CN100519700C - Diesel oil hydrogenation refining fractionation method and device thereof - Google Patents
Diesel oil hydrogenation refining fractionation method and device thereof Download PDFInfo
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- CN100519700C CN100519700C CNB2007100275610A CN200710027561A CN100519700C CN 100519700 C CN100519700 C CN 100519700C CN B2007100275610 A CNB2007100275610 A CN B2007100275610A CN 200710027561 A CN200710027561 A CN 200710027561A CN 100519700 C CN100519700 C CN 100519700C
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Abstract
The invention provides a hydrogenation refining fractionation method for diesel oil, which includes a stripping fractional distillation process for reaction generation oil steam and a dewatering process for refined diesel oil. Concrete technical project of the method is: hydrogenation refining reaction generation oil from low pressure separator enters feed inlet of fractionating tower with certain temperature; the fractionating tower employs steam stripping fractional distillation, superheating stripping steam is charged in tower bottom, tower top oil gas enters reflux pot on tower top after cooling, refined diesel oil at tower bottom enters one or more than one series connected vertical ionization dehydration pot after supercharging by pressure pump, heat exchanging and cooling; micro steam condensation water in the refined diesel oil aggregates to larger drip by high-voltage electric field in the ionization dehydration pot, sedimentates at pot bottom and is removed by dehydration pipeline; refined diesel oil without water comes from top of the ionization dehydration pot is the eligible final product. The invention also provides a device for realizing the method.
Description
Technical field
The present invention relates to a kind of diesel oil hydrogenation refining fractionation method, the present invention also relates to a kind of device of realizing this method simultaneously.
Background technology
Along with improving constantly that the oil quality of China is upgraded and required, the diesel oil hydrofining device is the main path that improves the diesel product quality.The diesel oil hydrofining device generally has single tower flow process and two kinds of the double-column processes that generally adopts at present early in design, both differences are that mainly double-column process Duoed a depriving hydrogen sulphide stripping tower than single tower flow process on the basis of separation column, thereby have solved the underproof problem of gasoline corrosion.No matter but be single tower flow process or double-column process, its separation column generally all is to adopt the steam stripped fractionation or adopt reboiler furnace to carry out fractionation.The steam stripped fractionation process is to go into a certain amount of superheated vapour in the separation column bottom blowing, to reduce oil gas dividing potential drop in the tower, helps the light constituent vaporization, at the bottom of the tower oil through pump boost the heat exchange cooling and behind the surge tank deposition dehydrating as the refined diesel oil product.Because adopt in the steam stripped fractionation process process, the refined diesel oil at the bottom of the tower has steam condenses inevitably, and lack effectively dehydration facility, thereby influence the refined diesel oil quality product, so now newly-built diesel hydrotreating unit all seldom adopts.
Present newly-built diesel hydrotreating unit is many, and what adopt is the technical process that reboiler furnace is set at the bottom of the separation column, this flow process is to be provided with process furnace at the bottom of separation column, at the bottom of oil returns separation column with the pump pump circulation at the bottom of the part tower after process furnace heats, for the product fractionation provides heat, at the bottom of another part tower oil after pump boosts heat exchange cooling as the refined diesel oil product;
Adopting the advantage of reboiler furnace flow process is the quality product height, and refined diesel oil is not moisture, but its shortcoming is to invest big, complicated operation, plant energy consumption height.The advantage that adopts separation column steam stripped flow process be reduced investment, simple to operate, plant energy consumption is low, easily is with water but shortcoming is a refined diesel oil.
" refining of petroleum and chemical industry " the 4th phase in 2006 had once disclosed one piece of name and had been called the article that the diesel oil hydrofining device is produced rocket engine fuel existing problems and solution, separation column wherein also is to adopt steam stripped, but install no effective dehydration means, treated oil often is with water at the bottom of the tower.
" oil refining design " the 3rd phase of nineteen ninety-five had once disclosed the article that one piece of name is called the novel fractionation flow scheme design of diesel oil hydrofining device, it is provided with reboiler furnace at the bottom of separation column, do not use steam stripped, at the bottom of the tower after the refined diesel oil product heat exchange cooling directly as qualified product.Its product is not moisture, steady quality, but the problem that exists is, use reboiler furnace that plant investment is increased, and operation energy consumption is also high, furnace maneuver is also complicated.
