CN102021024B - System for producing diesel of high quality and method thereof - Google Patents
System for producing diesel of high quality and method thereof Download PDFInfo
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Abstract
The present invention relates to a system for producing diesel of high quality and method thereof. The system comprises an extraction unit. The system is characterized in that the top of the extraction unit is connected with a raffinate-oil washing tower via pipes, the top of the raffinate-oil washing tower is connected with a hydrogenation reaction system via pipes, products are extracted from the bottom of the hydrogenation reaction system via pipes, the bottom of the extraction unit is connected with a return washing tower via pipes, the top of the return washing tower is connected with an extract-oil washing tower via pipes, the bottom of the return washing tower is connected with a recovery tower, the top of the extract-oil washing tower is connected with a extract-oil cutting tower via pipes, the top of the extract-oil cutting tower is connected respectively with the bottom of the extraction unit and connected with the bottom of the return tower via pipes, light aromatic hydrocarbon products are directly extracted out from the side lines of the extract-oil cutting tower via pipes, heavy aromatic hydrocarbon products are directly extracted out from the bottom of the extract-oil cutting tower via pipes, the top of the recovery tower is connected respectively with the bottom of the extraction unit and the bottom of the return tower, and the bottom of the recovery tower is connected with the top of the extraction unit via pipes. The hydrogenation unit is only applied to raffinate oil and extract oil with special requirements, so that the scale is small and the cost is low. Moreover, the diversification of raw materials processed by the system is obvious. Not only can straight-run diesel oil can be processed, but also the catalyzed diesel oil and the coking diesel oil can be processed. In addition, the invention separates aromatic hydrocarbon from diesel oil, therefore the cetane number of the diesel oil is improved greatly.
Description
Technical field
The present invention relates to a kind of preparation system and method thereof of diesel oil, particularly a kind of system of catalyzing hydrocarbon for recombinant production of high-quality diesel oil and method thereof.
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; From the generation oil of these explained hereafter, be referred to as catalytic hydrocarbon, gained catalytic hydrocarbon is through processing treatment, be generally Cutting Tap fractionation, can fractionate out the products such as net gas, liquefied gas tank, diesel oil, diesel oil, heavy oil, wherein diesel oil, the more than 70% of diesel oil total supply on diesel oil, diesel oil occuping market.
More and more stricter along with environmental requirement, the specification of petroleum products (fuel) also becomes more and more stricter.Take diesel oil as example, and the state such as the new diesel oil regulation Yi U.S., Europe, Japan implemented in succession in recent years, 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 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 producing is too low, cannot meet market demands.The principal element that affects diesel product quality is 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 at present catalytic diesel oil cetane value 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 subject to hydrogen resource limit.
There is following point in above-mentioned measure: the restriction that 1. construction investment is huge, process cost is high, scale is subject to raw material exists the irrational utilization of resource simultaneously; 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, adjust remaining little, also can cause the sulphur content in 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%.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 in China's diesel product are very large, catalytic cracking diesel oil occupies very high ratio, and this situation is by long-term existence.Therefore, the diesel quality upgrading sulphur that falls to be solved is urgently to be resolved hurrily with the problem that improves cetane value.
Therefore, provide a kind of low cost, less energy-consumption, low hydrogen consumption, the pollution-free treatment system of preparing low sulfur content and the high blended diesel of cetane value and method thereof just to become this technical field and be badly in need of the technical barrier solving.
Summary of the invention
One of object of the present invention is to provide a kind of low cost, less energy-consumption, low hydrogen consumption, the pollution-free system of preparing low sulfur content and improving diesel cetane-number.
For achieving the above object, the present invention takes following technical scheme:
A system of 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 hydrogenation reaction system by pipeline; Described hydrogenation reaction system bottom 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 extraction plant and the bottom of described back scrubber respectively 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; The oily Cutting Tap of described extraction bottom is by the direct extraction heavy aromatics of pipeline product; 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.
