CN201506776U - Extracted oil hydrogenation system for preparing high-quality diesel oil - Google Patents
Extracted oil hydrogenation system for preparing high-quality diesel oil Download PDFInfo
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- CN201506776U CN201506776U CN2009202228322U CN200920222832U CN201506776U CN 201506776 U CN201506776 U CN 201506776U CN 2009202228322 U CN2009202228322 U CN 2009202228322U CN 200920222832 U CN200920222832 U CN 200920222832U CN 201506776 U CN201506776 U CN 201506776U
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Abstract
The utility model relates to an extracted oil hydrogenation system for preparing high-quality diesel oil. The system comprises an extraction device, and is characterized in that the top portion of the extraction device is connected with a raffinate oil water scrubber through a pipeline, the top portion of the raffinate oil water scrubber is connected with a raffinate oil hydrogenation reaction system through a pipeline, the bottom of the extraction device is connected with a re-washing column through a pipeline, the top portion of the re-washing column is connected with an extracted oil water scrubber through a pipeline, the bottom of the re-washing column is connected with a recovery tower through a pipeline, the top portion of the extracted oil water scrubber is connected with an extracted oil cutting tower through a pipeline, the side line of the extracted oil cutting tower is connected with the bottom pipeline of the raffinate oil hydrogenation reaction system through a pipeline, and the bottom of the extracted oil cutting tower is connected with the bottom pipeline of the raffinate oil hydrogenation reaction system through a pipeline. The hydrogenation device of the utility model is especially suitable for raffinate oil or extracted oil under special requirements, and has 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 preparing high-quality diesel by extract oil hydrogenation.
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 fractionated processing and treating method of Cutting Tap: 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 described recovery tower with described extraction plant and described back scrubber respectively by pipeline; The oily Cutting Tap side line of described extraction is connected with the described hydrogenation reaction system bottom line of raffinating oil by pipeline or the oily Cutting Tap of described extraction bottom is connected with the described hydrogenation reaction system bottom line of raffinating oil by pipeline; Described recovery tower 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 one of the utility model embodiment;
Fig. 2 is the schematic flow sheet of another embodiment of the utility model.
Below by embodiment the utility model is described further, but and does not mean that restriction the utility model protection domain.
Embodiment
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 4000ppm, density is 815.2kg/m
3Aromaticity content is 22%, to be 49 straight-run diesel oil (feedstock property sees Table 1-1) add extraction tower 1 with 100 tons/hour flow and solvent with 360 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 160-341 ℃, and sulphur content is 585.4ppm, and density is 801.4kg/m
3, aromaticity content is 6.7%, cetane value is 55.6; The boiling range that gained is extracted oil out is 160-389 ℃, and sulphur content is 19555.6ppm, and density is 884.6kg/m
3, aromaticity content is 91.5%, cetane value is 19.0.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 82 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 7.3 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 0.4 ton/hour hydrogen with 82 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 7.3 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 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 with 82 tons/hour flow directly as the product extraction.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 378 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 54 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 0.3.28.8 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 6.1 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 4-2 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 6.1 tons/hour through the washing water that uses.110 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 260 ℃, tower top pressure 0.15MPa, tower bottom pressure 0.18MPa, reflux ratio is 10.Flow be 10.8 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons is in harmonious proportion product extraction and with described hydrogenation raffinate oil mixes as accent diesel oil and product with 3.57 tons/hour flow as diesel oil from the side line of the oily Cutting Tap 4-2 of described extraction, heavy aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 14.43 tons/hour flow as and the direct extraction of product (performance of gained heavy aromatics product sees Table 1-3).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 403.2 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 43.2 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 360 tons/hour flow at the bottom of recovery tower 6 towers.Gained blended diesel product property sees Table 1-2.