Therefore, in sum, all there is weak point in the prior art.
Summary of the invention
One of purpose of the present invention provides a kind of new diesel oil hydrogenation refining fractionation method, this method have reduce investment outlay, advantage simple to operate.
Above-mentioned purpose of the present invention realizes by following technical solution: a kind of diesel oil hydrogenation refining fractionation method, it is characterized in that this method comprises that a hydrogenation reaction generates oil vapour stripping fractionation process and a refined diesel oil ionization dehydration, wherein,
Described steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 210～290 ℃, fractionation tower temperature is 120～160 ℃, tower top pressure is 0.3～0.6Mpa, feed overheated stripped vapor at the bottom of separation column, the temperature of overheated stripped vapor is 250～400 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 30～50 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
Described ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 20～50 ℃ through the heat exchange cooling unit then, enter vertical ionization water knockout after the cooling;
(2) by 1.5～2.2 ten thousand volts high voltage direct current field action in the vertical ionization water knockout, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of ionization water knockout.
In order to prolong the time of electro-dewatering jar ionization dehydration, guarantee the effect of refined diesel oil dehydration, the electro-dewatering jar adopts vertical structure, and adopts multistage electro-dewatering, and promptly two or more electro-dewatering jar series connection are used.
The preferred implementation of diesel oil hydrogenation refining fractionation method of the present invention is: this method comprises that a hydrogenation reaction generates oil vapour stripping fractionation process and a refined diesel oil ionization dehydration, wherein,
Described steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 210～290 ℃, fractionation tower temperature is 120～160 ℃, tower top pressure is 0.6Mpa, feed overheated stripped vapor at the bottom of separation column, the temperature of stripped vapor is 250 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 40 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
Described ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 50 ℃ through the heat exchange cooling unit then, enter the electro-dewatering jar after the cooling;
(2) by 1.5～2.2 ten thousand volts high voltage direct current field action in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Stripped vapor described in the present invention can be the self-produced steam of waste heat boiler in the device, can be the steam of steam system pipe network in the factory also, needs only vapor pressure in the actually operating greater than the separation column internal pressure, normally adopts system's steam of 1.0Mpa.For making stripped vapor become 250 ℃～400 ℃ superheated vapour, can be with stripped vapor earlier through advancing separation column again after reaction heating furnace convection zone and the waste heat of flue gas of heating furnace heat exchange.
Another object of the present invention provides a kind of diesel oil hydrogenation refining fractionation device, and this device has the low and advantage simple to operate of operation energy consumption.
This purpose of the present invention realizes by the following technical solutions: a kind of diesel oil hydrogenation refining fractionation device, it comprises that hydrogenation reaction generates oil vapour stripping fractionation unit, this steam stripped fractionation unit comprises separation column, cat head water cooler and return tank of top of the tower, it is characterized in that described diesel oil hydrogenation refining fractionation device also comprises topping-up pump, refined diesel oil heat exchange cooling unit and refined diesel oil ionization water knockout, this water knockout adopts vertical water knockout, and described separation column, topping-up pump, refined diesel oil heat exchange cooling unit and refined diesel oil ionization water knockout link to each other successively.
The hydrofining reaction that is come by light pressure separator generates oil enters separation column with certain temperature opening for feed, separation column adopts the steam stripped fractionation, at the bottom of tower, feed stripped vapor, cat head oil gas enters return tank of top of the tower after cooling off, refined diesel oil at the bottom of the tower enters one or more placed in-line vertical ionization water knockouts after being cooled off through heat exchange by the topping-up pump supercharging, making micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down by the high-voltage electric field effect in the ionization water knockout takes off to jar end and by the dehydration pipeline, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of ionization water knockout, settled water is by the certain water level of variable valve control at the bottom of the electro-dewatering jar.
