CN102021022B - System for preparing high-quality diesel with dual-hydrogenation unit and method thereof - Google Patents
System for preparing high-quality diesel with dual-hydrogenation unit and method thereof Download PDFInfo
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- CN102021022B CN102021022B CN200910092956.8A CN200910092956A CN102021022B CN 102021022 B CN102021022 B CN 102021022B CN 200910092956 A CN200910092956 A CN 200910092956A CN 102021022 B CN102021022 B CN 102021022B
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000000605 extraction Methods 0.000 claims abstract description 175
- 238000011084 recovery Methods 0.000 claims abstract description 40
- 238000005406 washing Methods 0.000 claims abstract description 24
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 20
- 239000000284 extract Substances 0.000 claims abstract description 19
- 239000002283 diesel fuel Substances 0.000 claims description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 60
- 239000002904 solvent Substances 0.000 claims description 33
- 239000006210 lotion Substances 0.000 claims description 30
- 238000009835 boiling Methods 0.000 claims description 26
- 239000000203 mixture Substances 0.000 claims description 21
- 239000000126 substance Substances 0.000 claims description 16
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 12
- 239000011148 porous material Substances 0.000 claims description 12
- 239000003054 catalyst Substances 0.000 claims description 10
- 230000003197 catalytic effect Effects 0.000 claims description 10
- 238000006477 desulfuration reaction Methods 0.000 claims description 8
- 230000023556 desulfurization Effects 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 6
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical group O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 3
- 238000005520 cutting process Methods 0.000 abstract description 5
- 239000003921 oil Substances 0.000 description 75
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 18
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 17
- 239000005864 Sulphur Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000008569 process Effects 0.000 description 7
- 239000003643 water by type Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 3
- 238000004523 catalytic cracking Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
Abstract
The invention relates to a system for preparing high-quality diesel with a dual-hydrogenation unit and a method thereof. The system comprises an extraction device and is characterized in that: the top of the extraction device is connected with a raffinate washing tower by a pipeline; the top of the raffinate washing tower is connected with a raffinate hydrogenation reaction system by a pipeline; products are extracted from the bottom of the raffinate hydrogenation reaction system through a pipeline directly; the bottom of the extraction device is connected with a backwash tower by a pipeline; the top of the backwash tower is connected with an extract oil washing tower by a pipeline; the bottom of the backwash tower is connected with a recovery tower by a pipeline; the top of the extract oil washing tower is connected with an extract oil cutting tower by a pipeline; the top of the extract oil cutting tower is connected with the recovery tower and the extraction device and the lower part of the backwash tower by pipelines respectively; light aromatic hydrocarbons are extracted from a lateral line of the extract oil cutting tower through the pipeline directly; the bottom of the extract oil cutting tower is connected with a heavy aromatic hydrocarbon hydrogenation reaction system by a pipeline; products extracted from the bottom of the heavy aromatic hydrocarbon hydrogenation reaction system through pipelines are blended with the products extracted from the bottom of the raffinate hydrogenation reaction system; the top of the recovery tower is connected with the lower part of the extraction device and the lower part of the backwash tower by the pipeline respectively; and the bottom of the recovery tower is connected with the upper part of the extraction device by the pipeline. Compared with the ordinary diesel hydrorefining mode, the hydrogenation unit is used only for raffinate oil or extract oil meeting special requirements, and is small in scale and low in cost.
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 tow double hydrogenation units for preparing high-quality diesel 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 separation column 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 GB252-2000 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 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), 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), 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, 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 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 extraction plant and described back scrubber with recovery tower by pipeline; The oily Cutting Tap of described extraction bottom is connected with heavy aromatics hydrogenation reaction system by pipeline, and the oily Cutting Tap side line of described extraction is by the light aromatic hydrocarbon product of the direct extraction of pipeline; The product of described heavy aromatics hydrogenation reaction system bottom by pipeline extraction with described in the raffinate oil product of hydrogenation reaction system bottom extraction be in harmonious proportion; 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 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 straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas 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 by pipeline, is entered the hydrogenation reaction system of raffinating oil 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 and extracts oily water wash column out with the mixture that returns lotion, and the 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 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 extraction of the oily Cutting Tap side line of described extraction; The isolated heavy aromatics in described extraction oily Cutting Tap bottom enters heavy aromatics hydrogenation system, the diesel oil mediation extraction of the hydrogenation aromatic hydrocarbons of described heavy aromatics hydrogenation system bottom extraction and the bottom extraction of described hydrogenation reaction system; 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.
