CN115505426A - System and method for preparing special oil for cold liquid from naphthenic base distillate oil - Google Patents
System and method for preparing special oil for cold liquid from naphthenic base distillate oil Download PDFInfo
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- CN115505426A CN115505426A CN202211215227.9A CN202211215227A CN115505426A CN 115505426 A CN115505426 A CN 115505426A CN 202211215227 A CN202211215227 A CN 202211215227A CN 115505426 A CN115505426 A CN 115505426A
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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Abstract
The invention discloses a system and a method for preparing special cold liquid oil by naphthenic base distillate oil, wherein the system comprises a raw oil buffer tank, the raw oil buffer tank is sequentially connected with a filter, a hydrogenation mixer, a reaction feeding heating furnace, a hydrotreating reactor, a hydrodewaxing reactor, a hydrogenation complementary refining reactor, an air cooler, a high-pressure separator, a low-pressure separator and a fractionating tower according to the material flowing direction, the fractionating tower is provided with a tower top outlet, an upper side outlet, a lower side outlet and a tower bottom outlet, the tower top outlet is connected with a naphtha storage tank, the upper side outlet is connected with a special cold liquid oil storage tank 1#, the lower side outlet is connected with a special cold liquid oil storage tank 2#, and the tower bottom outlet is connected with a special cold liquid oil storage tank 3 #. The invention adopts the total hydrogen type high pressure hydrogenation technology, which comprises three combined process flows of hydrotreating, medium pressure hydrodewaxing and non-noble metal supplementing and refining, and the product fractionation to prepare the special oil for cold liquid.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a system and a method for preparing special oil for cold liquid from naphthenic base distillate oil.
Background
The refrigerating machine oil is special lubricating oil for refrigerating compressor and is important component for determining and influencing the refrigerating function and effect of refrigerating system. In the working process of the refrigeration compressor, the refrigerant is decompressed and evaporated to obtain low temperature, and the refrigerating machine oil lubricates working parts of the refrigeration device. Therefore, refrigerator oils are required to have strong lubricity, low-temperature fluidity, oxidation stability and high flash point. And the refrigerator oil and the refrigerant are required to be mutually soluble, the chemical stability of the product is excellent, and the service life of the product can be the same as that of a compressor. Since the refrigerating machine oil must be in a low-temperature environment of a refrigerating system for a long time, raw materials for producing the refrigerating machine oil must be selected. Depending on the production raw materials, the common refrigerating machine oils can be classified into two types: mineral oils and synthetic oils. The mineral oil type refrigerating machine oil on the market at present is basically naphthenic base refrigerating machine oil. Other types of mineral oils, while producing very low pour points, have poor miscibility with refrigerants and are not normally circulated in the compressor system, which can lead to severe lubrication failures. One of the main uses of naphthenic oils is in the production of refrigerator oils.
The main properties of the refrigerating machine oil, such as rheological property, viscosity-temperature property, low-temperature fluidity, flash point, and intersolubility with refrigerant, are determined by the properties of the base oil. Therefore, the selection of the refrigerating machine oil is mainly focused on the selection of the base oil. Therefore, the quality of the base oil is directly related to the quality level of the finished compressor oil. The preparation of the refrigerating machine oil by adopting a furfural refining-clay refining process by taking naphthenic base distillate oil as a raw material is proposed, but the naphthenic base distillate oil has high acid value in the second line and the first line, the special oil produced by adopting the furfural refining-clay refining process has poor effect, and the problems of equipment corrosion, coking and the like exist in the furfural refining process. The indexes of the product such as chromaticity, oxidation stability and the like are difficult to reach the quality standard, and can not meet the increasingly improved environmental protection requirement.
