CN101921623A - Method with tow double hydrogenation units for preparing high-quality diesel - Google Patents
Method with tow double hydrogenation units for preparing high-quality diesel Download PDFInfo
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Abstract
The invention relates to a method with double hydrogenation units for preparing high-quality diesel, which comprises the steps of: charging a raw material into an extraction plant to separate out raffinate oil and extract oil; enabling the rafinate oil to enter a raffinate oil bath tower to separate out diesel raffinate oil; processing the diesel raffinate oil in a raffinate oil hydrogenation system to extract diesel used as a diesel blending component; enabling the extract oil to enter a backwashing tower; enabling separated mixed aromatics to enter an extract oil bath tower and a cutting tower; enabling separated light aromatics to enter a light aromatic hydrogenation system; and extracting the hydrogenated aromatics together with the diesel in an blending way. Compared with a common diesel hydrofining method, the method of the invention only aims at the raffinate oil or specific extract oil; the method of the invention can treat diverse raw materials, can separate aromatics from the diesel to improve the cetane number of the diesel and reduce the condensation point; and furthermore, under the condition of meeting the condensation point and aromatics content requirements, the method of the invention blends part of or all aromatic components into the diesel, thereby improving the yield of the diesel.
Description
Technical field
The present invention relates to a kind of preparation method of diesel oil, particularly a kind of system and method thereof that has 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 and method thereof just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
One of purpose of the present invention 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 present invention takes 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 links to each other with light aromatic hydrogenation reactive system by pipeline, and the oily Cutting Tap of described extraction bottom is by the direct extraction heavy aromatics of pipeline product; Described light aromatic hydrogenation reactive 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.
Another object of the present invention provides the preparation method of above-mentioned high-quality diesel.
Above-mentioned purpose of the present invention reaches by the following technical programs:
A kind of method for preparing high-quality diesel, its step is as follows: straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas oil and solvent are added extraction plant carry out extracting, isolate and raffinate oil and extract oil out; Described raffinating oil enters the water wash column of raffinating oil by the extraction plant top and washes separation, isolates diesel oil and raffinates oil and wash water; Described diesel oil is raffinated oil and is entered the hydrogenation reaction system of raffinating oil by pipeline and carry out hydrogenating desulfurization; The diesel oil of described hydrogenation reaction system bottom extraction is as the direct extraction of diesel oil blending component; Described extraction oil and solvent enter back scrubber by pipeline and return and wash, and the isolated BTX aromatics in top enters with the mixture that returns lotion and extracts oily water wash column out, and isolated solvent in bottom and the mixture that returns lotion enter recovery tower; Described extraction profit is washed the isolated BTX aromatics of top of tower and is entered the oily Cutting Tap of extraction 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 lotion that returns in lotion and recovery tower top and mixes the back and recycle by bottom and the back scrubber bottom that pipeline enters extraction plant; The isolated light aromatic hydrocarbons of the oily Cutting Tap side line of described extraction enters light aromatic hydrogenation system; The hydrogenation aromatic hydrocarbons of described light aromatic hydrogenation system bottom extraction and the diesel oil mediation extraction of the described hydrogenation reaction system bottom extraction of raffinating oil; The isolated heavy aromatics in described extraction oily Cutting Tap bottom is as the direct extraction of product; Described recovery tower top is isolated and is returned lotion and enter the bottom and the back scrubber bottom of extraction plant by pipeline, and the solvent of described recovery tower bottom extraction enters extraction plant top by pipeline and recycles.
A kind of optimal technical scheme is characterized in that: described extraction plant is an extraction tower, and the solvent ratio of described extraction tower is 2～6; Temperature is 90～175 ℃; Pressure is 0.5～0.8MPa (cutting off); Described boiling range of raffinating oil is controlled at 160～345 ℃; The described boiling range of extracting oil out is controlled at 160～392 ℃, and described extraction tower solvent for use is tetramethylene sulfone, N-Methyl pyrrolidone or dimethyl sulfoxide (DMSO).
