CN201506772U - System of double hydrogenation device for preparing high-quality diesel oil - Google Patents
System of double hydrogenation device for preparing high-quality diesel oil Download PDFInfo
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- CN201506772U CN201506772U CN2009202228286U CN200920222828U CN201506772U CN 201506772 U CN201506772 U CN 201506772U CN 2009202228286 U CN2009202228286 U CN 2009202228286U CN 200920222828 U CN200920222828 U CN 200920222828U CN 201506772 U CN201506772 U CN 201506772U
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Abstract
The utility model relates to a system of a double hydrogenation device for preparing high-quality diesel oil, which comprises an extraction device and is characterized in that the top part of the extraction device is connected with a raffinate oil water scrubbing tower through a pipeline; the top part of the raffinate oil water scrubbing tower is connected with a raffinate oil hydrogenation reaction system through the pipeline; the bottom part of the extraction device is connected with a backwashing tower through the pipeline; the top part of the backwashing tower is connected with an extract oil water scrubbing tower through the pipeline; the bottom part of the backwashing tower is connected with a recovery tower through the pipeline; the top part of the extract oil water scrubbing tower is connected with an extract oil cutting tower; and the bottom part of the extract oil cutting tower is connected with a heavy aromatic hydrogenation reaction system through the pipeline. The hydrogenation device only aims to raffinate oil or extract oil under the special requirements and has the advantages of small scale and low cost.
Description
Technical field
The utility model relates to a kind of preparation system of diesel oil, particularly a kind of system of tow double hydrogenation units for preparing high-quality diesel.
Background technology
Catalytic cracking, catalytic pyrolysis and heavy oil catalytic pyrolysis technology are the core technologies of oil refining, and catalytic cracking is divided into wax catalysis cracking, heavy oil fluid catalytic cracking; Be referred to as catalytic hydrocarbon from the generation oil of these explained hereafter, the gained catalytic hydrocarbon is through processing treatment, generally be the separation column fractionation, can fractionate out products such as net gas, liquefaction vapour, diesel oil, diesel oil, heavy oil, wherein diesel oil, more than 70% of diesel oil total supply on diesel oil, the diesel oil occuping market.
Along with the more and more strictness of environmental requirement, it is more and more stricter that the specification of petroleum products (fuel) also becomes.With diesel oil is example, and new in recent years diesel oil specification is implemented in succession in states such as the U.S., Europe, Japan, and China also implements GB 252-2000 diesel oil new standard in January, 2002.Under new standard, existing catalytic diesel oil shows following deficiency through the processing and treating method of Cutting Tap cutting (fractionation): a diesel quality that is this treatment process is produced has much room for improvement, and diesel-fuel cetane number is on the low side, and stability is undesirable; The 2nd, the needed hydrogenation scale of above-mentioned treatment process is bigger than normal, causes full factory hydrogen consumption too high; The 3rd, the diesel cetane-number of being produced is low excessively, can't satisfy market demands.The principal element that influences the diesel product quality is the sulphur content and the diesel-fuel cetane number of diesel oil.Diesel-fuel cetane number is the key problem of diesel quality, the major measure that increases the catalytic diesel oil cetane value at present is high-pressure hydrogenation and high-pressure hydrogenation combination technique, catalytic diesel oil cetane value after high-pressure hydrogenation and the processing of high-pressure hydrogenation combination technique has a more substantial increase, but the construction investment of this technology is huge, running cost is very high, be subjected to the hydrogen resource limit.
There is following point in above-mentioned measure: there is the irrational utilization of resource simultaneously in the restriction that 1. construction investment is huge, process cost is high, scale is subjected to raw material; 2. adopt new catalyst, can increase diesel-fuel cetane number, still, can cause increasing considerably of hydrogen consumption; 3. adjust diesel oil boiling range scope, increase the measure of diesel cetane-number, it is little to adjust remaining, also can cause the sulphur content in the diesel oil to increase.