Disclosure of Invention
In view of the above, the invention provides a system and a method for preparing special cold liquid oil from naphthenic base distillate oil, wherein the special cold liquid oil is prepared by adopting a full-hydrogen high-pressure hydrogenation technology comprising three combined process procedures of hydrotreating, medium-pressure hydrodewaxing and non-noble metal supplement refining, and product fractionation.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides a system for special oil of cold liquid is prepared to naphthenic base distillate, includes the raw oil buffer tank, according to the material flow direction, the raw oil buffer tank is connected with filter, hydrogenation blender, reaction feed heating furnace, hydrotreating reactor, hydrogen pour point depression reactor, hydrogenation in proper order and supplyes refined reactor, air cooler, high pressure separator, low pressure separator, fractionating tower, the fractionating tower is equipped with top of the tower export, goes up side outlet, export at the bottom of the side of the tower, top of the tower export is connected with the naphtha holding vessel, goes up side outlet and is connected with the special oil holding vessel of 1# cold liquid, and the export at the bottom of the tower is connected with the special oil holding vessel of 2# cold liquid, and the export at the bottom of the tower is connected with the special oil holding vessel of 3# cold liquid.
Further, the system also comprises a raw oil/bottom oil reducing heat exchanger, a mixed hydrogen oil/refined oil heat exchanger, a mixed hydrogen oil/hydrodewaxing oil heat exchanger, a hydrogenated oil/low-temperature oil heat exchanger and a refined oil/low-temperature oil heat exchanger;
a cold material inlet and a cold material outlet of the raw oil/reduced bottom oil heat exchanger are respectively connected with the raw oil buffer tank and the filter, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the fractionating tower and a 3# cold liquid special oil storage tank;
the cold material inlet and outlet of the hydrogen-mixed oil/refined oil heat exchanger are respectively connected with the hydrogenation mixer and the hydrogen-mixed oil/hydrodewaxing oil heat exchanger, and the hot material inlet and outlet are respectively connected with the refined oil/low-temperature oil heat exchanger and the air cooler inlet;
the cold material inlet and outlet of the mixed hydrogen oil/hydrodewaxing oil heat exchanger are respectively connected with the mixed hydrogen oil/refined oil heat exchanger and the reaction feeding heating furnace, and the hot material inlet and outlet are respectively connected with the tower bottom outlet of the hydrodewaxing reactor and the tower top inlet of the hydrofinishing reactor;
a cold material inlet and a cold material outlet of the hydrogenated oil/low oil separation heat exchanger are respectively connected with a refined oil/low oil separation heat exchanger and an inlet of a fractionating tower, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the hydrotreating reactor and a tower top inlet of the hydrodewaxing reactor;
and a cold material inlet and a cold material outlet of the refined oil/low-oil-separation heat exchanger are respectively connected with the low-pressure separator and the hydrogenated oil/low-oil-separation heat exchanger, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the hydrogenation complementary refining reactor and the hydrogen-mixed oil/refined oil heat exchanger.
Further, the system comprises a hydrogenation system, wherein the hydrogenation system comprises a recycle hydrogen compressor, a fresh hydrogen compressor and a recycle hydrogen/fresh hydrogen mixer;
the inlet of the recycle hydrogen compressor is connected with the gas phase outlet of the high-pressure separator; the outlet is respectively connected with a recycle hydrogen/fresh hydrogen mixer, a hydrotreating reactor, a hydrodewaxing reactor and a hydrofinishing reactor;
the outlet of the fresh hydrogen compressor is connected with the inlet of a recycle hydrogen/fresh hydrogen mixer, and the outlet of the recycle hydrogen/fresh hydrogen mixer is connected with the hydrotreating reactor.
And the outlet of the new hydrogen compressor is also connected with the inlet of the water cooler, and the outlet of the water cooler is connected with the inlet of the new hydrogen compressor and used as an overflow return line.
Furthermore, the hydrotreating reactor is provided with 3 catalyst beds and two cold hydrogen sections.