A kind of optimal technical scheme is characterized in that: described extraction plant is an extraction tower, and the solvent ratio of described extraction tower is 3; Temperature is 130 ℃; Tower top pressure is 0.65MPa (cutting off), and the solvent that described extraction tower adopts is a dimethyl sulfoxide (DMSO).
A kind of optimal technical scheme is characterized in that: the service temperature of the described water wash column of raffinating oil is 60～100 ℃; Working pressure is 0.4～0.7MPa (cutting off); The boiling range that described diesel oil is raffinated oil is controlled at 160-345 ℃.
A kind of optimal technical scheme is characterized in that: the service temperature of the described water wash column of raffinating oil is 80 ℃; Working pressure is 0.55MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the catalyzer in the described hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity ratio of the hydrogenator of described hydrogenation reaction system is 1.5～3.5h
-1Hydrogen/oil volume ratio is 300; Service temperature is 300～360 ℃, and working pressure is 2.0～4.0MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the service temperature of described back scrubber is 80～120 ℃; Working pressure is 0.5～0.8MPa (cutting off); Return and wash than being 0.3～1.0.
A kind of optimal technical scheme is characterized in that: the service temperature of described back scrubber is 98 ℃; Working pressure is 0.6MPa (cutting off); Return and wash than being 0.6 (to charging).
A kind of optimal technical scheme is characterized in that: the service temperature of the oily water wash column of described extraction is 60～100 ℃; Working pressure is 0.5～0.7MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the service temperature of the oily water wash column of described extraction is 90 ℃; Working pressure is 0.6MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the tower top temperature in 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 (cutting off), and tower bottom pressure is 0.18～0.25MPa (cutting off), and reflux ratio is 6～10, is controlled at 160-205 ℃ at the boiling range of described light aromatic hydrocarbons; The boiling range of described heavy aromatics is controlled at 205-392 ℃.
A kind of 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 (cutting off), and tower bottom pressure is 0.21MPa (cutting off), and reflux ratio is 8, and the boiling range of described light aromatic hydrocarbons is controlled at 160-205 ℃; The boiling range of described heavy aromatics is controlled at 205-392 ℃.
A kind of optimal technical scheme is characterized in that: the catalyzer in the described light aromatic hydrogenation reactive system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity ratio of the hydrogenator in the described light aromatic hydrogenation reactive system is 2.0～5.0h
-1Hydrogen/oil volume ratio is 300; Service temperature is 160～215 ℃, and working pressure is 1.0～3.0MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the catalyzer in the described heavy aromatics hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator in the described heavy aromatics hydrogenation reaction system is than being 2.0h-1; Hydrogen/oil volume ratio is 300; Service temperature is 330 ℃, and working pressure is 6.0MPa (cutting off).
A kind of 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 (cutting off), and tower bottom pressure is 0.15～0.24MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the tower top temperature of described recovery tower is 105 ℃, and column bottom temperature is 149 ℃; Tower top pressure is 0.13MPa (cutting off), and tower bottom pressure is 0.16MPa (cutting off).
A kind of optimal technical scheme is characterized in that: the whole hydrogenation catalyst GHT-21 in the described hydrogenation reaction system, 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
| Index name | Unit | GHT-21 |
| Outward appearance | - | The 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 | - | The 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 used back scrubber of the present invention, 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 present invention is existing hydrogenation system, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser, stabilizer tower etc.
Beneficial effect:
The advantage for preparing the low sulfur content and the method for low olefin-content diesel oil of the present invention is: compare with the hydrorefined mode of ordinary diesel oil, hydrogenation unit of the present invention 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 present invention handles, can also handle catalytic diesel oil and and the mixture of coker gas oil; And the present invention separates aromatic hydrocarbons from diesel oil, has improved diesel-fuel cetane number greatly, has reduced condensation point of diesel oil; At last, the present invention 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.