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 that 0.5～0.8MPa(is exhausted); Described boiling range of raffinating oil is controlled at 160～345 ℃; The oily boiling range of described extraction is controlled at 160～392 ℃, 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 3; Temperature is 130 ℃; Tower top pressure is that 0.65MPa(is exhausted), the solvent that described extraction tower adopts is dimethyl sulfoxide (DMSO).
An optimal technical scheme, is characterized in that: described in the raffinate oil service temperature of water wash column be 60～100 ℃; Working pressure is that 0.4～0.7MPa(is exhausted); The boiling range that described diesel oil is raffinated oil is controlled at 160-345 ℃.
An optimal technical scheme, is characterized in that: described in the raffinate oil service temperature of water wash column be 80 ℃; Working pressure is that 0.55MPa(is exhausted).
An optimal technical scheme, is characterized in that: the catalyzer in described hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator of described hydrogenation reaction system is 1.5～3.5h
-1; Hydrogen/oil volume ratio is 300; Service temperature is 300～360 ℃, and working pressure is that 2.0～4.0MPa(is exhausted).
An optimal technical scheme, is characterized in that: the service temperature of described back scrubber is 80～120 ℃; Working pressure is that 0.5～0.8MPa(is exhausted); Return and wash than being 0.3～1.0.
An optimal technical scheme, is characterized in that: the service temperature of described back scrubber is 98 ℃; Working pressure is that 0.6MPa(is exhausted); Return wash than for 0.6(to charging).
An 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 that 0.5～0.7MPa(is exhausted).
An optimal technical scheme, is characterized in that: the service temperature of the oily water wash column of described extraction is 90 ℃; Working pressure is that 0.6MPa(is exhausted).
An 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 that 0.15～0.2MPa(is exhausted), tower bottom pressure is that 0.18～0.25MPa(is exhausted), reflux ratio is 6～10, at 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 ℃.
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 that 0.17MPa(is exhausted), tower bottom pressure is that 0.21MPa(is exhausted), reflux ratio is 8, 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 ℃.
An optimal technical scheme, is characterized in that: the catalyzer in described light aromatic hydrogenation reactive system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator in described light aromatic hydrogenation reactive system is 2.0～5.0h-1; Hydrogen/oil volume ratio is 300; Service temperature is 160～215 ℃, and working pressure is that 1.0～3.0MPa(is exhausted).
An optimal technical scheme, is characterized in that: the catalyzer in described heavy aromatics hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator in described heavy aromatics hydrogenation reaction system is 2.0h-1; Hydrogen/oil volume ratio is 300; Service temperature is 330 ℃, and working pressure is that 6.0MPa(is exhausted).
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 that 0.12～0.20MPa(is exhausted), tower bottom pressure is that 0.15～0.24MPa(is exhausted).
An 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 that 0.13MPa(is exhausted), tower bottom pressure is that 0.16MPa(is exhausted).