A method for preparing special cold liquid oil by using the system for preparing the special cold liquid oil by using the naphthenic-base distillate oil comprises the following steps:
1) The naphthenic base normal second line distillate oil and the reduced first line distillate oil enter a raw oil buffer tank, are pumped out by a raw material booster pump, enter a raw oil/reduced bottom oil heat exchanger, firstly exchange heat with reduced bottom oil, and then enter an automatic filter to remove mechanical impurities larger than 20 mu in the oil;
2) Pumping the filtered raw oil to a hydrogenation mixer by a reaction feed pump, mixing the raw oil with hydrogen, allowing the mixed raw oil to enter a mixed hydrogen oil/refined oil heat exchanger to exchange heat with a hydrogenation complementary refining reaction product from a refined oil/low-pressure oil heat exchanger, allowing the mixed raw oil to enter the mixed hydrogen oil/hydrodewaxing oil heat exchanger to exchange heat with the hydrodewaxing reaction product, allowing the mixed hydrogen oil/hydrodewaxing oil heat exchanger to enter a reaction feed heating furnace, heating to 331-383 ℃, and allowing the mixed hydrogen oil/hydrodewaxing oil heat exchanger to enter a hydrotreating reactor;
3) Under the action of a catalyst and under the hydrogen partial pressure of 15MPa and the temperature of 360-410 ℃, a hydrotreating reactor carries out desulfurization, denitrification and aromatic saturated cracking reactions to remove impurities in raw oil, and a hydrotreating reaction product enters a hydrogenated oil/low-temperature-fraction oil heat exchanger, exchanges heat with low-temperature-fraction oil from a refined oil/low-temperature-fraction oil heat exchanger to 352-402 ℃, and then enters a hydrodewaxing reactor;
4) The hydrodewaxing reaction product enters a hydro-oil/hydrodewaxing oil heat exchanger to exchange heat with the hydro-oil, the temperature is reduced to 253-333 ℃, and the hydro-refining product enters a hydrofinishing reactor;
5) The hydrogenation complementary refining reactor reacts under the action of a refining catalyst to remove residual olefin and other impurities, and the aromatic hydrocarbon is saturated; the reaction product of the hydrogenation refining reactor exchanges heat with low-fraction oil through a refined oil/low-fraction oil heat exchanger, enters a hydrogen-mixed oil/refined oil heat exchanger to exchange heat with hydrogen-mixed oil, is mixed with desalted water, and enters an air cooler;
6) The air cooler reduces the temperature of the reaction product of the hydrofinishing to 40 ℃, and the reaction product is sent to a high-pressure separator for three-phase separation of gas, oil and water, and the water phase is sulfur-containing sewage and is sent to an acidic water stripping device for treatment; the oil phase enters a low-pressure separator; the gas phase is circulating hydrogen and enters a hydrogenation system;
7) And the oil phase of the low-pressure separator enters an atmospheric tower to be subjected to atmospheric distillation, naphtha is cut out from the tower top, special oil for 1# cold liquid is discharged from the upper side line, special oil for 1# cold liquid is discharged from the lower side line, and special oil for 3# cold liquid is discharged from the tower bottom, and is respectively sent to a naphtha storage tank, a special oil storage tank for 1# cold liquid, a special oil storage tank for 2# cold liquid and a special oil storage tank for 3# cold liquid after passing through a reducing furnace and a reducing tower.
Further, gas-phase recycle hydrogen of the high-pressure separator enters a recycle hydrogen compressor, the recycle hydrogen at the outlet of the recycle hydrogen compressor is divided into four paths, and the first path is mixed with hydrogen from a new hydrogen compressor and then enters a hydrogenation mixer to be mixed with the raw oil; the second path is sent to a hydrotreating reactor to be used as quenching hydrogen; the third path is sent to the inlet of the hydrodewaxing reactor as the quenching hydrogen; the fourth way is to add the refined reactor of hydrogenation as the quench hydrogen; the hydrogen at the outlet of the new hydrogen compressor is divided into two paths, one path is mixed with the circulating hydrogen, and the other path returns to the inlet pipeline of the new hydrogen compressor through the water cooler to be used as an overflow return line of the new hydrogen compressor.
Further, the mass ratio of the normal second-line distillate to the reduced first-line distillate is 2.5.
Further, the pressure of the fractionating tower is controlled to be 0.1MPa, the temperature of the top of the tower is controlled to be 110-120 ℃, the temperature of the bottom of the tower is controlled to be 330-340 ℃, the 1# cold liquid special oil is distillate oil with the distillation range of 275-290 ℃, the 2# cold liquid special oil is distillate oil with the distillation range of 290-320 ℃, and the 3# cold liquid special oil is distillate oil with the distillation range of more than 320 ℃.