The present invention adopts vertical ionization water knockout, vertical ionization water knockout is because the difference of altitude of its opening for feed, discharge port is big, material is subjected to the effect of electric field time long in water knockout, plays the purpose that prolongs electro-dewatering jar ionization dewatering time, guarantees the effect of refined diesel oil dehydration.On the other hand, its opening for feed, the difference of altitude that discharge port is bigger help the sedimentation of water droplet in jar, thereby can reduce the water content of refined diesel oil product, improve the precision of product.Simultaneously, adopt vertical ionization water knockout, particularly when a plurality of vertical ionization water knockouts are connected, can save the space greatly.
The present invention can do following improvement: described ionization water knockout is one or more, a plurality of ionization water knockout series connection.Adopt a plurality of ionization water knockout series connection, can prolong the time of ionization water knockout ionization dehydration, guarantee the effect of refined diesel oil dehydration.
The middle and lower part of the electro-dewatering tank described in the present invention is equipped with the charging distribution pipe, the middle and upper part of tank body is equipped with battery lead plate, opening for feed is opened the sidewall at tank body, and be lower than the installation site of charging distribution pipe, a tank deck and a jar end, have discharge port and dehydrated mouth at center position, in the tank body and described discharge port opposite position place also is equiped with flow-stopping plate, and tank deck also has tank deck drain, high voltage electric intake and relief valve port.
Heat exchange cooling unit described in the present invention is an interchanger, and the entrance end of interchanger links to each other with the exit end of topping-up pump, and the exit end of interchanger links to each other with the entrance end of ionization water knockout.The diesel fuel temperature that enters the ionization water knockout is low more, and its dehydrating effect is good more.But the diesel fuel temperature of coming from topping-up pump is still very high usually, at this moment need and install interior other low temperature logistics that need heat up by the interchanger heat exchange with high temperature diesel oil, thereby reach the purpose of diesel fuel temperature reduction.
Heat exchange cooling unit among the present invention mainly comprises refined diesel oil interchanger and water cooler at the bottom of one or more towers, and these interchanger and water cooler generally link to each other in placed in-line mode, to reach better heat exchange effect.
Refined diesel oil is earlier by interior other low temperature logistics heat exchange that need heat up of refined diesel oil interchanger at the bottom of one or more towers and device at the bottom of the common tower, after the heat exchange at the bottom of the tower temperature of diesel oil then also to pass through air cooler or water cooler and air or water heat exchange as also failing to meet the requirements of temperature.Considering when the flow process of its concrete heat exchange will design according to device, mainly is to be purpose with energy-conservation.Typical heat exchange process is: the temperature that reduces diesel oil at the bottom of the separation column after oil and the raw material diesel oil heat exchange of advancing before the reaction feed process furnace again by air cooler.
The present invention is on the basis of traditional diesel oil hydrofining device separation column stripping fractionation flow process, by increasing an ionization dehydration newly at the separation column rear portion, thereby solves traditional moisture underproof problem of stripping fractionation flow process refined diesel oil.Compared with prior art, the present invention has following unusual effect:
1, facility investment relatively economizes.Technology of the present invention is compared with reboiler furnace technology, has reduced a reboiler furnace, two recycle pumps, though increased the electro-dewatering jar, the electro-dewatering jar is a generic container equipment, and investment is also little, and investment is still saved generally.
2, operation energy consumption is lower.Energy consumption in the technology normal running of the present invention is mainly stripped vapor and the electricity consumption of electro-dewatering jar.And the energy consumption in the normal running of reboiler furnace technology is mainly the fuel consumption of reboiler furnace and the current consumption of recycle pump, and the fuel consumption of reboiler furnace is very large.Same device employing technology ratio of the present invention employing reboiler furnace technology can be saved the energy consumption about 15%.
3, simple to operate, safe.Stripped vapor in the technology of the present invention and electro-dewatering jar all need not too much adjustment when device shutting down and normal running.Reboiler furnace technology increased the difficulty of device shutting down and normal running, and the security of process furnace is relatively poor relatively then because of many process furnace.
Diesel oil hydrogenation refining fractionation device of the present invention can be used for the fractionating system of all kinds of diesel oil hydrofining devices.Along with China's diesel product quality upgrading, incite somebody to action constantly newly-built or transformation diesel oil hydrofining device in the coming years, so this invention will have very big application prospect.
Description of drawings
Fig. 1 is the structural representation of the embodiment of the invention one;
Fig. 2 is the structural representation of electro-dewatering jar among Fig. 1;
Fig. 3 is the structural representation of the embodiment of the invention two.