A kind of optimal technical scheme: it is characterized in that: described hydrogenation reaction system bottom is connected with the Cutting Tap of raffinating oil by pipeline.
Another object of the present invention is to provide the preparation method of above-mentioned high-quality diesel.
Above-mentioned purpose of the present invention reaches by the following technical programs:
A method of preparing high-quality diesel, its step is as follows: add extraction plant to carry out extracting in straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas oil and/or residual oil and solvent, isolate and raffinate oil and extract oil out; Described raffinating oil enters by extraction plant top the water wash column of raffinating oil and washes separatedly, isolates that diesel oil is raffinated oil and washing water; Described diesel oil is raffinated oil and is entered and in hydrogenation reaction system, carried out hydrogenating desulfurization by pipeline; The diesel oil of described hydrogenation reaction system bottom extraction is as the direct extraction of blended diesel; Described extraction oil and solvent enter back scrubber by pipeline and return and wash, and top is isolated BTX aromatics and entered and extract oily water wash column out with the mixture that returns lotion, and the mixture that described extraction oil water wash column bottom is isolated solvent and returned lotion enters recovery tower; Described extraction profit is washed top of tower and is isolated BTX aromatics and enter and extract oily Cutting Tap out with the mixture that returns lotion, and described extraction profit is washed the isolated water of tower bottom and recycled after treatment; The oily Cutting Tap of described extraction top is isolated to be returned the isolated bottom and the back scrubber bottom that enter extraction plant after lotion mixes returned in lotion and recovery tower top and recycles; The isolated light aromatic hydrocarbons of the oily Cutting Tap side line of described extraction is as the direct extraction of product, and the isolated heavy aromatics in described extraction oil Cutting Tap bottom is as the direct extraction of product; Bottom and the back scrubber bottom of returning lotion and entering extraction plant by pipeline isolated at described recovery tower top, and the solvent of described recovery tower bottom extraction enters extraction plant top by pipeline and recycles.
A kind of optimal technical scheme, it is characterized in that: the hydrogenated diesel oil of described hydrogenation reaction system bottom extraction enters by pipeline the Cutting Tap of raffinating oil and processes, gained solar oil is by the direct extraction in Cutting Tap top of raffinating oil as product, and gained heavy gas oil passes through Cutting Tap bottom extraction directly as product.
An optimal technical scheme, is characterized in that: described extraction plant is extraction tower, and the solvent ratio of described extraction tower is 2～6; Temperature is 90～175 ℃; Pressure is 0.5～0.8MPa (absolutely); Described boiling range of raffinating oil is controlled at 160-398 ℃; The oily boiling range of described extraction is controlled at 160-441 ℃, and described extraction tower solvent for use is tetramethylene sulfone, N-Methyl pyrrolidone or dimethyl sulfoxide (DMSO).
An optimal technical scheme, is characterized in that: described extraction plant is extraction tower, and the solvent ratio of described extraction tower is 4; Temperature is 150 ℃; Tower top pressure is 0.65MPa (absolutely), and the solvent that described extraction tower adopts is tetramethylene sulfone.
An optimal technical scheme, is characterized in that: described in the raffinate oil temperature of water wash column be 60～100 ℃; Pressure is 0.4～0.7MPa (absolutely); The boiling range that described diesel oil is raffinated oil is controlled at 160-398 ℃.
An optimal technical scheme, is characterized in that: described in the raffinate oil temperature of water wash column be 80 ℃; The pressure of water wash column of raffinating oil is 0.55MPa (absolutely).
An optimal technical scheme, is characterized in that: the catalyzer in described hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and/or GHT-23; The volume space velocity of the hydrogenator in described hydrogenation reaction system is than being 1.5-3.5h
-1; Hydrogen/oil volume ratio is 300; Service temperature is 300～360 ℃, and working pressure is 2.0～4.0MPa (absolutely).
An optimal technical scheme, is characterized in that: the temperature of described back scrubber is 80～120 ℃; Pressure is 0.5～0.8MPa (absolutely); Return and wash than being 0.3～1.0 (to charging).
