CN108998092B - Process for producing lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate - Google Patents
Process for producing lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- 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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M177/00—Special methods of preparation of lubricating compositions; Chemical modification by after-treatment of components or of the whole of a lubricating composition, not covered by other classes
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- C—CHEMISTRY; METALLURGY
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
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Abstract
The invention relates to the technical field of lubricating oil base oil, in particular to a process for producing lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate oil. The heavy-traffic asphalt distillate oil is used as a main raw material, and the circulating oil is used as an auxiliary raw material, so that the hydrogenation treatment is carried out together, the recovery effect of the heavy-traffic asphalt distillate oil is improved, and particularly, cold low-molecular oil and hot low-molecular oil in the process enter a main stripping tower for stripping, so that the cleanliness of the oil product is improved. In addition, two-stage hydrogenation reaction adopts different catalysts for synergistic reaction, so that the efficiency of hydrogenation catalysis is increased. Meanwhile, the acidic water treatment device is adopted, so that the discharge amount of acidic water is reduced. The invention has reasonable route design and ensures the overall reasonability, advancement and long-period safe and stable operation of the device design. The standard lubricating oil base oil can be obtained by adopting the method for producing the lubricating oil base oil.
Description
Technical Field
The invention relates to the technical field of lubricating oil base oil, in particular to a process for producing lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate oil.
Background
In recent years, due to the development of automobile engine technology, automobile engine oil is developed to high-quality multi-grade oil with low viscosity and low volatility, and the requirements on economy, volatility and shear stability are higher and higher, so that the demand of high-performance lubricating oil is also higher and higher. Although the construction investment in the early stage of the hydrotreatment of the lubricating oil is slightly higher than that of the traditional refining process, if the process advantages of the hydrotreatment and the factors that the supply of high-quality crude oil suitable for producing the lubricating oil is increasingly tense and the like are comprehensively considered, the development of the hydrotreatment process can be expected to have wider prospects.
The prior production process of the lubricating oil comprises solvent dewaxing, propane deasphalting, clay refining, hydrorefining and the like, and the lubricating oil base oil produced by the conventional three sets of methods dominates, but the demand is gradually reduced. High viscosity index lubricant base oils produced by hydroprocessing are increasing and becoming less desirable. The heavy traffic asphalt distillate oil is prepared by atmospheric distillation and reduced pressure distillation of crude oil, relatively cheap heavy traffic asphalt distillate oil is utilized, lubricating oil base oil with higher added value is produced by a hydrotreating process, low-sulfur automotive diesel blending components and partial naphtha which reach the national five standards are by-produced, and lower investment is strived to obtain greater benefit.
However, due to the complexity of the heavy cross-linked bitumen distillate oil component, the quality of the lubricant base oil obtained by the conventional hydrotreating process is poor and does not meet various indexes of the standard lubricant base oil. Therefore, there is a need to develop a process for hydrotreating heavy traffic bitumen distillate oil to produce a standard lube base oil.
Disclosure of Invention
The invention aims to provide a process for producing standard lubricating oil base oil by using heavy-traffic asphalt distillate oil as a main raw material.