Embodiment
Embodiment one
As Fig. 1, shown in Figure 2, a kind of diesel oil hydrogenation refining fractionation device, comprise that hydrogenation reaction generates oil vapour stripping fractionation unit, this steam stripped fractionation unit comprises separation column 3, cat head water cooler 14 and return tank of top of the tower 4, the sidewall of separation column 3 has hydrogenation reaction and gives birth to olefiant opening for feed 1 and stripped vapor inlet 2, wherein hydrogenation reaction is given birth to the top that olefiant opening for feed 1 is positioned at stripped vapor inlet 2, link to each other by cat head oil gas volatilization pipeline 9 between the cat head of separation column 3 and the cat head water cooler 14, draw two pipelines from return tank of top of the tower 4, be respectively reflux pipeline 15 and fuel dispensing outlet pipeline 15, wherein reflux pipeline 15 links to each other with the cat head of separation column 3, and fuel dispensing outlet pipeline 15 is directly exported gasoline.
This diesel oil hydrogenation refining fractionation device also comprises topping-up pump 5, refined diesel oil heat exchange cooling unit 6 and vertical electro-dewatering jar 7, separation column 3, topping-up pump 5, refined diesel oil heat exchange cooling unit 6 and vertical electro-dewatering jar 7 link to each other successively, heat exchange cooling unit 6 in the present embodiment is an interchanger, also can adopt the placed in-line mode of a plurality of interchanger, the topping-up pump egress line 10 of the entrance end of this interchanger and topping-up pump 5 links to each other, and the outlet line 11 of this interchanger links to each other with the opening for feed 72 of electro-dewatering jar 7.
As shown in Figure 2, the middle and lower part of electro-dewatering jar 7 tank bodies is equipped with charging distribution pipe 71, the middle and upper part of tank body is equipped with battery lead plate 74, opening for feed 72 is opened the sidewall at tank body, and its aperture position is lower than the installation site of charging distribution pipe 71, a tank deck and a jar end, have discharge port 77 and dehydrated mouth 73 at center position, wherein discharge port 77 links to each other with treated oil outlet line .12, with qualified refined diesel oil finished product output, dehydrated mouth 73 links to each other with dehydration pipeline 13, be used for water is discharged, settled water can be controlled certain water level by variable valve at the bottom of 7 jars in the electro-dewatering jar, in the tank body and discharge port 77 opposite position places also are equiped with flow-stopping plate 75, and tank deck also has tank deck drain 79, high voltage electric intake 78 and relief valve port 76.
Adopt said apparatus to carry out the method for diesel oil hydrogenation refining fractionation, this method can be divided into hydrogenation reaction and generate oil vapour stripping fractionation process and refined diesel oil ionization dehydration, wherein,
The steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 210 ℃, fractionation tower temperature is 120 ℃, tower top pressure is 0.3Mpa, at the bottom of separation column, feed overheated stripped vapor, stripped vapor adopts the self-produced 0.5Mpa steam of waste heat boiler, and through reaction heating furnace convection zone heat exchange to 250 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 30 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
The ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 20 ℃ through the heat exchange cooling unit then, enter the electro-dewatering jar after the cooling;
(2) by 1.5 ten thousand volts high-voltage electric field effect in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Adopt said apparatus to carry out the method for diesel oil hydrogenation refining fractionation, its operation steps also can adopt following step:
The steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 290 ℃, fractionation tower temperature is 160 ℃, tower top pressure is 0.6Mpa, at the bottom of separation column, feed overheated stripped vapor, stripped vapor adopts 1.0MPa system steam, and through reaction heating furnace convection zone heat exchange to 350 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 50 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
The ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 20～50 ℃ through the heat exchange cooling unit then, enter the electro-dewatering jar after the cooling;
(2) by 2.2 ten thousand volts high-voltage electric field effect in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Adopt said apparatus to carry out the method for diesel oil hydrogenation refining fractionation, its operation steps can also adopt following step:
The steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 240 ℃, fractionation tower temperature is 130 ℃, tower top pressure is 0.6Mpa, at the bottom of separation column, feed overheated stripped vapor, stripped vapor adopts 1.0MPa system steam, and through reaction heating furnace convection zone heat exchange to 260 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 40 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
The ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 50 ℃ through the heat exchange cooling unit then, enter the electro-dewatering jar after the cooling;
(2) by 2.2 ten thousand volts high-voltage electric field effect in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Embodiment two
That shown in Figure 3 is second embodiment of diesel oil hydrogenation refining fractionation device of the present invention, different with embodiment one is, adopt two placed in-line vertical electro-dewatering jars to carry out processed among the present invention, can certainly adopt a plurality of vertical electro-dewatering jars to carry out processed.