According to the technical scheme, compared with the prior art, the invention has the beneficial effects that:
the molecular structure of the naphthenic base distillate oil is obviously improved by carrying out the processes of hydrotreating, hydrodewaxing and complementary refining on the naphthenic base distillate oil and processing, the oxidation resistance and the low-temperature kinematic viscosity of the oil are improved, and the service life of the oil is prolonged. The special oil for cold liquid has unique oxidation resistance, excellent wear resistance, extremely high purity and stability, and is suitable for the working conditions of precision instruments in various high-pressure and various complex electromagnetic environments.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic view of a system for producing cold liquid-specific oil from naphthenic distillate oil according to the present invention;
in fig. 1:
the heat exchanger is characterized in that the heat exchanger 1 is a raw oil/bottom oil reducing heat exchanger, the heat exchanger 2 is a mixed hydrogen oil/refined oil heat exchanger, the heat exchanger 3 is a mixed hydrogen oil/condensate falling oil heat exchanger, the heat exchanger 4 is a hydrogenated oil/low-temperature oil heat exchanger, and the heat exchanger 5 is a refined oil/low-temperature oil heat exchanger.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
As shown in fig. 1, the present invention provides a system for preparing a special cold liquid oil from naphthenic base distillate oil, which comprises a raw oil buffer tank, wherein the raw oil buffer tank is sequentially connected with a filter, a hydrogenation mixer, a reaction feed heating furnace, a hydrotreating reactor, a hydrodewaxing reactor, a hydrogenation complementary refining reactor, an air cooler, a high pressure separator, a low pressure separator and a fractionating tower according to a material flow direction, the fractionating tower is provided with a tower top outlet, an upper side outlet, a lower side outlet and a tower bottom outlet, the tower top outlet is connected with a naphtha storage tank, the upper side outlet is connected with a special cold liquid oil storage tank # 1, the lower side outlet is connected with a special cold liquid oil storage tank # 2, and the tower bottom outlet is connected with a special cold liquid oil storage tank # 3.
In order to perfect the technical scheme, the system also comprises a raw oil/bottom oil reducing heat exchanger, a mixed hydrogen oil/refined oil heat exchanger, a mixed hydrogen oil/hydrodewaxing oil heat exchanger, a hydrogenated oil/low-temperature oil heat exchanger and a refined oil/low-temperature oil heat exchanger;
a cold material inlet and a cold material outlet of the raw oil/bottom-reduced oil heat exchanger are respectively connected with a raw oil buffer tank and a filter, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of a fractionating tower and a 3# cold liquid special oil storage tank;
the cold material inlet and outlet of the hydrogen-mixed oil/refined oil heat exchanger are respectively connected with the hydrogenation mixer and the hydrogen-mixed oil/hydrodewaxing oil heat exchanger, and the hot material inlet and outlet are respectively connected with the refined oil/low-temperature oil heat exchanger and the air cooler inlet;
the cold material inlet and outlet of the mixed hydrogen oil/hydrodewaxing oil heat exchanger are respectively connected with the mixed hydrogen oil/refined oil heat exchanger and the reaction feeding heating furnace, and the hot material inlet and outlet are respectively connected with the tower bottom outlet of the hydrodewaxing reactor and the tower top inlet of the hydrofinishing reactor;
a cold material inlet and a cold material outlet of the hydrogenated oil/low oil separation heat exchanger are respectively connected with the refined oil/low oil separation heat exchanger and an inlet of a fractionating tower, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the hydrotreating reactor and a tower top inlet of the hydrodewaxing reactor;
the cold material inlet and outlet of the refined oil/low-temperature oil separation heat exchanger are respectively connected with the low-pressure separator and the hydrogenated oil/low-temperature oil separation heat exchanger, and the hot material inlet and outlet are respectively connected with the bottom outlet of the hydrogenation complementary refining reactor and the hydrogen-mixed oil/refined oil heat exchanger.
In order to perfect the technical scheme, the system also comprises a hydrogenation system, wherein the hydrogenation system comprises a recycle hydrogen compressor, a new hydrogen compressor and a recycle hydrogen/new hydrogen mixer;
the inlet of the recycle hydrogen compressor is connected with the gas phase outlet of the high-pressure separator; the outlet is respectively connected with a circulating hydrogen/fresh hydrogen mixer, a hydrotreating reactor, a hydrodewaxing reactor and a hydrofinishing reactor;
the outlet of the fresh hydrogen compressor is connected with the inlet of the recycle hydrogen/fresh hydrogen mixer, and the outlet of the recycle hydrogen/fresh hydrogen mixer is connected with the hydrotreating reactor.