The process for producing the lubricating oil base oil by hydrotreating heavy traffic asphalt distillate oil comprises the following steps:
(1) a hydrogenation reaction part:
firstly, sending heavy-traffic asphalt distillate oil outside the device into the device, exchanging heat with lubricating oil base oil, heating, then sending into a filter to remove particles larger than 25 microns, mixing with circulating oil from a fractionation part, and then sending into a raw oil buffer tank protected by inert gas to form raw oil;
exchanging heat between the raw oil in the raw oil buffer tank and the reaction effluent from the hydrotreating reactor, mixing the raw oil with mixed hydrogen, entering a hydrotreating reactor for hydrotreating reaction, and then entering the hydrotreating reactor for hydrotreating reaction, wherein quenching hydrogen injection facilities are arranged between bed layers of the reactor and between the reactors;
thirdly, after exchanging heat between the reaction effluent from the hydrotreating reactor and the raw oil in the raw oil buffer tank, the reaction effluent enters a thermal high-pressure separator for gas-liquid separation to form thermal high-pressure gas and thermal high-pressure oil;
the hot high-pressure gas exchanges heat with the cold low-pressure gas and the mixed hydrogen in sequence, then enters a cold high-pressure separator after being cooled by a hot high-pressure gas air cooler to be subjected to oil-gas-water separation, and the cold high-pressure gas coming out of the top, namely the circulating hydrogen enters a circulating hydrogen compressor through a circulating hydrogen cyclone dealkylator and a circulating hydrogen desulfurization tower and is divided into two paths: one path of the hydrogen is used as quench hydrogen to a hydrofining reactor and a hydrotreating reactor to control the inlet temperature of a reactor bed layer, and the other path of the hydrogen is mixed with fresh hydrogen from a fresh hydrogen compressor to form mixed hydrogen; cold high-pressure oil enters a cold low-pressure separator to become cold low-pressure gas and cold low-pressure oil, the cold low-pressure gas is discharged out of the system after being desulfurized in the device, and the cold low-pressure oil and hot high-pressure gas exchange heat and then enter a main stripping tower;
the hot high-pressure oil enters a hot low-pressure separator to become hot low-pressure gas and hot low-pressure oil, and the hot low-pressure gas is cooled by a hot low-pressure gas air cooler and then mixed with cold high-pressure oil to enter a cold low-pressure separator; directly feeding hot low-fraction oil into a main stripping tower;
acid water is discharged from the bottoms of the cold high-pressure separator and the cold low-pressure separator;
(2) fractional distillation part:
mixing cold low-fraction oil and hot low-fraction oil in a main stripping tower to form low-fraction oil, feeding stripping steam from the bottom of the main stripping tower, cooling top gas of the main stripping tower by a top air cooler of the main stripping tower, and feeding the cooled top gas into a reflux tank at the top of the main stripping tower for oil-gas-water separation, wherein one part of top oil phase of the main stripping tower is used as reflux of the main stripping tower, and the other part of top oil phase of the main stripping tower is used as feed of a debutanizer; the discharged sulfur-containing sewage is sent to the outside of the device for desulfurization;
secondly, exchanging heat between the liquid phase at the bottom of the main stripping tower and the reaction effluent from the hydrotreating reactor, heating the liquid phase by a heating furnace, then feeding the liquid phase into a fractionating tower, stripping the liquid phase at the bottom of the fractionating tower by using water vapor, cooling the gas at the top of the fractionating tower by an air cooler at the top of the fractionating tower, feeding the gas at the top of the fractionating tower into a reflux tank at the top of the fractionating tower, boosting a part of the liquid phase in the reflux tank by a heavy naphtha pump, cooling the gas by a heavy naphtha cooler, then feeding the gas out; the oily sewage is conveyed to the hydrogenation part through the top of the fractionating tower and is used as reaction water injection for recycling; tower bottom oil is taken as cycle oil and is delivered to a raw oil buffer tank of a hydrogenation reaction part;
the fractionating tower is provided with two side strippers: a aviation kerosene side stripper and a lubricating oil base oil side stripper;
the heat at the bottom of the aviation kerosene side steam stripping tower is provided by a debutanizer, and the product at the bottom of the aviation kerosene side steam stripping tower is discharged out of the device after being boosted by an aviation kerosene pump and cooled by the debutanizer and an aviation kerosene air cooler;
steam stripping is adopted at the bottom of the lubricating oil base oil side stripping tower; and after the pressure of the product at the bottom of the tower is increased by a lubricating oil base oil pump, the product is cooled and dehydrated by a debutanizer reboiler, a lubricating oil base oil air cooler and a lubricating oil base oil coalescer and then is discharged out of the device to prepare the lubricating oil base oil.
Wherein:
the hydrofining reactor selects catalysts FZC-102K and FF-20 with the mass ratio of 1: 1. The inlet temperature of the catalyst bed layer of the hydrofining reactor is 400-420 ℃, the outlet temperature is 425-440 ℃, the inlet hydrogen partial pressure of the hydrofining reactor is 13-16MPa, and the volume space velocity is 0.5-0.7h-1Reactor inlet gas-oil volume ratio 830- > 870: 1.
The hydrotreating reactor selects catalysts FC-14 and FF-20 with the mass ratio of 1: 1. The inlet temperature of the catalyst bed layer of the hydrotreating reactor is 425-435 ℃, the outlet temperature is 430-440 ℃, the inlet hydrogen partial pressure of the hydrotreating reactor is 13-16MPa, and the volume space velocity is 0.8-0.9h-1Reactor inlet gas-oil volume ratio 830- > 870: 1.