An optimal technical scheme, is characterized in that: the temperature of described back scrubber is 98 ℃; Pressure is 0.6MPa (absolutely); Return and wash than being 0.6.
An optimal technical scheme, is characterized in that: the temperature of the oily water wash column of described extraction is 60～100 ℃; Pressure is 0.5～0.7MPa (absolutely).
An optimal technical scheme, is characterized in that: the temperature of the oily water wash column of described extraction is 90 ℃; Pressure is 0.6MPa (absolutely).
An optimal technical scheme, is characterized in that: described in the raffinate oil tower top temperature of Cutting Tap be 180～200 ℃, column bottom temperature is 360～380 ℃; Working pressure is-0.06～-0.04MPa (absolutely); The boiling range of described diesel oil is controlled 160-365 ℃, and the boiling range of described solvent oil is controlled at 365-396 ℃.
An optimal technical scheme, is characterized in that: the tower top temperature of the oily Cutting Tap of described extraction is 110～140 ℃, and column bottom temperature is 370～390 ℃; Tower top pressure is 0.15～0.2MPa (absolutely), and tower bottom pressure is 0.18～0.25MPa (absolutely), and reflux ratio is 6～10, and the boiling range of described light aromatic hydrocarbons is controlled at 160～205 ℃; The boiling range of described heavy aromatics is controlled at 205～422 ℃.
An optimal technical scheme, is characterized in that: the tower top temperature in the oily Cutting Tap of described extraction is 120 ℃, and column bottom temperature is 380 ℃; Tower top pressure is 0.17MPa (absolutely), and tower bottom pressure is 0.21MPa (absolutely), and reflux ratio is 8.
An optimal technical scheme, is characterized in that: the tower top temperature of described recovery tower is 100～120 ℃, and column bottom temperature is 145～180 ℃; Tower top pressure is 0.12～0.20MPa (absolutely), and tower bottom pressure is 0.15～0.24MPa (absolutely).
An optimal technical scheme, is characterized in that: the tower top temperature of described recovery tower is 110 ℃, and column bottom temperature is 161 ℃; Tower top pressure is 0.15MPa (absolutely), and tower bottom pressure is 0.18MPa (absolutely).
An optimal technical scheme, is characterized in that: the whole hydrogenation catalyst GHT-21 in described hydrogenation reaction system, and GHT-22 and GHT-23 once pile up from top to bottom, and its physico-chemical property is as shown in the table respectively:
The physico-chemical property of GHT-21
| Index name | Unit | GHT-21 |
| Outward appearance | - | Grey trilobal cross |
| Specification | mm | Φ1.5-2.0 |
| Intensity | N/cm | 180 |
| Bulk density | g/ml | 0.75 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 10 |
| NiO | m％ | 2.1 |
| CoO | m％ | 0.16 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
The physico-chemical property of GHT-22
| Index name | Unit | GHT-22 |
| Outward appearance | _ | Grey trilobal cross |
| Specification | mm | Φ1.5-2.0 |
| Intensity | N/cm | 180 |
| Bulk density | g/ml | 0.73 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 15 |
| NiO | m％ | 1.7 |
| CoO | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
The physico-chemical property of GHT-23
| Index name | Unit | GHT-23 |
| Outward appearance | - | Cylindric |
| Specification | mm | Φ4.0-4.5 |
| Intensity | N/cm | 250 |
| Bulk density | g/ml | 0.80 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 5.5 |
| NiO | m％ | 1.0 |
| CoO | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
Straight-run diesel oil of the present invention, catalytic diesel oil and coker gas oil can be arbitrary proportions.
The cut point (boiling range) of light aromatic hydrocarbons of the present invention and heavy aromatics can be adjusted.
The present invention's back scrubber used, water wash column, recovery tower and Cutting Tap are conventional back scrubber, water wash column, recovery tower and Cutting Tap.Extraction plant used is that the patent No. is disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The present invention's hydrogenation reaction system used is existing hydrogenation system, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser, stabilizer tower etc.