In order to perfect the technical scheme, the hydrogen recovery system further comprises a water cooler, wherein the outlet of the new hydrogen compressor is also connected with the inlet of the water cooler, and the outlet of the water cooler is connected with the inlet of the new hydrogen compressor and used as an overflow return line.
The hydrotreating reactor is provided with 3 catalyst beds and two cold hydrogen sections.
A method for preparing special oil for cold liquid from naphthenic base distillate oil comprises the following steps:
1) The naphthenic base distillate oil normal second line and the naphthenic base distillate oil first line are used as raw materials, the naphthenic base distillate oil normal second line and the naphthenic base distillate oil first line enter a raw oil buffer tank, are pumped out by a raw material booster pump and enter a raw oil/bottom oil reducing heat exchanger to exchange heat with bottom oil, and then the naphthenic base distillate oil/bottom oil reducing heat exchanger is subjected to automatic filtration to remove mechanical impurities larger than 20 mu in the oil;
2) Pumping the filtered raw oil to a hydrogenation mixer by a reaction feed pump, mixing the raw oil with hydrogen, exchanging heat between the mixed raw oil and a hydrogenation complementary refining reaction product from a refined oil/low-oil heat exchanger after mixing, then exchanging heat between the mixed raw oil and the hydrogenation complementary refining reaction product in a mixed-hydrogen oil/hydrodewaxing oil heat exchanger and the hydrodewaxing reaction product, then heating the mixed raw oil to 331-383 ℃ in a reaction feed heating furnace, and then feeding the heated raw oil into a hydrotreating reactor;
3) Under the action of a catalyst and under the hydrogen partial pressure of 15MPa and the temperature of 360-410 ℃, a hydrotreating reactor carries out desulfurization, denitrification and aromatic saturated cracking reactions to remove impurities in raw oil, and a hydrotreating reaction product enters a hydrogenated oil/low-temperature-fraction oil heat exchanger, exchanges heat with low-temperature-fraction oil from a refined oil/low-temperature-fraction oil heat exchanger to 352-402 ℃, and then enters a hydrodewaxing reactor;
4) The hydrodewaxing reaction product enters a mixed hydrogen oil/hydrodewaxing oil heat exchanger to exchange heat with mixed hydrogen oil, the temperature is reduced to 253-333 ℃, and the product enters a hydrofinishing reactor;
5) The hydrogenation complementary refining reactor reacts under the action of a refining catalyst to remove residual olefin and other impurities and saturate aromatic hydrocarbon; the reaction product of the hydrogenation-supplementing refining reactor is subjected to heat exchange with low-temperature oil through a refined oil/low-temperature oil heat exchanger at the temperature of 185-195 ℃, then enters a hydrogen-mixed oil/refined oil heat exchanger to exchange heat with hydrogen-mixed oil, is controlled at the temperature of 130-140 ℃, and is mixed with desalted water to enter an air cooler;
6) The air cooler reduces the temperature of the reaction product of the hydrofinishing to 40 ℃, and the reaction product is sent to a high-pressure separator for three-phase separation of gas, oil and water, and the water phase is sulfur-containing sewage and is sent to an acidic water stripping device for treatment; the oil phase enters a low-pressure separator; the gas phase is circulating hydrogen and enters a hydrogenation system;
7) And the oil phase of the low-pressure separator enters an atmospheric tower to be subjected to atmospheric distillation, the pressure of the fractionating tower is controlled to be 0.1MPa, the temperature of the top of the tower is 110-120 ℃, the temperature of the bottom of the tower is 330-340 ℃, naphtha is cut out from the top of the tower, special oil for 1# cold liquid is discharged from the upper lateral line, special oil for 1# cold liquid is discharged from the lower lateral line, and special oil for 3# cold liquid is discharged from the bottom of the tower, and the special oil for 3# cold liquid is respectively sent to a naphtha storage tank, a special oil storage tank for 1# cold liquid, a special oil storage tank for 2# cold liquid and a special oil storage tank for 3# cold liquid after passing through a reduction furnace and a reduction tower. The special oil for the No. 1 cold liquid is distillate oil with the distillation range between 275 and 290 ℃, the special oil for the No. 2 cold liquid is distillate oil with the distillation range between 290 and 320 ℃, and the special oil for the No. 3 cold liquid is distillate oil with the distillation range more than 320 ℃.