The device of employing present embodiment carries out the method for diesel oil hydrogenation refining fractionation, and this method can be divided into hydrogenation reaction and generate oil vapour stripping fractionation process and refined diesel oil ionization dehydration, wherein,
The steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 250 ℃, fractionation tower temperature is 150 ℃, tower top pressure is 0.6Mpa, at the bottom of separation column, feed overheated stripped vapor, stripped vapor adopts 1.0MPa system steam, and through reaction heating furnace convection zone heat exchange to 250 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 40 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
The ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 50 ℃ through the heat exchange cooling unit then, the cooling back enters two placed in-line vertical electro-dewatering jars from the middle part;
(2) by 2.2 ten thousand volts high-voltage electric field effect in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Embodiment three
Different with embodiment one is, heat exchange cooling unit in the present embodiment adopts interchanger and air cooler series combination formula structure, promptly this heat exchange cooling unit 6 adopts one or more interchanger and the placed in-line mode of air cooler, the exit end of last interchanger links to each other with the entrance end of air cooler, the entrance end of first interchanger links to each other with the exit end of topping-up pump 5, and the exit end of air cooler links to each other with the entrance end of electro-dewatering jar 7.
The device of employing present embodiment carries out the method for diesel oil hydrogenation refining fractionation, and this method can be divided into hydrogenation reaction and generate oil vapour stripping fractionation process and refined diesel oil ionization dehydration, wherein,
The steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 250 ℃, fractionation tower temperature is 150 ℃, tower top pressure is 0.6Mpa, at the bottom of separation column, feed overheated stripped vapor, stripped vapor adopts 1.0MPa system steam, and through reaction heating furnace convection zone heat exchange to 250 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 40 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
The ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, pass through interchanger and air cooler postcooling to 50 ℃ then, enter the electro-dewatering jar after the cooling;
(2) by 2.2 ten thousand volts high-voltage electric field effect in the electro-dewatering jar, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of electro-dewatering jar.
Embodiment four
Different with embodiment three is, heat exchange cooling unit 6 in the present embodiment adopts one or more interchanger and the placed in-line mode of water cooler, the exit end of last interchanger links to each other with the entrance end of water cooler, the entrance end of first interchanger links to each other with the exit end of topping-up pump 5, and the exit end of water cooler links to each other with the entrance end of electro-dewatering jar 7.Because glassware for drinking water has big specific heat, the diesel fuel temperature that enters electro-dewatering jar 7 can be cooled to a lower value.
Claims (8)
1. the fractionating method of a diesel oil hydrofining product is characterized in that this method comprises that a hydrogenation reaction generates oil vapour stripping fractionation process and a refined diesel oil ionization dehydration, wherein,
Described steam stripped process comprises the steps:
(1) hydrogenation reaction of coming from the reactive system light pressure separator generates the opening for feed that oil enters separation column, the feeding temperature of separation column is 210～290 ℃, fractionation tower temperature is 120～160 ℃, tower top pressure is 0.3～0.6Mpa, feed overheated stripped vapor at the bottom of separation column, the temperature of overheated stripped vapor is 250～400 ℃;
(2) hydrogenation reaction generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 30～50 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
Described ionization dehydration comprises the steps:
(1) with the refined diesel oil at the bottom of the separation column by the topping-up pump supercharging, be cooled to 20～50 ℃ through the heat exchange cooling unit then, enter vertical ionization water knockout after the cooling;
(2) by 1.5～2.2 ten thousand volts high voltage direct current field action in the vertical ionization water knockout, make the micro-steam condenses in the refined diesel oil be gathered into bigger drops of water fall down to a jar end, and by the dehydration pipeline take off, become the qualified refined diesel oil product of every index after water-free refined diesel oil comes out from the top of ionization water knockout.