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 the 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, 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 160-365 ℃, sulphur content is 2900ppm, density is 816.3kg/m
3aromaticity content is 18%, to be 50.9 straight-run diesel oil (feedstock property is in Table 1-1) add extraction tower 1 to carry out extracting with solvent with the flow of 100 tons/hour to cetane value together with the flow of 300 tons/hour, the temperature of extraction tower 1 is 175 ℃, and pressure is 0.8MPa, and solvent ratio is 6, solvent for use is 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; It is 160-388 ℃ that gained is extracted oily boiling range out, and sulphur content is 17013.3ppm, and density is 884.1kg/m
3, aromaticity content is 91.5%, cetane value is 19.3.The gained top by extraction tower 1 with the flow of 85 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 7.8 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 60 ℃, working pressure is 0.5MPa, raffinating oil after gained washing mixed the hydrogen of 0.25 ton/hour with the flow of 85 tons/hour by water wash column 2-1 top and entered the hydrogenation reaction system 3-1 that raffinates oil and carry out hydrogenating desulfurization, through the washing water using, with the flow of 7.8 tons/hour, by the water wash column bottom of raffinating oil, directly discharge.The temperature of reaction of the described hydrogenator in hydrogenation reaction system 3-1 of raffinating oil 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 85 tons/hour and be in harmonious proportion the direct extraction of product as diesel oil.The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 315 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 45 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 24 tons/hour, the mixture that returns lotion, meanwhile, 4.6 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 60 ℃, and working pressure is 0.5MPa.Extraction after washing oil, by extracting oily water wash column 2-2 overhead extraction out, enters and extracts oily Cutting Tap 4 out, through 4.6 tons/hour of the washing waters that use by extracting the directly discharge of oily water wash column 2-2 bottom out.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 with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is the direct extraction of flow product with 2.96 tons/hour from the side line of the oily Cutting Tap 4 of described extraction; Heavy aromatics mixes the hydrogen of 0.28 ton/hour from the bottom of oily Cutting Tap 4 towers of described extraction with the flow of 12.04 tons/hour and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator in described heavy aromatics hydrogenation reaction system 3-2 is 300 ℃, reaction pressure is 4.0MPa, hydrogen-oil ratio is 300, and air speed is 1.0h
-1, gained hydrogenation heavy aromatics is usingd the flow extraction of 12.04 tons/hour raffinate oil and mix as diesel oil blending component with described hydrogenation of raffinating oil hydrogenation reaction system 3-1 extraction.At the bottom of back scrubber 5 towers, 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, pressure on top surface 0.20MPa, tower bottom pressure 0.24MPa with the flow of 336 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 36 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 300 tons/hour.The character of products obtained therefrom is in Table 1-2,1-3.
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 160-365 ℃, sulphur content is 3700ppm, density is 866.8kg/m
3aromaticity content is 58%, to be 28.9 catalytic diesel oil (feedstock property is in Table 2-1) add extraction tower 1 to carry out extracting with solvent with the flow of 100 tons/hour to cetane value together with the flow of 1020 tons/hour, the temperature of extraction tower 1 is 150 ℃, and pressure is 0.65MPa, and solvent ratio is 4, solvent for use is 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; It is 160-386 ℃ that gained is extracted oily boiling range out, and sulphur content is 6384.3ppm, and density is 903.8kg/m
3, aromaticity content is 91.7%, cetane value is 15.3.The gained top by extraction tower 1 with the flow of 49 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 4.5 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 0.6MPa, raffinating oil after gained washing mixed the hydrogen of 0.36 ton/hour with the flow of 49 tons/hour by water wash column 2-1 top and entered the hydrogenation reaction system 3-1 that raffinates oil and carry out hydrogenating desulfurization, through the washing water using, with the flow of 4.5 tons/hour, by the water wash column bottom of raffinating oil, directly discharge.The temperature of reaction of the described hydrogenator in hydrogenation reaction system 3-1 of raffinating oil 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 is usingd the flow of 49 tons/hour and be in harmonious proportion the direct extraction of product as diesel oil.The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 1071 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 153 tons/hour 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.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 89.25 tons/hour, the mixture that returns lotion, meanwhile, 15.6 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 after washing oil, by extracting oily water wash column 2-2 overhead extraction out, enters and extracts oily Cutting Tap 4 out, through 15.6 tons/hour of the washing waters that use by extracting the directly discharge of oily water wash column 2-2 bottom out.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 with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is usingd the flow of 10.15 tons/hour as the direct extraction of product from the side line of the oily Cutting Tap 4 of described extraction; Heavy aromatics mixes the hydrogen of 2.29 tons/hour from the bottom of oily Cutting Tap 4 towers of described extraction with the flow of 40.85 tons/hour and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator in described heavy aromatics hydrogenation reaction system 3-2 is 330 ℃, reaction pressure is 5.0MPa, hydrogen-oil ratio is 300, and air speed is 1.5h
-1, gained hydrogenation heavy aromatics is in harmonious proportion with the flow extraction of 10.15 tons/hour and with the diesel oil of the described hydrogenation reaction system 3-1 extraction of raffinating oil.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 0.18MPa with the flow of 1134.75 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 114.75 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 1020 tons/hour.The character of products obtained therefrom is in Table 2-2,2-3.