Europe has come into effect new Europe VI diesel oil standard at present, wherein requires the sulphur content of diesel oil to be not more than 0.005% (wt), and aromaticity content is not more than 15%, and density is not more than 825kg/m
3, polycyclic aromatic hydrocarbons is not more than 2%.For the most refinery of China, equally also must require in the face of higher national IV diesel oil standard: sulphur content is not more than 0.005% (wt), and aromaticity content is not more than 15%.The diesel quality solution must be considered the transition from national III diesel oil standard to national IV diesel oil standard, and programme should be disposable according to national IV diesel oil standard programme preferably.
Because ratio and developed country's difference of each blend component are very big in China's diesel product, catalytic cracking diesel oil occupies very high ratio, and this situation is with long-term existence.Therefore, diesel quality upgrading problem of falling sulphur and raising cetane value to be solved needs to be resolved hurrily.
Therefore, provide the treatment system of the high blended diesel of a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content and cetane value just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides a kind of low cost, less energy-consumption, low hydrogen consumption, pollution-free preparation low sulfur content and improves the system of diesel cetane-number.
For achieving the above object, the utility model is taked following technical scheme:
A kind of system for preparing high-quality diesel comprises extraction plant; It is characterized in that: described extraction plant top is connected with the water wash column of raffinating oil by pipeline; The described water wash column top of raffinating oil is connected with the hydrogenation reaction system of raffinating oil by pipeline; The described hydrogenation reaction system bottom of raffinating oil is by the direct extraction product of pipeline; Described extraction plant bottom is connected with back scrubber by pipeline; Described back scrubber top is connected with the oily water wash column of extraction by pipeline; Described back scrubber bottom is connected with recovery tower by pipeline; Described extraction profit is washed top of tower and is connected with the oily Cutting Tap of extraction by pipeline; The oily Cutting Tap of described extraction top is connected with the bottom of recovery tower with described extraction plant and described back scrubber by pipeline; The oily Cutting Tap of described extraction bottom links to each other with the heavy aromatics hydrogenation reaction system by pipeline, and the oily Cutting Tap side line of described extraction is by the light aromatic hydrocarbon product of the direct extraction of pipeline; Described heavy aromatics hydrogenation reaction system bottom is in harmonious proportion by the product and the described product of raffinating oil hydrogenation reaction system bottom extraction of pipeline extraction; Described recovery tower upper top is connected with the bottom of described extraction plant and the bottom of described back scrubber respectively by pipeline; Described recovery tower bottom is connected with the top of described extraction plant by pipeline.
Straight-run diesel oil of the present utility model, catalytic diesel oil and coker gas oil can be arbitrary proportions.
The cut point (boiling range) of light aromatic hydrocarbons of the present utility model and heavy aromatics can be adjusted.
The used back scrubber of the utility model, water wash column, recovery tower and Cutting Tap are conventional back scrubber, water wash column, recovery tower and Cutting Tap.Used extraction plant is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The used hydrogenation reaction system of the utility model is existing hydrogenation system, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser, stabilizer tower etc.
Beneficial effect:
The advantage of the preparation low sulfur content of the present utility model and the system of low olefin-content diesel oil is: compare with the hydrorefined mode of ordinary diesel oil, hydrogenation unit of the present utility model only at raffinate oil or special requirement under extraction oil, small scale, cost is low; Simultaneously, straight-run diesel oil is not only handled in the raw material variation that the utility model is handled, can also handle catalytic diesel oil and and the mixture of coker gas oil; And the utility model is separated aromatic hydrocarbons from diesel oil, has improved diesel-fuel cetane number greatly, has reduced condensation point of diesel oil; At last, the utility model can under the situation that satisfies condensation point of diesel oil and aromaticity content, enter part or all of mediation of aromatic component in the diesel oil according to practical situation, increases production of diesel oil.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment.