Beneficial effect:
The low sulfur content of preparing of the present invention with the system of low olefin-content diesel oil and the advantage of method thereof is: compare with the hydrorefined mode of ordinary diesel oil, hydrogenation unit of the present invention only for raffinate oil or special requirement under extraction oil, small scale, cost is low; Meanwhile, the diversification of feedstock that the present invention processes, not only processes straight-run diesel oil, can also process catalytic diesel oil and and the mixture of coker gas oil; And the present invention separates aromatic hydrocarbons from diesel oil, greatly improved diesel-fuel cetane number, reduced condensation point of diesel oil; Finally, the present invention can in the situation that meeting condensation point of diesel oil and aromaticity content, partly or entirely be in harmonious proportion aromatic component to enter in diesel oil according to practical situation, increases production of diesel oil.
Below by the drawings and specific embodiments, the present invention will be further described, but and do not mean that limiting the scope of the invention.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of one of embodiment of the present invention;
Fig. 2 is the schematic flow sheet of another embodiment of the present invention.
Below by embodiment, the present invention will be further described, but and do not mean that limiting the scope of the invention.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the embodiment of the present invention, some utility appliance in figure do not mark as tank, pump, interchanger, condenser etc., but this is known to those of ordinary skills.
As shown in Figure 1, by boiling range, be 160-425 ℃, sulphur content is 5000ppm, density is 874.1kg/m3, aromaticity content is 29%, to be 43 straight-run diesel oil add extraction tower 1 to carry out extracting with solvent with the flow of 100 tons/hour with the mixture (feedstock property is in Table 1-1) of residual oil to cetane value together with the flow of 540 tons/hour, the temperature of extraction tower 1 is 175 ℃, pressure is 0.8MPa, solvent ratio is 6, and solvent for use is tetramethylene sulfone, and the boiling range that gained is raffinated oil is 160-398 ℃, sulphur content is 1333ppm, and density is 853.2kg/m
3, aromaticity content is 8.6%, cetane value is 51.7; It is 160-441 ℃ that gained is extracted oily boiling range out, and sulphur content is 16000ppm, and density is 943.4kg/m
3, aromaticity content is 90.2%, cetane value is 17.The gained top by extraction tower 1 with the flow of 75 tons/hour of raffinating oil enters the water wash column 2-1 middle part of raffinating oil, simultaneously, washing water enters with the flow of 6.6 tons/hour the water wash column 2-1 top of raffinating oil, the head temperature of water wash column 2-1 of raffinating oil is 60 ℃, top pressure is 0.4MPa, raffinating oil after gained washing mixed the hydrogen of 0.97 ton/hour with the flow of 75 tons/hour by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, through the washing water using, with the flow of 6.6 tons/hour, by the water wash column 2-1 bottom of raffinating oil, directly discharges.The temperature of reaction of the hydrogenator in described hydrogenation reaction system 3 is 320 ℃, and reaction pressure is 4.0MPa, and hydrogen-oil ratio is 300, and air speed is 3.5h-1, and gained hydrogenation is raffinated oil and with the flow of 75 tons/hour, entered the Cutting Tap 4-1 that raffinates oil and process; The boiling range that described hydrogenation is raffinated oil is 160-396 ℃, and sulphur content is 160ppm, and density is 850.1kg/m3, and aromaticity content is 8.60%, and cetane value is 51.8.The tower top temperature of the described Cutting Tap 4-1 that raffinates oil is 180 ℃, and column bottom temperature is 360 ℃, and pressure is-0.06MPa.The Cutting Tap 4-1 overhead extraction flow of raffinating oil be the diesel oil of 65.15 tons/hour directly as product, at the bottom of tower, extraction flow is that the solvent oil of 9.85 tons/hour is directly as product.