The present invention will be further described below by the drawings and specific embodiments, but and do not mean that limiting the scope of the invention.
Description of drawings
Fig. 1 is the schematic flow sheet of one of embodiment of the invention.
The present invention will be further described below by embodiment, 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 invention, 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 mixes 0.42 ton/hour hydrogen from the side line of the oily Cutting Tap 4 of described extraction with 2.96 tons/hour flow and enters light aromatic hydrogenation reactive system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described light aromatic hydrogenation reactive system 3-2 is 160 ℃, reaction pressure is 1.0MPa, hydrogen-oil ratio is 300, and air speed is 2.0h
-1, the light aromatic hydrocarbons of gained hydrogenation is raffinated oil with 2.96 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.Heavy aromatics from the bottom of oily Cutting Tap 4 towers of described extraction with 12.04 tons/hour flow as the direct extraction of product.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 embodiment of the invention, 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 mixes 0.57 ton/hour hydrogen from the side line of the oily Cutting Tap 4 of described extraction with 10.15 tons/hour flow and enters light aromatic hydrogenation reactive system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described light aromatic hydrogenation reactive system 3-2 is 215 ℃, reaction pressure is 3.0MPa, hydrogen-oil ratio is 300, air speed is 5.0h-1, and the light aromatic hydrocarbons of gained hydrogenation 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.Heavy aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 40.85 tons/hour flow as the direct extraction of product.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 1, be the schematic flow sheet of the embodiment of the invention, 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 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 mixes 0.5 ton/hour hydrogen from the side line of the oily Cutting Tap 4 of described extraction with 5.04 tons/hour flow and enters light aromatic hydrogenation reactive system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator among the described light aromatic hydrogenation reactive system 3-2 is 185 ℃, reaction pressure is 2.0MPa, hydrogen-oil ratio is 300, and air speed is 3.5h
-1, the light aromatic hydrocarbons of gained hydrogenation is in harmonious proportion with 5.04 tons/hour flow extraction and with the diesel oil of the described hydrogenation reaction system 3-1 extraction of raffinating oil; Heavy aromatics from the bottom of oily Cutting Tap 4 towers of described extraction with 20.96 tons/hour flow as the direct extraction of 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 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
Table 1-2 blended diesel product property table
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
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
Table 3-3 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.
Claims (7)
1. method for preparing high-quality diesel, its step is as follows: straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas oil and solvent are added extraction plant carry out extracting, isolate and raffinate oil and extract oil out; Described raffinating oil enters the water wash column of raffinating oil by the extraction plant top and washes separation, isolates diesel oil and raffinates oil and wash water; Described diesel oil is raffinated oil and is entered the hydrogenation reaction system of raffinating oil by pipeline and carry out hydrogenating desulfurization; The diesel oil of described hydrogenation reaction system bottom extraction is as the direct extraction of diesel oil blending component; Described extraction oil and solvent enter back scrubber by pipeline and return and wash, and the isolated BTX aromatics in top enters with the mixture that returns lotion and extracts oily water wash column out, and isolated solvent in bottom and the mixture that returns lotion enter recovery tower; Described extraction profit is washed the isolated BTX aromatics of top of tower and is entered the oily Cutting Tap of extraction 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 lotion that returns in lotion and recovery tower top and mixes the back and recycle by bottom and the back scrubber bottom that pipeline enters extraction plant; The isolated light aromatic hydrocarbons of the oily Cutting Tap side line of described extraction enters light aromatic hydrogenation system; The hydrogenation aromatic hydrocarbons of described light aromatic hydrogenation system bottom extraction and the diesel oil mediation extraction of the described hydrogenation reaction system bottom extraction of raffinating oil; The isolated heavy aromatics in described extraction oily Cutting Tap bottom is as the direct extraction of product; Described recovery tower top is isolated and is returned lotion and enter the bottom and the back scrubber bottom of extraction plant by pipeline, and the solvent of described recovery tower bottom extraction enters extraction plant top by pipeline and recycles.