Below by embodiment the utility model is described further, but and does not mean that restriction the utility model protection domain.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
As shown in Figure 1, be 160-365 ℃ with boiling range, sulphur content is 2900ppm, density is 816.3kg/m
3Aromaticity content is 18%, to be 50.9 straight-run diesel oil (feedstock property sees Table 1-1) add extraction tower 1 with 100 tons/hour flow and solvent with 300 tons/hour flow to cetane value together carries out extracting, the temperature of extraction tower 1 is 175 ℃, and pressure is 0.8MPa, and solvent ratio is 6, solvent for use is a tetramethylene sulfone, the boiling range that gained is raffinated oil is 160-342 ℃, and sulphur content is 409.4ppm, and density is 805.4kg/m
3, aromaticity content is 5.03%, cetane value is 56.5; The boiling range that gained is extracted oil out is 160-388 ℃, and sulphur content is 17013.3ppm, and density is 884.1kg/m
3, aromaticity content is 91.5%, cetane value is 19.3.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 85 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 7.8 tons/hour flow, the service temperature of water wash column 2-1 of raffinating oil is 60 ℃, working pressure is 0.5MPa, raffinating oil after the gained washing mixed 0.25 ton/hour hydrogen with 85 tons/hour flow by water wash column 2-1 top and entered the hydrogenation reaction system 3-1 that raffinates oil and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 7.8 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator among the described hydrogenation reaction system 3-1 that raffinates oil is 260 ℃, and reaction pressure is 2.0MPa, and hydrogen-oil ratio is 300, and air speed is 1.5h
-1, the gained hydrogenation is raffinated oil and is in harmonious proportion the direct extraction of product with 85 tons/hour flow as diesel oil.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 315 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 45 tons/hour the lotion that returns enters by back scrubber 5 bottoms, the service temperature of back scrubber 5 is 80 ℃, and working pressure is 0.5MPa, returns and washes than 0.3.24 tons/hour in the extraction of back scrubber 5 cat head extraction oil and the mixture that returns lotion enter by pipeline and extract oily water wash column 2-2 middle part out, meanwhile, washing water enters for 4.6 tons/hour extracts oily water wash column 2-2 top out, the service temperature of the oily water wash column 2-2 of described extraction is 60 ℃, and working pressure is 0.5MPa.Extraction oil after the washing enters the oily Cutting Tap 4 of extraction by the extraction of the oily water wash column 2-2 cat head of extraction, directly discharges bottom the oily water wash column 2-2 of extraction for 4.6 tons/hour through the washing water that uses.110 ℃ of oily Cutting Tap 4 tower top temperatures of described extraction, column bottom temperature is 260 ℃, tower top pressure 0.15MPa, tower bottom pressure 0.18MPa, reflux ratio is 10.Flow be 9.0 tons/hour return lotion from the oily Cutting Tap 4 top extraction of described extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons is from the direct extraction of flow product with 2.96 tons/hour of the side line of the oily Cutting Tap 4 of described extraction; Heavy aromatics mixes 0.28 ton/hour hydrogen from the bottom of oily Cutting Tap 4 towers of described extraction with 12.04 tons/hour flow and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described heavy aromatics hydrogenation reaction system 3-2 is 300 ℃, reaction pressure is 4.0MPa, hydrogen-oil ratio is 300, and air speed is 1.0h
-1, gained hydrogenation heavy aromatics is raffinated oil with 12.04 tons/hour flow extraction and with described hydrogenation of raffinating oil hydrogenation reaction system 3-1 extraction and is mixed as diesel oil blending component.The solvent of extraction and the mixture that returns lotion enter recovery tower 6,120 ℃ of the tower top temperatures of recovery tower 6,180 ℃ of column bottom temperatures, roof pressure power 0.20MPa, tower bottom pressure 0.24MPa with 336 tons/hour flow at the bottom of back scrubber 5 towers.The lotion that returns of recovery tower 6 cat head extraction enters the bottom of back scrubber 5 bottoms and extraction tower 1 with 36 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 300 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 1-2,1-3.