Embodiment 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 160-365 ℃, 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 to carry out extracting with solvent with the flow of 100 tons/hour with the mixture (feedstock property is in Table 3-1) of coker gas oil to cetane value together with the flow of 520 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 160-339 ℃, and sulphur content is 535.1ppm, and density is 817.4kg/m
3, aromaticity content is 13.4%, cetane value is 49.1; It is 160-392 ℃ that gained is extracted oily boiling range out, and sulphur content is 11169.2ppm, and density is 892.1kg/m
3, aromaticity content is 91.1%, cetane value is 19.2.The gained top by extraction tower 1 with the flow of 74 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 6.8 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 0.30 ton/hour with the flow of 74 tons/hour by water wash column 2-1 top and entered hydrogenation reaction system 3-1 and carry out hydrogenating desulfurization, through the washing water using, with the flow of 6.8 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 3-1 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 74 tons/hour and be in harmonious proportion the direct extraction of product as diesel oil.The extraction oil obtaining from extraction tower 1 and the mixture of solvent enter back scrubber 5 with the flow of 546 tons/hour at the bottom of by extraction tower 1 tower, while flow is that the lotion that returns of 78 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 49.4 tons/hour, the mixture that returns lotion, meanwhile, 8.0 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 out, through 8.0 tons/hour of the washing waters that use by extracting the directly discharge of oily water wash column 2-2 bottom out.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 with returning after lotion mixes of recovery tower 6 top extraction; Light aromatic hydrocarbons is usingd the flow of 5.04 tons/hour as the direct extraction of product from the side line of the oily Cutting Tap 4 of described extraction; Heavy aromatics mixes the hydrogen of 0.89 ton/hour from the bottom of oily Cutting Tap 4 towers of described extraction with the flow of 20.96 tons/hour and enters heavy aromatics hydrogenation reaction system 3-2 and carry out hydrogenating desulfurization, the temperature of reaction of the hydrogenator in described heavy aromatics hydrogenation reaction system 3-2 is 300 ℃, reaction pressure is 6.0MPa, hydrogen-oil ratio is 300, and air speed is 2.0h
-1, gained hydrogenation heavy aromatics is in harmonious proportion with the flow extraction of 20.96 tons/hour and with the diesel oil of the described hydrogenation reaction system 3-1 extraction of raffinating oil.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 0.15MPa with the flow of 574.6 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 54.6 tons/hour, at the bottom of recovery tower 6 towers, the solvent of extraction enters extraction tower 1 top with the flow of 520 tons/hour.The character of products obtained therefrom is in 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
The light aromatic hydrocarbon product property list of table 1-3:
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 2 embodiment 2 raw materials and product property table
Table 2-1 feedstock property
Table 2-2 blended diesel product property table
The light aromatic hydrocarbon product property list of table 2-3:
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 3 embodiment 3 raw materials and product property table
Table 3-1 feedstock property
Table 3-2 blended diesel product property table
The light aromatic hydrocarbon product property list of table 3-3:
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 (8)
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 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 extraction plant and described back scrubber with recovery tower by pipeline; The oily Cutting Tap of described extraction bottom is connected with heavy aromatics hydrogenation reaction system by pipeline, and the oily Cutting Tap side line of described extraction is by the light aromatic hydrocarbon product of the direct extraction of pipeline; The product of described heavy aromatics hydrogenation reaction system bottom by pipeline extraction with described in the raffinate oil product of hydrogenation reaction system bottom extraction be in harmonious proportion; 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.
2. a method of preparing high-quality diesel, its step is as follows: add extraction plant to carry out extracting straight-run diesel oil and/or catalytic diesel oil and/or hydrogenation coker gas 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 by pipeline, is entered the hydrogenation reaction system of raffinating oil and carry out hydrogenating desulfurization; The diesel oil of the described hydrogenation reaction system bottom extraction of raffinating oil 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 and extracts oily water wash column out with the mixture that returns lotion, and the 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 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 extraction of the oily Cutting Tap side line of described extraction; The isolated heavy aromatics in the oily Cutting Tap of described extraction bottom enters heavy aromatics hydrogenation system, the hydrogenation aromatic hydrocarbons of described heavy aromatics hydrogenation system bottom extraction with described in the raffinate oil diesel oil of hydrogenation reaction system bottom extraction be in harmonious proportion extraction; 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.