2. the fractionating method of a kind of diesel oil hydrofining product according to claim 1 is characterized in that:
In the described steam stripped process, the tower top pressure in the step (1) is 0.6Mpa, and the temperature of overheated stripped vapor is 250 ℃; Hydrogenation reaction in the step (2) generates in the oil and to enter return tank of top of the tower after gasoline component and hydrogen sulfide enter cat head water cooler postcooling to 40 ℃ with stripped vapor, carries out gas, oil, water three phase separation;
In the described ionization dehydration, the refined diesel oil in the step (1) is cooled to 50 ℃ through the heat exchange cooling unit then by the topping-up pump supercharging, enters the ionization water knockout after the cooling.
3. the fractionating method of a kind of diesel oil hydrofining product according to claim 1 and 2, it is characterized in that: described stripped vapor is the self-produced steam of waste heat boiler in the use device or the steam of the full 1.0Mpa of factory steam system, and is through the superheated vapour behind reaction heating furnace convection zone and the heating furnace high-temperature flue gas heat exchange.
4. device of realizing the fractionating method of the described diesel oil hydrofining product of claim 1, it comprises that hydrogenation reaction generates oil vapour stripping fractionation unit, this steam stripped fractionation unit comprises separation column, cat head water cooler and return tank of top of the tower, it is characterized in that: the fractionation plant of described diesel oil hydrofining product also comprises topping-up pump, refined diesel oil heat exchange cooling unit and refined diesel oil ionization water knockout, this water knockout adopts vertical water knockout, and described separation column, topping-up pump, refined diesel oil heat exchange cooling unit and refined diesel oil ionization water knockout link to each other successively.
5. the fractionation plant of a kind of diesel oil hydrofining product according to claim 4 is characterized in that: described vertical ionization water knockout is one or more, a plurality of ionization water knockout series connection.
6. according to the fractionation plant of claim 4 or 5 described a kind of diesel oil hydrofining products, it is characterized in that: the middle and lower part of described ionization water knockout tank body is equipped with the charging distribution pipe, the middle and upper part of tank body is equipped with battery lead plate, opening for feed is opened the sidewall at tank body, and be lower than the installation site of charging distribution pipe, a tank deck and a jar end, have discharge port and dehydrated mouth at center position, in the tank body and described discharge port opposite position place also is equiped with flow-stopping plate, and tank deck also has tank deck drain, high voltage electric intake and relief valve port.
7. according to the fractionation plant of claim 4 or 5 described a kind of diesel oil hydrofining products, it is characterized in that: described heat exchange cooling unit is an interchanger, the entrance end of this interchanger links to each other with the exit end of topping-up pump, and the exit end of this interchanger links to each other with the entrance end of ionization water knockout.
8. the fractionation plant of a kind of diesel oil hydrofining product according to claim 7 is characterized in that: described interchanger is one or more, and a plurality of interchanger are connected successively.
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| CN101580731B (en) * | 2008-05-15 | 2012-10-17 | 中国石油天然气股份有限公司 | Method for improving diesel oil yield of gasoline and diesel oil fractionating tower |
| CN102373074B (en) * | 2010-08-21 | 2013-11-27 | 中国石油化工股份有限公司 | Sump oil electric dehydration device |
| CN102373073B (en) * | 2010-08-21 | 2013-09-11 | 中国石油化工股份有限公司 | Hydrocarbon oil electric dehydration apparatus |
| CN103421542B (en) * | 2013-08-08 | 2015-03-11 | 华南理工大学 | Diesel hydrogenation process |
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| CN107267202B (en) * | 2017-07-20 | 2023-04-25 | 武汉轻工大学 | Method and device for stripping fractionation and negative pressure desorption of hydrogenated diesel refinery gas |
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| CN113999698A (en) * | 2020-07-27 | 2022-02-01 | 中国石油化工股份有限公司 | Diesel oil dehydration device, stripping system and diesel oil dehydration method |
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2007
- 2007-04-13 CN CNB2007100275610A patent/CN100519700C/en active Active
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