The acidic water stripping process is as follows:
firstly, acid water enters a raw material water degassing tank, and the separated light oil gas is sent to a low-pressure gas pipe network; the degassed acid water enters an oil remover for sedimentation and oil removal, and the separated light sump oil is intermittently and automatically flowed to a sump oil tank and is pressurized and conveyed to a factory sump oil tank area; the deoiled acidic water enters a raw material water tank to form raw material water, is pressurized by a raw material water feeding pump, exchanges heat with purified water at the bottom of a main stripping tower, and enters the upper part of the main stripping tower;
secondly, after the heat exchange between the purified water at the bottom of the main stripping tower and the raw material water, pressurizing the purified water by a purified water pressurizing pump, cooling the purified water by a purified water cooler, and sending the purified water to a raw material water degassing tank for recycling;
thirdly, the acidic gas on the top of the main stripping tower is condensed by an air cooler on the top of the tower and then enters a reflux tank on the top of the tower, and the non-condensed acidic gas is sent to a subsequent treatment device.
In the step I of the acid water stripping process, the pressure of a raw material water degassing tank is 0.2-0.25MPa, the pressure of a raw material water tank is normal pressure, the deoiled acid water enters the raw material water tank to form raw material water, and the raw material water is pressurized by a raw material water feed pump and exchanges heat with purified water at the bottom of a main stripping tower to 110 ℃.
The bottom temperature of the main stripping tower is 120-130 ℃, the bottom pressure of the main stripping tower is 0.14-0.15MPa, the top temperature of the main stripping tower is 105-115 ℃, and the top pressure of the main stripping tower is 0.10-0.11 MPa.
In the second step of the acid water stripping process, the acid water is cooled to 30-40 ℃ by a purified water cooler.
In the third step of the acid water stripping process, the acid gas on the top of the main stripping tower is condensed to 75-80 ℃ by an air cooler on the top of the tower.
The invention has the following beneficial effects:
the heavy-duty asphalt distillate oil is used as a main raw material, and the circulating oil is used as an auxiliary raw material, so that the hydrogenation treatment is carried out together, the recovery effect of the heavy-duty asphalt distillate oil is improved, and particularly, the cold low-fraction oil and the hot low-fraction oil enter the main stripping tower for stripping, so that the cleanliness of the oil product is improved. In addition, the two-stage hydrogenation adopts different catalysts for synergistic reaction, so that the efficiency of hydrogenation catalysis is increased. Meanwhile, the acidic water treatment device is adopted, so that the discharge amount of acidic water is reduced. The invention has reasonable route design and ensures the overall reasonability, advancement and long-period safe and stable operation of the device design. The invention effectively reduces the energy consumption of the device, reasonably recovers the waste heat of the device, reaches an advanced level, and reduces the equipment investment on the premise of ensuring reliable performance. The invention can obtain standard lubricating oil base oil.
Drawings
FIG. 1 is a partial process flow diagram of a hydrogenation reaction;
FIG. 2 is a process flow diagram of a fractionation section;
FIG. 3 is a flow diagram of an acidic water treatment process.
Detailed Description
The present invention is further described below with reference to examples.