The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 565 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 81 tons/hour 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.The extraction oil of back scrubber 5 overhead extractions is entered and is extracted out oily water wash column 2-2 middle part by pipeline with the flow of the mixture that returns lotion with 41.2 tons/hour, meanwhile, washing water enters extraction oily water wash column 2-2 top with the flow of 8.2 tons/hour, 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 washing cuts by extracting oily water wash column 2-2 overhead extraction out and entering the oily Cutting Tap 4-2 of extraction by pipeline, through the washing water using, with the flow of 8.2 tons/hour, bottom the oily water wash column 2-2 of extraction, directly discharges.110 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 370 ℃, tower top pressure 0.15MPa, tower bottom pressure 0.18MPa, reflux ratio is 10.Flow be 16.2 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is usingd the flow of 3.64 tons/hour from the side line of the oily Cutting Tap 4-2 of described extraction and is in harmonious proportion the direct extraction of product as gasoline, and heavy aromatics is usingd the flow of 21.36 tons/hour as the direct extraction of product from the bottom of the oily Cutting Tap 4-2 of described extraction tower.At the bottom of described back scrubber 5 towers, the solvent of extraction and the mixture that returns lotion enter recovery tower 6,100 ℃ of the tower top temperatures of recovery tower 6,175 ℃ of column bottom temperatures, pressure on top surface 0.18MPa, tower bottom pressure 0.2MPa with the flow of 604.8 tons/hour.The lotion that returns of recovery tower 6 overhead extractions enters the bottom of back scrubber 5 bottoms and extraction tower 1 with the flow of 54.8 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 540 tons/hour.Products obtained therefrom character is in Table 2.
Embodiment 2
As shown in Figure 1, be the schematic flow sheet of the embodiment of the present invention, some utility appliance in figure do not mark as tank, pump, interchanger, condenser etc., but this is known to those of ordinary skills.
As shown in Figure 1, by boiling range, be 160-425 ℃, sulphur content is 2000ppm, density is 879.2kg/m
3aromaticity content is 50%, to be 32 straight-run diesel oil add extraction tower 1 to carry out extracting with solvent with the flow of 100 tons/hour with the mixture (feedstock property is in Table 1-2) of residual oil to cetane value together with the flow of 864 tons/hour, the temperature of extraction tower 1 is 150 ℃, and pressure is 0.65MPa, and solvent ratio is 5, solvent for use is N-Methyl pyrrolidone, the boiling range that gained is raffinated oil is 160-399 ℃, and sulphur content is 667ppm, and density is 855.6kg/m
3, aromaticity content is 22.53%, cetane value is 44; It is 160-439 ℃ that gained is extracted oily boiling range out, and sulphur content is 4000ppm, and density is 917.2kg/m
3, aromaticity content is 91.2%, cetane value is 14.The gained top by extraction tower 1 with the flow of 60 tons/hour of raffinating oil enters the water wash column 2-1 middle part of raffinating oil, simultaneously, washing water enters with the flow of 5.3 tons/hour the water wash column 2-1 top of raffinating oil, the service temperature of water wash column 2-1 of raffinating oil is 80 ℃, working pressure is 0.55MPa, raffinating oil after gained washing mixed the hydrogen of 0.31 ton/hour with the flow of 60 tons/hour by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, through the washing water using, with the flow of 5.3 tons/hour, by the water wash column bottom of raffinating oil, directly discharges.The temperature of reaction of the hydrogenator in 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, gained hydrogenation is raffinated oil and with the flow of 60 tons/hour, is entered the Cutting Tap 4-1 that raffinates oil and process; The tower top temperature of the described Cutting Tap 4-1 that raffinates oil is 190 ℃, and column bottom temperature is 370 ℃, and working pressure is-0.05MPa.The Cutting Tap 4-1 overhead extraction flow of raffinating oil be the diesel oil of 51.68 tons/hour directly as product, at the bottom of tower, extraction flow is that the solvent oil of 8.32 tons/hour is directly as product.
