invention.
The invention provides five specific examples, namely example 1-example 5, of transformer oil production by using the process flow shown in fig. 1, wherein the process steps are as follows:
(1) A hydrofining process:
the hydrocracking diesel oil 810 from the hydrocracking device firstly enters a buffer tank 21, is sent to a heat exchanger 31 through a pump 11, is mixed with circulating hydrogen 816, is sent to a heating furnace 01 to be heated to the required reaction temperature, enters a hydrogenation reactor 41 to be subjected to hydrofining, and enters a separation tank 22 after the reaction produced oil exchanges heat through a hydrogenation heat exchanger 31. The liquid phase oil at the bottom of the separating tank is used as the feed of the fractionating tower 51, the gas phase part at the top of the separating tank discharges waste hydrogen 815, part of the waste hydrogen passes through the separating tank 25, is pressurized by the circulator 61 and then enters the separating tank 26, the waste hydrogen is mixed with the raw materials after being cut by the separating tank 26 and then enters the heating furnace, wherein the new hydrogen 811 and the recycle hydrogen are mixed in the separating tank 26 and then are replenished into the system.
(2) A fractionation and stripping process:
the liquid phase oil at the bottom of the separation tank 22 enters a fractionating tower 51 after heat exchange by a heat exchanger 32, part of the bottom oil of the fractionating tower 51 is heated by a reboiling furnace 02 and then returns to the fractionating tower 51, light components with the initial boiling point less than 280 ℃ are removed from the top of the fractionating tower 51, part of the bottom oil of the fractionating tower is used as a qualified transformer oil base oil 813 or 7# industrial white oil production device after heat exchange and temperature reduction by the fractionating heat exchanger 32, the detected properties of the transformer oil base oil 813 are shown in a table 3, and the detected properties of the 7# industrial white oil are shown in a table 5; after the antioxidant is added into the base oil of the transformer oil produced at the bottom of the tower, a qualified transformer oil product is produced, the properties of the transformer oil are shown in table 4, light components at the top of the fractionating tower 51 are cooled by a cooler 33 and then enter a reflux tank 23 at the top of the tower, a gas phase 814 separated by the reflux tank enters a torch system, a part of a liquid phase 812 is refluxed, and a part of the liquid phase is sent out of the device; and introducing nitrogen 817 to the bottom of the fractionating tower to strip the generated transformer oil base oil, and removing light hydrocarbon components and water vapor in the transformer oil base oil.
The main properties of the raw materials of examples 1 to 5 are shown in Table 1, the process conditions are shown in Table 2, the properties of the transformer oil base oil are shown in Table 3, the properties of the finished transformer oil are shown in Table 4, and the properties of the finished No. 7 industrial white oil are shown in Table 5.
Table 1 main properties of raw materials of example 1 to example 5
| Analysis item | Unit of | Example 1 | Example 2 | Example 3 | Example 4 | Example 5 |
| Bromine index | mgBr/100g | 484 | 900 | 580 | 359 | 273 |
| Initial boiling point | ℃ | 284 | 288 | 286 | 289 | 283 |
| Dried cake | ℃ | 362 | 368 | 365 | 364 | 368 |
| Flash point | ℃ | ＞142 | ＞142 | ＞142 | ＞142 | ＞141 |
Table 2 process conditions and target product yields of examples 1 to 5
Table 3 main properties of the transformer oil base oils of examples 1 to 5
| Analysis item | Unit of | Example 1 | Example 2 | Example 3 | Example 4 | Example 5 |
| Bromine index | mgBr/100g | 180 | 135 | 38 | 65 | 55 |
| Initial boiling point | ℃ | 285 | 285 | 288 | 285 | 283 |
| Dried cake | ℃ | 362 | 363 | 364 | 364 | 367 |
| Flash point | ℃ | 142 | 142 | 142 | 141 | 137 |
Table 4 main properties of transformer oils of examples 1 to 3
Table 5 main properties of 7# technical white oils of examples 4 to 5
The foregoing is only a preferred embodiment of the present invention, and it should be noted that those skilled in the art can make various improvements and modifications without departing from the principle of the present invention, and the improvements and modifications are also within the protection scope of the present invention.