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 2900ppm, density is 843.8kg/m
3Aromaticity content is 52%, to be 30 catalytic diesel oil (feedstock property sees Table 2-1) add extraction tower 1 with 100 tons/hour flow and solvent with 920 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 160-343 ℃, and sulphur content is 1020.4ppm, and density is 827.2kg/m
3, aromaticity content is 19.1%, cetane value is 43.6; The boiling range that gained is extracted oil out is 160-387 ℃, and sulphur content is 5106.5ppm, and density is 864.2kg/m
3, aromaticity content is 90.6%, cetane value is 14.0.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 54 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 4.9 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 0.56 ton/hour hydrogen with 54 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 4.9 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 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 with 54 tons/hour flow directly as the product extraction.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 966 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 138 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 0.7.80.5 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 14.1 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 4-2 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 14.1 tons/hour through the washing water that uses.130 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 270 ℃, tower top pressure 0.18MPa, tower bottom pressure 0.21MPa, reflux ratio is 8.Flow be 34.5 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons is in harmonious proportion product extraction with 9.12 tons/hour flow as diesel oil from the side line of the oily Cutting Tap 4-2 of described extraction and raffinates oil with described hydrogenation and mix as accent diesel oil and product, heavy aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 36.88 tons/hour flow as and the direct extraction of product (performance of gained heavy aromatics product sees Table 2-3).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 1023.5 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 103.5 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 920 tons/hour flow at the bottom of recovery tower 6 towers.Gained blended diesel product property sees Table 2-2.
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 2900ppm, density is 825.2kg/m
3Aromaticity content is 24%, to be 41 straight-run diesel oil add extraction tower 1 with 100 tons/hour flow and solvent with 420 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 160-341 ℃, and sulphur content is 440.5ppm, and density is 811.4kg/m
3, aromaticity content is 6.1%, cetane value is 46.8; The boiling range that gained is extracted oil out is 160-389 ℃, and sulphur content is 12152.4ppm, and density is 881.6kg/m
3, aromaticity content is 91.5%, cetane value is 19.1.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 79 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 7.2 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 0.25 ton/hour hydrogen with 79 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 7.2 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 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 with 79 tons/hour flow directly as the product extraction.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 420 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 63 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 1.0.39.9 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 6.4 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 4-2 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 6.4 tons/hour through the washing water that uses.140 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 390 ℃, tower top pressure 0.20MPa, tower bottom pressure 0.25MPa, reflux ratio is 6.Flow be 18.9 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; Light aromatic hydrocarbons is in harmonious proportion product direct extraction (performance of gained light aromatic hydrocarbon product see Table 3-3) with 4.16 tons/hour flow as gasoline from the side line of the oily Cutting Tap 4-2 of described extraction, and heavy aromatics is raffinated oil with the gained hydrogenation with 16.84 tons/hour flow extraction from the bottom of the oily Cutting Tap 4-2 of described extraction tower and mixed as diesel oil mediation product.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 441 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 44.1 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 420 tons/hour flow at the bottom of recovery tower 6 towers.Gained blended diesel product property sees Table 3-2.
Table 1 embodiment 1 raw material and product property table
Table 1-1 feedstock property
Table 1-2 blended diesel product property table
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 85.57 |
Table 1-3 heavy aromatics product property table:
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
Table 2-2 blended diesel product property table
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 63.12 | |
| Sulphur content | ppm | 159.2 | GB/T261 |
Table 2-3 heavy aromatics product property table:
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
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 95.84 | |
| Sulphur content | ppm | 479.2 | GB/T261 |
| Aromaticity content | m％ | 21.04 | GB/T0118 |
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 described recovery tower with described extraction plant and described back scrubber respectively by pipeline; The oily Cutting Tap side line of described extraction is connected with the described hydrogenation reaction system bottom line of raffinating oil by pipeline or the oily Cutting Tap of described extraction bottom is connected with the described hydrogenation reaction system bottom line of raffinating oil by pipeline; Described recovery tower 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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| CN2009202228322U CN201506776U (en) | 2009-09-18 | 2009-09-18 | Extracted oil hydrogenation system for preparing high-quality diesel oil |
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| CN2009202228322U CN201506776U (en) | 2009-09-18 | 2009-09-18 | Extracted oil hydrogenation system for preparing high-quality diesel oil |
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