The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 904 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 130 tons/hour enters by back scrubber 5 bottoms, the service temperature of back scrubber 5 is 100 ℃, working pressure is 0.65MPa, returns and washes than 0.7.The extraction oil of back scrubber 5 overhead extractions is entered and is extracted out oily water wash column 2-2 middle part by pipeline with 72.5 tons/hour, the mixture that returns lotion, meanwhile, 13.1 tons/hour of washing waters enter 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 washing is entered and is extracted out oily Cutting Tap 4-2 by pipeline by extracting oily water wash column 2-2 tower top out, through 13.1 tons/hour of the washing waters that use by extracting the directly discharge of oily water wash column 2-2 bottom out.125 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 380 ℃, tower top pressure 0.18MPa, tower bottom pressure 0.21MPa, reflux ratio is 8.Flow be 32.5 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is usingd the flow of 6.45 tons/hour from the side line of the oily Cutting Tap 4-2 of described extraction and is in harmonious proportion the direct extraction of product as gasoline, and heavy aromatics is usingd the flow of 33.55 tons/hour as the direct extraction of product from the bottom of the oily Cutting Tap 4-2 of described extraction tower.At the bottom of back scrubber 5 towers, 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, pressure on top surface 0.15MPa, tower bottom pressure 0.17MPa with the flow of 961.5 tons/hour.The lotion that returns of recovery tower 6 overhead extractions enters the bottom of back scrubber 5 bottoms and extraction tower 1 with the flow of 97.5 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 864 tons/hour.
Products obtained therefrom character is in Table 3.
As shown in Figure 2, be the schematic flow sheet of the embodiment of the present invention, some utility appliance in figure do not mark as tank, pump, interchanger, condenser etc., but this is known to those of ordinary skills.
As shown in Figure 2, by boiling range, be 160-395 ℃, sulphur content is 4000ppm, density is 857.6kg/m
3aromaticity content is 38%, to be 38 straight-run diesel oil add extraction tower 1 to carry out extracting with solvent with the flow of 100 tons/hour with the mixture (feedstock property is in Table 1-3) of residual oil to cetane value together with the flow of 600 tons/hour, the temperature of extraction tower 1 is 90 ℃, and pressure is 0.5MPa, and solvent ratio is 2, solvent for use is dimethyl sulfoxide (DMSO), the boiling range that gained is raffinated oil is 160-365 ℃, and sulphur content is 1000ppm, and density is 846.2kg/m
3, aromaticity content is 14.32%, cetane value is 48.7; It is 160-420 ℃ that gained is extracted oily boiling range out, and sulphur content is 10667ppm, and density is 885.4kg/m
3, aromaticity content is 93.2%, cetane value is 17.The gained top by extraction tower 1 with the flow of 70 tons/hour of raffinating oil enters the water wash column 2-1 middle part of raffinating oil, simultaneously, washing water enters with the flow of 6.4 tons/hour the water wash column 2-1 top of raffinating oil, the service temperature of water wash column 2-1 of raffinating oil is 100 ℃, working pressure is 0.7MPa, raffinating oil after gained washing mixed the hydrogen of 0.5 ton/hour with the flow of 70 tons/hour by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, through the washing water using, with the flow of 6.4 tons/hour, by the water wash column bottom of raffinating oil, directly discharges.The temperature of reaction of the hydrogenator in 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, gained hydrogenation is raffinated oil and is usingd the flow of 70 tons/hour directly as product extraction.The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 630 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 90 tons/hour 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.The extraction oil of back scrubber 5 overhead extractions is entered and is extracted out oily water wash column 2-2 middle part by pipeline with 57 tons/hour, the mixture that returns lotion, meanwhile, 9.2 tons/hour of washing waters enter 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 after washing oil, by extracting oily water wash column 2-2 overhead extraction out, enters and extracts oily Cutting Tap 4-2 out, through 9.2 tons/hour of the washing waters that use by extracting the directly discharge of oily water wash column 2-2 bottom out.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 27 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is usingd the flow of 5.95 tons/hour from the side line of the oily Cutting Tap 4-2 of described extraction and is in harmonious proportion the direct extraction of product as gasoline, and heavy aromatics is usingd the flow of 24.05 tons/hour as the direct extraction of product from the bottom of the oily Cutting Tap 4-2 of described extraction tower.At the bottom of back scrubber 5 towers, 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, pressure on top surface 0.12MPa, tower bottom pressure 0.14MPa with the flow of 663 tons/hour.The lotion that returns of recovery tower 6 overhead extractions enters the bottom of back scrubber 5 bottoms and extraction tower 1 with the flow of 63 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 600 tons/hour.Products obtained therefrom character sees the following form 4.