Embodiment 2
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
As shown in Figure 1, be 160-365 ℃ with boiling range, sulphur content is 3700ppm, density is 866.8kg/m
3Aromaticity content is 58%, to be 28.9 catalytic diesel oil (feedstock property sees Table 2-1) add extraction tower 1 with 100 tons/hour flow and solvent with 1020 tons/hour flow to cetane value together carries out extracting, the temperature of extraction tower 1 is 150 ℃, and pressure is 0.65MPa, and solvent ratio is 4, solvent for use is a N-Methyl pyrrolidone, the boiling range that gained is raffinated oil is 160-345 ℃, and sulphur content is 906.1ppm, and density is 831.4kg/m
3, aromaticity content is 22.9%, cetane value is 43.1; The boiling range that gained is extracted oil out is 160-386 ℃, and sulphur content is 6384.3ppm, and density is 903.8kg/m
3, aromaticity content is 91.7%, cetane value is 15.3.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 49 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 4.5 tons/hour flow, the service temperature of water wash column 2-1 of raffinating oil is 80 ℃, working pressure is 0.6MPa, raffinating oil after the gained washing mixed 0.36 ton/hour hydrogen with 49 tons/hour flow by water wash column 2-1 top and entered the hydrogenation reaction system 3-1 that raffinates oil and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 4.5 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator among the described hydrogenation reaction system 3-1 that raffinates oil is 290 ℃, and reaction pressure is 3.0MPa, and hydrogen-oil ratio is 300, and air speed is 2.5h
-1, the gained hydrogenation is raffinated oil and is in harmonious proportion the direct extraction of product with 49 tons/hour flow as diesel oil.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 1071 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 153 tons/hour the lotion that returns enters by back scrubber 5 bottoms, the service temperature of back scrubber 5 is 100 ℃, working pressure is 0.7MPa, returns and washes than 0.7.89.25 tons/hour in the extraction of back scrubber 5 cat head extraction oil and the mixture that returns lotion enter by pipeline and extract oily water wash column 2-2 middle part out, meanwhile, washing water enters for 15.6 tons/hour extracts oily water wash column 2-2 top out, the service temperature of the oily water wash column 2-2 of described extraction is 80 ℃, and working pressure is 0.65MPa.Extraction oil after the washing enters the oily Cutting Tap 4 of extraction by the extraction of the oily water wash column 2-2 cat head of extraction, directly discharges bottom the oily water wash column 2-2 of extraction for 15.6 tons/hour through the washing water that uses.130 ℃ of oily Cutting Tap 4 tower top temperatures of described extraction, column bottom temperature is 270 ℃, tower top pressure 0.18MPa, tower bottom pressure 0.21MPa, reflux ratio is 8.Flow be 38.25 tons/hour return lotion from the oily Cutting Tap 4 top extraction of described extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons from the side line of the oily Cutting Tap 4 of described extraction with 10.15 tons/hour flow as the direct extraction of product; Heavy aromatics mixes 2.29 tons/hour hydrogen from the bottom of oily Cutting Tap 4 towers of described extraction with 40.85 tons/hour flow and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described heavy aromatics hydrogenation reaction system 3-2 is 330 ℃, reaction pressure is 5.0MPa, hydrogen-oil ratio is 300, and air speed is 1.5h
-1, gained hydrogenation heavy aromatics is in harmonious proportion with 10.15 tons/hour flow extraction and with the diesel oil of the described hydrogenation reaction system 3-1 extraction of raffinating oil.The solvent of extraction and the mixture that returns lotion enter recovery tower 6,110 ℃ of the tower top temperatures of recovery tower 6,160 ℃ of column bottom temperatures, roof pressure power 0.15MPa, tower bottom pressure 0.18MPa with 1134.75 tons/hour flow at the bottom of back scrubber 5 towers.The lotion that returns of recovery tower 6 cat head extraction enters the bottom of back scrubber 5 bottoms and extraction tower 1 with 114.75 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 1020 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 2-2,2-3.