The gas-phase recycle hydrogen of the high-pressure separator enters a recycle hydrogen compressor, the recycle hydrogen at the outlet of the recycle hydrogen compressor is divided into four paths, and the first path is mixed with hydrogen from a new hydrogen compressor and then enters a hydrogenation mixer to be mixed with raw oil; the second path is sent to a hydrotreating reactor to be used as quenching hydrogen; the third path is sent to the inlet of the hydrodewaxing reactor to be used as quenching hydrogen; the fourth path is used as quenching hydrogen for a hydrogenation and supplement refining reactor; the hydrogen at the outlet of the new hydrogen compressor is divided into two paths, one path is mixed with the circulating hydrogen, and the other path returns to an inlet pipeline of the new hydrogen compressor through a water cooler to be used as an overflow return line of the new hydrogen compressor.
The mass ratio of normal second-line distillate to reduced first-line distillate is 2.5. The special oil for 1# cold liquid is discharged from the upper side line, the pressure is 0.1MPa, the extraction temperature is 280 ℃, the special oil for 2# cold liquid is discharged from the lower side line, the extraction temperature is 310 ℃, and the indexes of the special oil for 1# to 3# cold liquid are shown in table 2.
Table 1: feedstock Properties and feed Limit
Table 2: special oil index for 1# -3# cold liquid
From table 2, the product has better low-temperature kinematic viscosity, extremely high purity and stability, and is suitable for the working conditions of precision instruments under various high-voltage and various complex electromagnetic environments.
In the present specification, the embodiments are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. The utility model provides a system for cold liquid special oil is prepared to naphthenic base distillate oil, its characterized in that, includes the raw oil buffer tank, according to material flow direction, the raw oil buffer tank is connected with filter, hydrogenation mixer, reaction feed heating furnace, hydrotreating reactor, hydrogen pour point depression reactor, hydrogenation replenishment refining reactor, air cooler, high pressure separator, low pressure separator, fractionating tower in proper order, the fractionating tower is equipped with top of the tower export, goes up side outlet, export at the bottom of the tower, top of the tower export is connected with the naphtha holding vessel, goes up side outlet and is connected with 1# cold liquid special oil holding vessel, and the export is connected with 2# cold liquid special oil holding vessel at the bottom of the tower.
2. The system for preparing cold liquid special oil from naphthenic base distillate oil according to claim 1, which is characterized by further comprising a raw oil/bottom oil reducing heat exchanger, a hydrogen mixed oil/refined oil heat exchanger, a hydrogen mixed oil/hydrodewaxing oil heat exchanger, a hydrogenated oil/low oil heat exchanger and a refined oil/low oil heat exchanger;
a cold material inlet and a cold material outlet of the raw oil/bottom-reduced oil heat exchanger are respectively connected with the raw oil buffer tank and the filter, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the fractionating tower and a special 3# cold liquid oil storage tank;
the cold material inlet and outlet of the mixed hydrogen oil/refined oil heat exchanger are respectively connected with the hydrogenation mixer and the mixed hydrogen oil/hydrodewaxing oil heat exchanger, and the hot material inlet and outlet are respectively connected with the refined oil/low-temperature oil heat exchanger and the air cooler inlet;
the cold material inlet and outlet of the mixed hydrogen oil/hydrodewaxing oil heat exchanger are respectively connected with the mixed hydrogen oil/refined oil heat exchanger and the reaction feeding heating furnace, and the hot material inlet and outlet are respectively connected with the tower bottom outlet of the hydrodewaxing reactor and the tower top inlet of the hydrogenation refining reactor;
the cold material inlet and outlet of the hydrogenated oil/low oil separation heat exchanger are respectively connected with the refined oil/low oil separation heat exchanger and the inlet of the fractionating tower, and the hot material inlet and outlet are respectively connected with the outlet at the bottom of the hydrotreating reactor and the inlet at the top of the hydrodewaxing reactor;
and a cold material inlet and a cold material outlet of the refined oil/low-oil-separation heat exchanger are respectively connected with the low-pressure separator and the hydrogenated oil/low-oil-separation heat exchanger, and a hot material inlet and a hot material outlet are respectively connected with a tower bottom outlet of the hydrogenation complementary refining reactor and the hydrogen-mixed oil/refined oil heat exchanger.