Table 1 feedstock property
Table 1-1 embodiment 1 feedstock property
Table 1-2 embodiment 2 feedstock properties
Table 1-3 embodiment 3 feedstock properties
Table 2 embodiment 1 product property table
Table 2-1 solar oil product property table
Table 2-2 solvent oil product property table
The light aromatic hydrocarbon product of table 2-3 is mainly followed GB252-2000 standard, and specific nature is as follows:
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 4.00 | |
| Sulphur content | ppm | 4000 | GB/T380 |
Table 2-4 heavy aromatics product property table:
GB11132-2002 method test for aromaticity content in diesel oil; 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 GBT/6536.
Table 3 embodiment 2 product property tables
Table 3-1 solar oil product property table
Table 3-2 solvent oil product property table
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 8.32 | |
| Sulphur content | ppm | 568.43 | GB/T261 |
| Aromaticity content | m％ | 39.68 | GB/T0118 |
| Cetane value | 39.2 | GB/T0174 |
The light aromatic hydrocarbon product of table 3-3 is mainly followed GB252-2000 standard, and specific nature is as follows:
Table 3-4 heavy aromatics product property table:
GB11132-2002 method test for aromaticity content in diesel oil; 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 4 embodiment 3 product property tables
Table 4-1 diesel product property list
The light aromatic hydrocarbon product of table 4-2 is mainly followed GB252-2000 standard, and specific nature is as follows:
Table 4-3 heavy aromatics product property table:
GB11132-2002 method test for aromaticity content in diesel oil; 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 (9)
1. a system of 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 hydrogenation reaction system by pipeline; Described hydrogenation reaction system bottom 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 extraction plant and the bottom of described back scrubber respectively 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; The oily Cutting Tap of described extraction bottom is by the direct extraction heavy aromatics of pipeline product; 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.
2. the system of preparing high-quality diesel according to claim 1, is characterized in that: described hydrogenation reaction system bottom is connected with the Cutting Tap of raffinating oil by pipeline.
3. a method of preparing high-quality diesel, its step is as follows: add extraction plant to carry out extracting in straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas oil and/or residual oil and solvent, isolate and raffinate oil and extract oil out; Described raffinating oil enters by extraction plant top the water wash column of raffinating oil and washes separatedly, isolates that diesel oil is raffinated oil and washing water; Described diesel oil is raffinated oil and is entered and in hydrogenation reaction system, carried out hydrogenating desulfurization by pipeline; The diesel oil of described hydrogenation reaction system bottom extraction is as the direct extraction of blended diesel; Described extraction oil and solvent enter back scrubber by pipeline and return and wash, and top is isolated BTX aromatics and entered and extract oily water wash column out with the mixture that returns lotion, and the mixture that described back scrubber bottom is isolated solvent and returned lotion enters recovery tower; Described extraction profit is washed top of tower and is isolated BTX aromatics and enter and extract oily Cutting Tap out with the mixture that returns lotion, and described extraction profit is washed the isolated water of tower bottom and recycled after treatment; Bottom and back scrubber bottom that the oily Cutting Tap of described extraction top is isolated enters extraction plant by pipeline after returning that lotion and recovery tower top are isolated and returning lotion and mix recycle; The isolated light aromatic hydrocarbons of the oily Cutting Tap side line of described extraction is as the direct extraction of product, and the isolated heavy aromatics in described extraction oil Cutting Tap bottom is as the direct extraction of product; The isolated lotion that returns in described recovery tower top enters bottom and the back scrubber bottom of extraction plant by pipeline, the solvent of described recovery tower bottom extraction enters extraction plant top by pipeline and recycles.