Example 1
The process for producing the lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate oil comprises the following two parts:
(1) a hydrogenation reaction part:
firstly, sending heavy-traffic asphalt distillate oil outside the device into the device, exchanging heat with lubricating oil base oil, heating, then sending into a filter to remove particles larger than 25 microns, mixing with circulating oil from a fractionation part, and then sending into a raw oil buffer tank protected by inert gas to form raw oil;
exchanging heat between the raw oil in the raw oil buffer tank and the reaction effluent from the hydrotreating reactor, mixing the raw oil with mixed hydrogen, entering a hydrotreating reactor for hydrotreating reaction, and then entering the hydrotreating reactor for hydrotreating reaction, wherein quenching hydrogen injection facilities are arranged between bed layers of the reactor and between the reactors;
thirdly, after exchanging heat between the reaction effluent from the hydrotreating reactor and the raw oil in the raw oil buffer tank, the reaction effluent enters a thermal high-pressure separator for gas-liquid separation to form thermal high-pressure gas and thermal high-pressure oil;
the hot high-pressure gas exchanges heat with the cold low-pressure gas and the mixed hydrogen in sequence, then enters a cold high-pressure separator after being cooled by a hot high-pressure gas air cooler to be subjected to oil-gas-water separation, and the cold high-pressure gas coming out of the top, namely the circulating hydrogen enters a circulating hydrogen compressor through a circulating hydrogen cyclone dealkylator and a circulating hydrogen desulfurization tower and is divided into two paths: one path of the hydrogen is used as quench hydrogen to a hydrofining reactor and a hydrotreating reactor to control the inlet temperature of a reactor bed layer, and the other path of the hydrogen is mixed with fresh hydrogen from a fresh hydrogen compressor to form mixed hydrogen; cold high-pressure oil enters a cold low-pressure separator to become cold low-pressure gas and cold low-pressure oil, the cold low-pressure gas is discharged out of the system after being desulfurized in the device, and the cold low-pressure oil and hot high-pressure gas exchange heat and then enter a main stripping tower;
the hot high-pressure oil enters a hot low-pressure separator to become hot low-pressure gas and hot low-pressure oil, and the hot low-pressure gas is cooled by a hot low-pressure gas air cooler and then mixed with cold high-pressure oil to enter a cold low-pressure separator; directly feeding hot low-fraction oil into a main stripping tower;
acid water is discharged from the bottoms of the cold high-pressure separator and the cold low-pressure separator;
(2) fractional distillation part:
mixing cold low-fraction oil and hot low-fraction oil in a main stripping tower to form low-fraction oil, feeding stripping steam from the bottom of the main stripping tower, cooling top gas of the main stripping tower by a top air cooler of the main stripping tower, and feeding the cooled top gas into a reflux tank at the top of the main stripping tower for oil-gas-water separation, wherein one part of top oil phase of the main stripping tower is used as reflux of the main stripping tower, and the other part of top oil phase of the main stripping tower is used as feed of a debutanizer; the discharged sulfur-containing sewage is sent to the outside of the device for desulfurization;
secondly, exchanging heat between the liquid phase at the bottom of the main stripping tower and the reaction effluent from the hydrotreating reactor, heating the liquid phase by a heating furnace, then feeding the liquid phase into a fractionating tower, stripping the liquid phase at the bottom of the fractionating tower by using water vapor, cooling the gas at the top of the fractionating tower by an air cooler at the top of the fractionating tower, feeding the gas at the top of the fractionating tower into a reflux tank at the top of the fractionating tower, boosting a part of the liquid phase in the reflux tank by a heavy naphtha pump, cooling the gas by a heavy naphtha cooler, then feeding the gas out; the oily sewage is conveyed to the hydrogenation part through the top of the fractionating tower and is used as reaction water injection for recycling; tower bottom oil is taken as cycle oil and is delivered to a raw oil buffer tank of a hydrogenation reaction part;
the fractionating tower is provided with two side strippers: a aviation kerosene side stripper and a lubricating oil base oil side stripper;
the heat at the bottom of the aviation kerosene side steam stripping tower is provided by a debutanizer, and the product at the bottom of the aviation kerosene side steam stripping tower is discharged out of the device after being boosted by an aviation kerosene pump and cooled by the debutanizer and an aviation kerosene air cooler;
steam stripping is adopted at the bottom of the lubricating oil base oil side stripping tower; and after the pressure of the product at the bottom of the tower is increased by a lubricating oil base oil pump, the product is cooled and dehydrated by a debutanizer reboiler, a lubricating oil base oil air cooler and a lubricating oil base oil coalescer and then is discharged out of the device to prepare the lubricating oil base oil.
The acidic water stripping process is as follows:
firstly, acid water enters a raw material water degassing tank, and the separated light oil gas is sent to a low-pressure gas pipe network; the degassed acid water enters an oil remover for sedimentation and oil removal, and the separated light sump oil is intermittently and automatically flowed to a sump oil tank and is pressurized and conveyed to a factory sump oil tank area; the deoiled acidic water enters a raw material water tank to form raw material water, the raw material water is pressurized by a raw material water feed pump, and the raw material water and purified water at the bottom of a main stripping tower exchange heat to 110 ℃ and enter the upper part of the main stripping tower;
secondly, after the heat exchange between the purified water at the bottom of the main stripping tower and the raw material water, pressurizing the purified water by a purified water pressurizing pump, cooling the purified water to 40 ℃ by a purified water cooler, and sending the purified water to a raw material water degassing tank for recycling;
thirdly, condensing the acidic gas on the top of the main stripping tower to 75 ℃ through an air cooler on the top of the tower, then entering a reflux tank on the top of the tower, and sending the uncondensed acidic gas to a subsequent treatment device.