Embodiment 3
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
As shown in Figure 2, be 160-365 ℃ with boiling range, sulphur content is 3300ppm, density is 835.6kg/m
3Aromaticity content is 33.6%, to be 41.3 straight-run diesel oil add extraction tower 1 with 100 tons/hour flow and solvent with 520 tons/hour flow with the mixture (feedstock property sees Table 3-1) of coker gas oil to cetane value carries out extracting, the temperature of extraction tower 1 is 90 ℃, and pressure is 0.5MPa, and solvent ratio is 2, solvent for use is a dimethyl sulfoxide (DMSO), the boiling range that gained is raffinated oil is 160-339 ℃, and sulphur content is 535.1ppm, and density is 817.4kg/m
3, aromaticity content is 13.4%, cetane value is 49.1; The boiling range that gained is extracted oil out is 160-392 ℃, and sulphur content is 11169.2ppm, and density is 892.1kg/m
3, aromaticity content is 91.1%, cetane value is 19.2.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 74 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 6.8 tons/hour flow, the service temperature of water wash column 2-1 of raffinating oil is 100 ℃, working pressure is 0.7MPa, raffinating oil after the gained washing mixed 0.30 ton/hour hydrogen with 74 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3-1 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 6.8 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator among the described hydrogenation reaction system 3-1 is 260 ℃, and reaction pressure is 2.0MPa, and hydrogen-oil ratio is 300, and air speed is 1.5h
-1, the gained hydrogenation is raffinated oil and is in harmonious proportion the direct extraction of product with 74 tons/hour flow as diesel oil.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 546 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 78 tons/hour the lotion that returns enters by back scrubber 5 bottoms, the service temperature of back scrubber 5 is 120 ℃, working pressure is 0.8MPa, returns and washes than 1.0.49.4 tons/hour in the extraction of back scrubber 5 cat head extraction oil and the mixture that returns lotion enter by pipeline and extract oily water wash column 2-2 middle part out, meanwhile, washing water enters for 8.0 tons/hour extracts oily water wash column 2-2 top out, the service temperature of the oily water wash column 2-2 of described extraction is 100 ℃, and working pressure is 0.7MPa.Extraction oil after the washing enters the oily Cutting Tap 4 of extraction by the extraction of the oily water wash column 2-2 cat head of extraction, directly discharges bottom the oily water wash column 2-2 of extraction for 8.0 tons/hour through the washing water that uses.140 ℃ of oily Cutting Tap 4 tower top temperatures of described extraction, column bottom temperature is 390 ℃, tower top pressure 0.20MPa, tower bottom pressure 0.25MPa, reflux ratio is 6.Flow be 23.4 tons/hour return lotion from the oily Cutting Tap 4 top extraction of described extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons from the side line of the oily Cutting Tap 4 of described extraction with 5.04 tons/hour flow as the direct extraction of product; Heavy aromatics mixes 0.89 ton/hour hydrogen from the bottom of oily Cutting Tap 4 towers of described extraction with 20.96 tons/hour flow and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described heavy aromatics hydrogenation reaction system 3-2 is 300 ℃, reaction pressure is 6.0MPa, hydrogen-oil ratio is 300, and air speed is 2.0h
-1, gained hydrogenation heavy aromatics is in harmonious proportion with 20.96 tons/hour flow extraction and with the diesel oil of the described hydrogenation reaction system 3-1 extraction of raffinating oil.The solvent of extraction and the mixture that returns lotion enter recovery tower 6,100 ℃ of the tower top temperatures of recovery tower 6,145 ℃ of column bottom temperatures, roof pressure power 0.12MPa, tower bottom pressure 0.15MPa with 574.6 tons/hour flow at the bottom of back scrubber 5 towers.The lotion that returns of recovery tower 6 cat head extraction enters the bottom of back scrubber 5 bottoms and extraction tower 1 with 54.6 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 520 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 3-2,3-3.