3. The system for preparing cold liquid special oil from naphthenic base distillate oil according to claim 1, further comprising a hydrogenation system, wherein the hydrogenation system comprises a recycle hydrogen compressor, a fresh hydrogen compressor and a recycle hydrogen/fresh hydrogen mixer;
the inlet of the recycle hydrogen compressor is connected with the gas phase outlet of the high-pressure separator; the outlet is respectively connected with a circulating hydrogen/fresh hydrogen mixer, a hydrotreating reactor, a hydrodewaxing reactor and a hydrofinishing reactor;
the outlet of the fresh hydrogen compressor is connected with the inlet of a recycle hydrogen/fresh hydrogen mixer, and the outlet of the recycle hydrogen/fresh hydrogen mixer is connected with the hydrotreating reactor.
4. The system for preparing cold liquid special oil from naphthenic base distillate oil as claimed in claim 3, further comprising a water cooler, wherein the outlet of the fresh hydrogen compressor is further connected with the inlet of the water cooler, and the outlet of the water cooler is connected with the inlet of the fresh hydrogen compressor and is used as a return overflow line.
5. The system for preparing cold liquid special oil from naphthenic base distillate oil according to claim 3, wherein the hydrotreating reactor is provided with 3 catalyst beds and two cold hydrogen sections.
6. The method for preparing the special cold liquid oil by using the system for preparing the special cold liquid oil by using the naphthenic base distillate oil of any one of claims 1 to 5 is characterized by comprising the following steps of:
1) The naphthenic normal second-line distillate oil and the reduced first-line distillate oil enter a raw oil buffer tank, are pumped out by a raw material booster pump, enter a raw oil/reduced bottom oil heat exchanger, firstly exchange heat with reduced bottom oil, and then enter an automatic filter to remove mechanical impurities larger than 20 mu in the oil;
2) Pumping the filtered raw oil to a hydrogenation mixer by a reaction feed pump, mixing the raw oil with hydrogen, exchanging heat between the mixed raw oil and a hydrogenation complementary refining reaction product from a refined oil/low-oil heat exchanger after mixing, then exchanging heat between the mixed raw oil and the hydrogenation complementary refining reaction product in a mixed-hydrogen oil/hydrodewaxing oil heat exchanger and the hydrodewaxing reaction product, then heating the mixed raw oil to 331-383 ℃ in a reaction feed heating furnace, and then feeding the heated raw oil into a hydrotreating reactor;
3) Under the action of a catalyst and under the hydrogen partial pressure of 15MPa and the temperature of 360-410 ℃, a hydrotreating reactor carries out desulfurization, denitrification and aromatic saturated cracking reactions to remove impurities in raw oil, and a hydrotreating reaction product enters a hydrogenated oil/low-temperature-fraction oil heat exchanger, exchanges heat with low-temperature-fraction oil from a refined oil/low-temperature-fraction oil heat exchanger to 352-402 ℃, and then enters a hydrodewaxing reactor;
4) The hydrodewaxing reaction product enters a hydro-oil/hydrodewaxing oil heat exchanger to exchange heat with the hydro-oil, the temperature is reduced to 253-333 ℃, and the hydro-refining product enters a hydrofinishing reactor;
5) The hydrogenation complementary refining reactor reacts under the action of a refining catalyst to remove residual olefin and other impurities, and the aromatic hydrocarbon is saturated; the reaction product of the hydrogenation-supplementing refining reactor exchanges heat with low-temperature oil through a refined oil/low-temperature oil heat exchanger, then enters a hydrogen-mixed oil/refined oil heat exchanger to exchange heat with hydrogen-mixed oil, and then is mixed with desalted water to enter an air cooler;
6) The air cooler reduces the temperature of the reaction product of the hydrofinishing to 40 ℃, and the reaction product is sent to a high-pressure separator for three-phase separation of gas, oil and water, and the water phase is sulfur-containing sewage and is sent to an acidic water stripping device for treatment; the oil phase enters a low-pressure separator; the gas phase is circulating hydrogen and enters a hydrogenation system;
7) And the oil phase of the low-pressure separator enters an atmospheric tower to be subjected to atmospheric distillation, naphtha is cut out from the tower top, special oil for 1# cold liquid is discharged from the upper side line, special oil for 1# cold liquid is discharged from the lower side line, and special oil for 3# cold liquid is discharged from the tower bottom, and is respectively sent to a naphtha storage tank, a special oil storage tank for 1# cold liquid, a special oil storage tank for 2# cold liquid and a special oil storage tank for 3# cold liquid after passing through a reducing furnace and a reducing tower.