Example 1 the hydroprocessing unit operating conditions are shown in table 1 and the sour water stripping unit operating conditions are shown in table 2.
TABLE 1 hydrogenation unit operating conditions Table
Table 2 sour water stripping plant operating conditions table
| Serial number | Item | Unit of | Parameter(s) |
| 1 | Raw water degassing tank pressure | MPa | 0.21 |
| 2 | Pressure of raw material water tank | MPa | Atmospheric pressure |
| 3 | Temperature at bottom of main stripping tower | ℃ | 126 |
| 4 | Top temperature of main stripper | ℃ | 111 |
| 5 | Pressure at bottom of main stripping tower | MPa | 0.14 |
| 6 | Top pressure of main stripper | MPa | 0.11 |
Example 2
The acidic water stripping process is as follows:
firstly, acid water enters a raw material water degassing tank, and the separated light oil gas is sent to a low-pressure gas pipe network; the degassed acid water enters an oil remover for sedimentation and oil removal, and the separated light sump oil is intermittently and automatically flowed to a sump oil tank and is pressurized and conveyed to a factory sump oil tank area; the deoiled acidic water enters a raw material water tank to form raw material water, the raw material water is pressurized by a raw material water feed pump, and the raw material water and purified water at the bottom of a main stripping tower exchange heat to 100 ℃ and enter the upper part of the main stripping tower;
secondly, after the heat exchange between the purified water at the bottom of the main stripping tower and the raw material water, pressurizing the purified water by a purified water pressurizing pump, cooling the purified water to 35 ℃ by a purified water cooler, and sending the purified water to a raw material water degassing tank for recycling;
thirdly, condensing the acidic gas on the top of the main stripping tower to 78 ℃ through an air cooler on the top of the tower, then entering a reflux tank on the top of the tower, and sending the non-condensed acidic gas to a subsequent treatment device.
Example 2 the hydroprocessing unit operating conditions are shown in table 3 and the sour water stripping unit operating conditions are shown in table 4.
TABLE 3 operating conditions of hydrogenation reactor
Table 4 sour water stripping plant operating conditions table
| Serial number | Item | Unit of | Parameter(s) |
| 1 | Raw water degassing tank pressure | MPa | 0.23 |
| 2 | Pressure of raw material water tank | MPa | Atmospheric pressure |
| 3 | Temperature at bottom of main stripping tower | ℃ | 122 |
| 4 | Top temperature of main stripper | ℃ | 105 |
| 5 | Pressure at bottom of main stripping tower | MPa | 0.15 |
| 6 | Top pressure of main stripper | MPa | 0.10 |
Otherwise as in example 1.
Example 3
The acidic water stripping process is as follows:
firstly, acid water enters a raw material water degassing tank, and the separated light oil gas is sent to a low-pressure gas pipe network; the degassed acid water enters an oil remover for sedimentation and oil removal, and the separated light sump oil is intermittently and automatically flowed to a sump oil tank and is pressurized and conveyed to a factory sump oil tank area; the deoiled acidic water enters a raw material water tank to form raw material water, the raw material water is pressurized by a raw material water feed pump, and the raw material water and purified water at the bottom of a main stripping tower exchange heat to 105 ℃ and enter the upper part of the main stripping tower;
secondly, after the heat exchange between the purified water at the bottom of the main stripping tower and the raw material water, pressurizing the purified water by a purified water pressurizing pump, cooling the purified water to 30 ℃ by a purified water cooler, and sending the purified water to a raw material water degassing tank for recycling;
thirdly, condensing the acidic gas on the top of the main stripping tower to 80 ℃ through an air cooler on the top of the tower, then entering a reflux tank on the top of the tower, and sending the non-condensed acidic gas to a subsequent treatment device.
Example 3 the hydroprocessing unit operating conditions are shown in table 5 and the sour water stripping unit operating conditions are shown in table 6.