4. the method for preparing high-quality diesel according to claim 3, it is characterized in that: the hydrogenated diesel oil of described hydrogenation reaction system bottom extraction enters by pipeline the Cutting Tap of raffinating oil and processes, gained solar oil is by the direct extraction in Cutting Tap top of raffinating oil as product, and gained heavy gas oil passes through Cutting Tap bottom extraction directly as product.
5. the method for preparing high-quality diesel according to claim 3, is characterized in that: described extraction plant is extraction tower, and the solvent ratio of described extraction tower is 2 ~ 6; Temperature is 90 ~ 175 ℃; Pressure is absolute pressure 0.5 ~ 0.8MPa; Described boiling range of raffinating oil is controlled at 160-398 ℃; The oily boiling range of described extraction is controlled at 160-441 ℃, and described extraction tower solvent for use is tetramethylene sulfone, N-Methyl pyrrolidone or dimethyl sulfoxide (DMSO).
6. the method for preparing high-quality diesel according to claim 3, is characterized in that: described in the raffinate oil temperature of water wash column be 60 ~ 100 ℃; Pressure is absolute pressure 0.4 ~ 0.7MPa; The boiling range that described diesel oil is raffinated oil is controlled at 160-398 ℃.
7. the method for preparing high-quality diesel according to claim 3, is characterized in that: the catalyzer in described hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and/or GHT-23; The volume space velocity of the hydrogenator in described hydrogenation reaction system is than being 1.5-3.5h
-1; Hydrogen/oil volume ratio is 300; Service temperature is 300 ~ 360 ℃, and working pressure is absolute pressure 2.0 ~ 4.0MPa.
8. the method for preparing high-quality diesel according to claim 3, is characterized in that: the temperature of described back scrubber is 80 ~ 120 ℃; Pressure is absolute pressure 0.5 ~ 0.8MPa; Return and wash than being 0.3 ~ 1.0; The temperature of the oily water wash column of described extraction is 60 ~ 100 ℃; Pressure is absolute pressure 0.5 ~ 0.7MPa; The tower top temperature of the described Cutting Tap of raffinating oil is 180 ~ 200 ℃, and column bottom temperature is 360 ~ 380 ℃; Working pressure is absolute pressure-0.06 ~-0.04MPa; The boiling range of described diesel oil is controlled 160-365 ℃, and the boiling range of described solvent oil is controlled at 365-396 ℃; The tower top temperature of the oily Cutting Tap of described extraction is 110 ~ 140 ℃, and column bottom temperature is 370 ~ 390 ℃; Tower top pressure is absolute pressure 0.15 ~ 0.2MPa, and tower bottom pressure is absolute pressure 0.18 ~ 0.25MPa, and reflux ratio is 6 ~ 10, and the boiling range of described light aromatic hydrocarbons is controlled at 160 ~ 205 ℃; The boiling range of described heavy aromatics is controlled at 205 ~ 422 ℃; The tower top temperature of described recovery tower is 100 ~ 120 ℃, and column bottom temperature is 145 ~ 180 ℃; Tower top pressure is absolute pressure 0.12 ~ 0.20MPa, and tower bottom pressure is absolute pressure 0.15 ~ 0.24MPa.
9. the method for preparing high-quality diesel according to claim 3, is characterized in that: the whole hydrogenation catalyst GHT-21 in described hydrogenation reaction system, and GHT-22 and GHT-23 pile up from top to bottom successively, and its physico-chemical property is as shown in the table respectively:
The physico-chemical property of GHT-21
The physico-chemical property of GHT-22
The physico-chemical property of GHT-23
。
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