3. the method for preparing high-quality diesel according to claim 2, 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 ~ 345 ℃; The oily boiling range of described extraction is controlled at 160 ~ 392 ℃, and described extraction tower solvent for use is tetramethylene sulfone, N-Methyl pyrrolidone or dimethyl sulfoxide (DMSO).
4. the method for preparing high-quality diesel according to claim 2 is characterized in that: described in the raffinate oil service temperature of water wash column be 60 ~ 100 ℃; Working pressure is absolute pressure 0.4 ~ 0.7MPa; The boiling range that described diesel oil is raffinated oil is controlled at 160-345 ℃.
5. the method for preparing high-quality diesel according to claim 2, is characterized in that: described in the catalyzer of raffinating oil in hydrogenation reaction system be hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator of the described hydrogenation reaction system of raffinating oil is 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, hydrogenation catalyst GHT-21, and the physico-chemical property of GHT-22 and GHT-23 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
。
6. the method for preparing high-quality diesel according to claim 2, is characterized in that: the service temperature of described back scrubber is 80 ~ 120 ℃; Working pressure is absolute pressure 0.5 ~ 0.8MPa; 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 absolute pressure 0.5 ~ 0.7MPa; 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 absolute pressure 0.15 ~ 0.2MPa, and tower bottom pressure is absolute pressure 0.18 ~ 0.25MPa, and reflux ratio is 6 ~ 10, at 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 ℃; 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.
7. the method for preparing high-quality diesel according to claim 2, is characterized in that: the catalyzer in described heavy aromatics hydrogenation reaction system is hydrogenation catalyst GHT-21, GHT-22 and GHT-23; The volume space velocity of the hydrogenator in described heavy aromatics hydrogenation reaction system is 1.0 h
-1~ 2.0h
-1; Hydrogen/oil volume ratio is 300; Service temperature is 300 ~ 330 ℃, and working pressure is absolute pressure 4.0 ~ 6.0MPa, hydrogenation catalyst GHT-21, and the physico-chemical property of GHT-22 and GHT-23 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
。
8. the method for preparing high-quality diesel according to claim 2, it is characterized in that: described in whole hydrogenation catalyst GHT-21 of raffinating oil in hydrogenation reaction system and described heavy aromatics hydrogenation reaction system, 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
The physico-chemical property of GHT-22
The physico-chemical property of GHT-23
。
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5527448A (en) * | 1993-04-23 | 1996-06-18 | Institut Francais Du Petrole | Process for obtaining a fuel through extraction and hydrotreatment of a hydrocarbon charge, and the gas oil obtained |
| 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 |
| CN1814708A (en) * | 2005-02-05 | 2006-08-09 | 中国石油化工股份有限公司 | Method for modifying poor-quality diesel-oil by cut fraction |
| CN201506772U (en) * | 2009-09-18 | 2010-06-16 | 北京金伟晖工程技术有限公司 | System of double hydrogenation device for preparing high-quality diesel oil |
-
2009
- 2009-09-18 CN CN200910092956.8A patent/CN102021022B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5527448A (en) * | 1993-04-23 | 1996-06-18 | Institut Francais Du Petrole | Process for obtaining a fuel through extraction and hydrotreatment of a hydrocarbon charge, and the gas oil obtained |
| 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 |
| CN1814708A (en) * | 2005-02-05 | 2006-08-09 | 中国石油化工股份有限公司 | Method for modifying poor-quality diesel-oil by cut fraction |
| CN201506772U (en) * | 2009-09-18 | 2010-06-16 | 北京金伟晖工程技术有限公司 | System of double hydrogenation device for preparing high-quality diesel oil |
Non-Patent Citations (3)
| Title |
|---|
| 李族光.芳烃抽提工艺发展的回顾.《石油炼制》.1986,(第8期),第16-21页. |
| 芳烃抽提工艺发展的回顾;李族光;《石油炼制》;19861231(第8期);第16-21页 * |
| 赵野,张文成等.清洁柴油的加氢技术进展.《工业催化》.2008,第16卷(第1期), * |
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