TABLE 5 operating conditions of hydrogenation reactor
Table 6 sour water stripping plant operating conditions table
| Serial number | Item | Unit of | Parameter(s) |
| 1 | Raw water degassing tank pressure | MPa | 0.25 |
| 2 | Pressure of raw material water tank | MPa | Atmospheric pressure |
| 3 | Temperature at bottom of main stripping tower | ℃ | 130 |
| 4 | Top temperature of main stripper | ℃ | 115 |
| 5 | Pressure at bottom of main stripping tower | MPa | 0.14 |
| 6 | Top pressure of main stripper | MPa | 0.10 |
Otherwise as in example 1.
Through detection, all indexes of the products obtained in the examples 1 to 3 meet the indexes of standard lubricating oil base oil.
Claims (10)
1. A process for producing lubricating oil base oil by hydrotreating heavy traffic asphalt distillate oil is characterized by comprising the following steps:
(1) a hydrogenation reaction part:
firstly, sending heavy-traffic asphalt distillate oil from a device into a hydrogenation reaction device, exchanging heat with lubricating oil base oil, heating, then sending into a filter to remove particles larger than 25 microns, mixing with circulating oil from a fractionation part, and then sending into a raw oil buffer tank protected by inert gas to form raw oil;
exchanging heat between the raw oil in the raw oil buffer tank and the reaction effluent from the hydrotreating reactor, mixing the raw oil with mixed hydrogen, entering a hydrotreating reactor for hydrotreating reaction, and then entering the hydrotreating reactor for hydrotreating reaction, wherein quenching hydrogen injection facilities are arranged between bed layers of the reactor and between the reactors;
thirdly, after exchanging heat between the reaction effluent from the hydrotreating reactor and the raw oil in the raw oil buffer tank, the reaction effluent enters a thermal high-pressure separator for gas-liquid separation to form thermal high-pressure gas and thermal high-pressure oil;
the hot high-pressure gas exchanges heat with the cold low-pressure gas and the mixed hydrogen in sequence, then enters a cold high-pressure separator after being cooled by a hot high-pressure gas air cooler to be subjected to oil-gas-water separation, and the cold high-pressure gas coming out of the top, namely the circulating hydrogen enters a circulating hydrogen compressor through a circulating hydrogen cyclone dealkylator and a circulating hydrogen desulfurization tower and is divided into two paths: one path of the hydrogen is used as quench hydrogen to a hydrofining reactor and a hydrotreating reactor to control the inlet temperature of a reactor bed layer, and the other path of the hydrogen is mixed with fresh hydrogen from a fresh hydrogen compressor to form mixed hydrogen; cold high-pressure oil enters a cold low-pressure separator to become cold low-pressure gas and cold low-pressure oil, the cold low-pressure gas is discharged out of the system after being desulfurized in the device, and the cold low-pressure oil and hot high-pressure gas exchange heat and then enter a main stripping tower;
the hot high-pressure oil enters a hot low-pressure separator to become hot low-pressure gas and hot low-pressure oil, and the hot low-pressure gas is cooled by a hot low-pressure gas air cooler and then mixed with cold high-pressure oil to enter a cold low-pressure separator; directly feeding hot low-fraction oil into a main stripping tower;
acid water is discharged from the bottoms of the cold high-pressure separator and the cold low-pressure separator;
(2) fractional distillation part:
mixing cold low-fraction oil and hot low-fraction oil in a main stripping tower to form low-fraction oil, feeding stripping steam from the bottom of the main stripping tower, cooling top gas of the main stripping tower by a top air cooler of the main stripping tower, and feeding the cooled top gas into a reflux tank at the top of the main stripping tower for oil-gas-water separation, wherein one part of top oil phase of the main stripping tower is used as reflux of the main stripping tower, and the other part of top oil phase of the main stripping tower is used as feed of a debutanizer; the discharged sulfur-containing sewage is sent to the outside of the device for desulfurization;
secondly, exchanging heat between the liquid phase at the bottom of the main stripping tower and the reaction effluent from the hydrotreating reactor, heating the liquid phase by a heating furnace, then feeding the liquid phase into a fractionating tower, stripping the liquid phase at the bottom of the fractionating tower by using water vapor, cooling the gas at the top of the fractionating tower by an air cooler at the top of the fractionating tower, feeding the gas at the top of the fractionating tower into a reflux tank at the top of the fractionating tower, boosting a part of the liquid phase in the reflux tank by a heavy naphtha pump, cooling the gas by a heavy naphtha cooler, then feeding the gas out; the oily sewage is conveyed to the hydrogenation part through the top of the fractionating tower and is used as reaction water injection for recycling; tower bottom oil is taken as cycle oil and is delivered to a raw oil buffer tank of a hydrogenation reaction part;
the fractionating tower is provided with two side strippers: a aviation kerosene side stripper and a lubricating oil base oil side stripper;
the heat at the bottom of the aviation kerosene side steam stripping tower is provided by a debutanizer, and the product at the bottom of the aviation kerosene side steam stripping tower is discharged out of the device after being boosted by an aviation kerosene pump and cooled by the debutanizer and an aviation kerosene air cooler;
steam stripping is adopted at the bottom of the lubricating oil base oil side stripping tower; and after the pressure of the product at the bottom of the tower is increased by a lubricating oil base oil pump, the product is cooled and dehydrated by a debutanizer reboiler, a lubricating oil base oil air cooler and a lubricating oil base oil coalescer and then is discharged out of the device to prepare the lubricating oil base oil.
2. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 1, wherein: the hydrofining reactor selects catalysts FZC-102K and FF-20 with the mass ratio of 1: 1.
3. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 1, wherein: the inlet temperature of the catalyst bed layer of the hydrofining reactor is 400-420 ℃, the outlet temperature is 425-440 ℃, the inlet hydrogen partial pressure of the hydrofining reactor is 13-16MPa, and the volume space velocity is 0.5-0.7h-1Reactor inlet gas-oil volume ratio 830- > 870: 1.
4. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 1, wherein: the hydrotreating reactor selects catalysts FC-14 and FF-20 with the mass ratio of 1: 1.
5. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 1, wherein: the inlet temperature of the catalyst bed layer of the hydrotreating reactor is 425-435 ℃, the outlet temperature is 430-440 ℃, the inlet hydrogen partial pressure of the hydrotreating reactor is 13-16MPa, and the volume space velocity is 0.8-0.9h-1Reactor inlet gas-oil volume ratio 830- > 870: 1.
6. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 1, wherein: the acidic water stripping process is as follows:
firstly, acid water enters a raw material water degassing tank, and the separated light oil gas is sent to a low-pressure gas pipe network; the degassed acid water enters an oil remover for sedimentation and oil removal, and the separated light sump oil is intermittently and automatically flowed to a sump oil tank and is pressurized and conveyed to a factory sump oil tank area; the deoiled acidic water enters a raw material water tank to form raw material water, is pressurized by a raw material water feeding pump, exchanges heat with purified water at the bottom of a main stripping tower, and enters the upper part of the main stripping tower;
secondly, after the heat exchange between the purified water at the bottom of the main stripping tower and the raw material water, pressurizing the purified water by a purified water pressurizing pump, cooling the purified water by a purified water cooler, and sending the purified water to a raw material water degassing tank for recycling;
thirdly, the acidic gas on the top of the main stripping tower is condensed by an air cooler on the top of the tower and then enters a reflux tank on the top of the tower, and the non-condensed acidic gas is sent to a subsequent treatment device.
7. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 6, wherein: in the step I of the acid water stripping process, the pressure of a raw material water degassing tank is 0.2-0.25MPa, the pressure of a raw material water tank is normal pressure, the deoiled acid water enters the raw material water tank to form raw material water, and the raw material water is pressurized by a raw material water feed pump and exchanges heat with purified water at the bottom of a main stripping tower to 110 ℃.
8. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 6, wherein: the bottom temperature of the main stripping tower is 120-130 ℃, the bottom pressure of the main stripping tower is 0.14-0.15MPa, the top temperature of the main stripping tower is 105-115 ℃, and the top pressure of the main stripping tower is 0.10-0.11 MPa.
9. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 6, wherein: in the second step of the acid water stripping process, the acid water is cooled to 30-40 ℃ by a purified water cooler.
10. The process of hydrotreating heavy cross-asphalted distillate oil to produce lube base oil of claim 6, wherein: in the third step of the acid water stripping process, the acid gas on the top of the main stripping tower is condensed to 75-80 ℃ by an air cooler on the top of the tower.
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Denomination of invention: Process for producing lube base oil by hydrotreating heavy asphalt distillate Effective date of registration: 20211029 Granted publication date: 20200825 Pledgee: Qishang bank Zhangdian sub branch Pledgor: SHANDONG QICHUANG PETROCHEMICAL ENGINEERING Co.,Ltd. Registration number: Y2021980011575 |
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