Table 1 embodiment 1 raw material and product property table
Table 1-1 feedstock property
| Project | Unit | Numerical value | Method |
| Flow | Ton/hour | 100.0 |
Table 1-2 blended diesel product property table
The light aromatic hydrocarbon product property list of table 1-3:
Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Diesel cetane-number is tested with GB/T386; The density of diesel oil is tested with GB/T1884-1885; Diesel oil boiling range scope is tested with GB/T6536.
Table 2 embodiment 2 raw materials and product property table
Table 2-1 feedstock property
| Project | Unit | Numerical value | Method |
| Flow | Ton/hour | 100.0 | |
| Sulphur content | ppm | 3700 | GB/T261 |
| Aromaticity content | m％ | 58.0 | GB/T0174 |
Table 2-2 blended diesel product property table
The light aromatic hydrocarbon product property list of table 2-3:
Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Diesel cetane-number is tested with GB/T386; The density of diesel oil is tested with GB/T1884-1885; Diesel oil boiling range scope is tested with GB/T6536.
Table 3 embodiment 3 raw materials and product property table
Table 3-1 feedstock property
Table 3-2 blended diesel product property table
The light aromatic hydrocarbon product property list of table 3-3:
Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Diesel cetane-number is tested with GB/T386; The density of diesel oil is tested with GB/T1884-1885; Diesel oil boiling range scope is tested with GB/T6536.
Claims (1)
1. a system for preparing high-quality diesel comprises extraction plant; It is characterized in that: described extraction plant top is connected with the water wash column of raffinating oil by pipeline; The described water wash column top of raffinating oil is connected with the hydrogenation reaction system of raffinating oil by pipeline; The described hydrogenation reaction system bottom of raffinating oil is by the direct extraction product of pipeline; Described extraction plant bottom is connected with back scrubber by pipeline; Described back scrubber top is connected with the oily water wash column of extraction by pipeline; Described back scrubber bottom is connected with recovery tower by pipeline; Described extraction profit is washed top of tower and is connected with the oily Cutting Tap of extraction by pipeline; The oily Cutting Tap of described extraction top is connected with the bottom of recovery tower with described extraction plant and described back scrubber by pipeline; The oily Cutting Tap of described extraction bottom links to each other with the heavy aromatics hydrogenation reaction system by pipeline, and the oily Cutting Tap side line of described extraction is by the light aromatic hydrocarbon product of the direct extraction of pipeline; Described heavy aromatics hydrogenation reaction system bottom is in harmonious proportion by the product and the described product of raffinating oil hydrogenation reaction system bottom extraction of pipeline extraction; Described recovery tower upper top is connected with the bottom of described extraction plant and the bottom of described back scrubber respectively by pipeline; Described recovery tower bottom is connected with the top of described extraction plant by pipeline.
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| CN2009202228286U CN201506772U (en) | 2009-09-18 | 2009-09-18 | System of double hydrogenation device for preparing high-quality diesel oil |
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| CN2009202228286U CN201506772U (en) | 2009-09-18 | 2009-09-18 | System of double hydrogenation device for preparing high-quality diesel oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011032352A2 (en) * | 2009-09-18 | 2011-03-24 | 北京金伟晖工程技术有限公司 | System for hydrogenating a raffinate to produce high quality diesel and method thereof |
| CN102021022B (en) * | 2009-09-18 | 2014-03-26 | 北京金伟晖工程技术有限公司 | System for preparing high-quality diesel with dual-hydrogenation unit and method thereof |
-
2009
- 2009-09-18 CN CN2009202228286U patent/CN201506772U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011032352A2 (en) * | 2009-09-18 | 2011-03-24 | 北京金伟晖工程技术有限公司 | System for hydrogenating a raffinate to produce high quality diesel and method thereof |
| WO2011032352A3 (en) * | 2009-09-18 | 2011-05-12 | 北京金伟晖工程技术有限公司 | System for hydrogenating raffinate to produce high quality diesel and method thereof |
| CN102021022B (en) * | 2009-09-18 | 2014-03-26 | 北京金伟晖工程技术有限公司 | System for preparing high-quality diesel with dual-hydrogenation unit and method thereof |
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