7. The method for preparing cold liquid special oil by naphthenic base distillate oil according to claim 6, characterized in that gas phase recycle hydrogen of a high-pressure separator enters a recycle hydrogen compressor, the recycle hydrogen at the outlet of the recycle hydrogen compressor is divided into four paths, the first path is mixed with hydrogen from a new hydrogen compressor and then enters a hydrogenation mixer to be mixed with raw oil; the second path is sent to a hydrotreating reactor to be used as quenching hydrogen; the third path is sent to the inlet of the hydrodewaxing reactor to be used as quenching hydrogen; the fourth way is to add the refined reactor of hydrogenation as the quench hydrogen; the hydrogen at the outlet of the new hydrogen compressor is divided into two paths, one path is mixed with the circulating hydrogen, and the other path returns to an inlet pipeline of the new hydrogen compressor through a water cooler to be used as an overflow return line of the new hydrogen compressor.
8. The method for preparing cold liquid special oil by naphthenic base distillate oil as claimed in claim 6, wherein the mass ratio of the normal second-line distillate oil to the reduced first-line distillate oil is 2.5.
9. The method for preparing cold liquid special oil from naphthenic base distillate oil as claimed in claim 6, wherein the pressure of the fractionating tower is controlled to be 0.1MPa, the temperature of the tower top is 110-120 ℃, the temperature of the tower bottom is 330-340 ℃, the 1# cold liquid special oil is distillate oil with the distillation range of 275-290 ℃, the 2# cold liquid special oil is distillate oil with the distillation range of 290-320 ℃, and the 3# cold liquid special oil is distillate oil with the distillation range of more than 320 ℃.
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Citations (5)
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| CN102311785A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Method for hydrogenating naphthenic base distillate to produce lubricating oil basic oil |
| CN110540871A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Processing method of naphthenic oil |
| CN113583711A (en) * | 2021-08-06 | 2021-11-02 | 山东京博石油化工有限公司 | Preparation method of base oil containing aromatic hydrocarbon refrigerator oil |
| CN113663617A (en) * | 2021-08-13 | 2021-11-19 | 中海沥青股份有限公司 | Low-viscosity refrigerator oil base oil and preparation method and application thereof |
| CN218710201U (en) * | 2022-09-29 | 2023-03-24 | 盘锦北方沥青股份有限公司 | System for preparing special oil for cold liquid from naphthenic base distillate oil |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311785A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Method for hydrogenating naphthenic base distillate to produce lubricating oil basic oil |
| CN110540871A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Processing method of naphthenic oil |
| CN113583711A (en) * | 2021-08-06 | 2021-11-02 | 山东京博石油化工有限公司 | Preparation method of base oil containing aromatic hydrocarbon refrigerator oil |
| CN113663617A (en) * | 2021-08-13 | 2021-11-19 | 中海沥青股份有限公司 | Low-viscosity refrigerator oil base oil and preparation method and application thereof |
| CN218710201U (en) * | 2022-09-29 | 2023-03-24 | 盘锦北方沥青股份有限公司 | System for preparing special oil for cold liquid from naphthenic base distillate oil |
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