2. the method for preparing high-quality diesel according to claim 1 is characterized in that: described extraction plant is an extraction tower, and the solvent ratio of described extraction tower is 2～6; Temperature is 90～175 ℃; Pressure is 0.5～0.8MPa (cutting off); Described boiling range of raffinating oil is controlled at 160～345 ℃; The described boiling range of extracting oil out is controlled at 160～392 ℃, and described extraction tower solvent for use is tetramethylene sulfone, N-Methyl pyrrolidone or dimethyl sulfoxide (DMSO).
3. the method for preparing high-quality diesel according to claim 1 is characterized in that: the service temperature of the described water wash column of raffinating oil is 60～100 ℃; Working pressure is 0.4～0.7MPa (cutting off); The boiling range that described diesel oil is raffinated oil is controlled at 160～345 ℃.
4. the method for preparing high-quality diesel according to claim 1 is characterized in that: the catalyzer in the described hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity ratio of the hydrogenator of described hydrogenation reaction system is 1.5～3.5h
-1Hydrogen/oil volume ratio is 300; Service temperature is 300～360 ℃, and working pressure is 2.0～4.0MPa (cutting off).
5. the method for preparing high-quality diesel according to claim 1 is characterized in that: the service temperature of described back scrubber is 80～120 ℃; Working pressure is 0.5～0.8MPa (cutting off); Return and wash than being 0.3～1.0; The service temperature of the oily water wash column of described extraction is 60～100 ℃; Working pressure is 0.5～0.7MPa (cutting off); Tower top temperature in 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 (cutting off), and tower bottom pressure is 0.18～0.25MPa (cutting off), and reflux ratio is 6～10, is controlled at 160～205 ℃ at the boiling range of described light aromatic hydrocarbons; The boiling range of described heavy aromatics is controlled at 205-392 ℃; 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 (cutting off), and tower bottom pressure is 0.15～0.24MPa (cutting off).
6. the method for preparing high-quality diesel according to claim 1 is characterized in that: the catalyzer in the described light aromatic hydrogenation reactive system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity ratio of the hydrogenator in the described light aromatic hydrogenation reactive system is 2.0～5.0h
-1Hydrogen/oil volume ratio is 300; Service temperature is 160～215 ℃, and working pressure is 1.0～3.0MPa (cutting off).
7. the method for preparing high-quality diesel according to claim 1, it is characterized in that: described hydrogenation reaction system, whole hydrogenation catalyst GHT-21 in described light aromatic hydrogenation reactive system and the described heavy aromatics hydrogenation reaction system, 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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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87107146A (en) * | 1987-10-30 | 1988-04-13 | 中国石油化工总公司 | Combining technique of catalytic cracking and extraction of heavy oil aroma |
| CN1769392A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Inferior diesel oil quality change method |
| US20060108263A1 (en) * | 2004-11-23 | 2006-05-25 | Chinese Petroleum Corporation | Oxidative desulfurization and denitrogenation of petroleum oils |
-
2010
- 2010-09-07 CN CN 201010273767 patent/CN101921623B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87107146A (en) * | 1987-10-30 | 1988-04-13 | 中国石油化工总公司 | Combining technique of catalytic cracking and extraction of heavy oil aroma |
| CN1769392A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Inferior diesel oil quality change method |
| US20060108263A1 (en) * | 2004-11-23 | 2006-05-25 | Chinese Petroleum Corporation | Oxidative desulfurization and denitrogenation of petroleum oils |
Non-Patent Citations (2)
| Title |
|---|
| 《河南石油》 20040630 何宗奇 "柴油精制装置的开发与应用" 第100-101页 1-7 第18卷, * |
| 何宗奇: ""柴油精制装置的开发与应用"", 《河南石油》 * |
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