Claims (8)
1. The production process of the transformer oil is characterized by comprising the following steps of:
(1) A hydrofining process:
taking hydrocracking diesel oil as a raw material, sending the hydrocracking diesel oil to a hydrogenation reaction unit, mixing the hydrocracking diesel oil with circulating hydrogen after heat exchange and temperature rise, sending the mixture to a heating furnace, heating the mixture by the heating furnace, and sending the mixture to a hydrogenation reactor for hydrorefining to obtain hydrogenation generated oil;
(2) A fractionation and stripping process:
and (3) sending the hydrogenated oil to a fractionation unit, performing heat exchange and temperature rise, then entering a fractionating tower for reduced pressure fractionation, producing the transformer oil base oil at the bottom of the tower, and adding an antioxidant to produce a qualified transformer oil product.
2. The process for producing transformer oil according to claim 1, wherein the hydrocracked diesel oil is a diesel oil produced by hydrocracking an atmospheric and vacuum wax oil as a raw material.
3. The process for producing transformer oil according to claim 2, wherein the hydrocracked diesel oil has a bromine index of 480 to 900mgBr/100g, an initial boiling point of 280 to 290 ℃, a dry point of 360 to 370 ℃ and a flash point of more than 141 ℃.
4. The production process of the transformer oil according to claim 1, wherein the inlet temperature of the hydrogenation reactor is 150-280 ℃, the total temperature rise of the bed layer is no more than 50 ℃, the reaction pressure is 2.3-3.1 MPa, and the hydrogen-oil ratio is 284-426.
5. The process for producing transformer oil according to claim 1, wherein the inlet temperature of the hydrogenation reactor is 170-280 ℃, the reaction pressure is 2.5-3.1 MPa, and the hydrogen-oil ratio is 325-980.
6. The production process of transformer oil according to claim 1, characterized in that the temperature at the bottom of the fractionating tower is controlled to not more than 320 ℃ by heating through a heater, and the pressure at the top of the fractionating tower is not more than 0.1MPa.
7. The process of claim 1, wherein the inert gas is introduced into the bottom of the fractionating tower to strip the produced transformer oil base oil and remove the light hydrocarbon components and water vapor from the transformer oil base oil.
8. The process for producing transformer oil according to claim 1, wherein the inert gas is nitrogen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211556233.0A CN115820298A (en) | 2022-12-06 | 2022-12-06 | Transformer oil production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211556233.0A CN115820298A (en) | 2022-12-06 | 2022-12-06 | Transformer oil production process |
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| CN115820298A true CN115820298A (en) | 2023-03-21 |
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| CN202211556233.0A Pending CN115820298A (en) | 2022-12-06 | 2022-12-06 | Transformer oil production process |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040206668A1 (en) * | 2000-05-19 | 2004-10-21 | China Petroleum Corporation, Fushun Research Institute of Petroleum and Petroch | Medium-pressure hydrocracking process |
| US20120251403A1 (en) * | 2011-03-31 | 2012-10-04 | Uop Llc | Apparatus for producing diesel |
| CN103773476A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing high-viscosity-index lubricant base oil by hydrocracking-isodewaxing combination |
| CN103789019A (en) * | 2012-11-05 | 2014-05-14 | 中国石油化工股份有限公司 | Method for hydrogenation of medium-low temperature coal tar to produce transformer oil base oil |
-
2022
- 2022-12-06 CN CN202211556233.0A patent/CN115820298A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040206668A1 (en) * | 2000-05-19 | 2004-10-21 | China Petroleum Corporation, Fushun Research Institute of Petroleum and Petroch | Medium-pressure hydrocracking process |
| US20120251403A1 (en) * | 2011-03-31 | 2012-10-04 | Uop Llc | Apparatus for producing diesel |
| CN103773476A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing high-viscosity-index lubricant base oil by hydrocracking-isodewaxing combination |
| CN103789019A (en) * | 2012-11-05 | 2014-05-14 | 中国石油化工股份有限公司 | Method for hydrogenation of medium-low temperature coal tar to produce transformer oil base oil |
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