CN201506774U - System for preparing high quality diesel oil through limiting hydrogenation scale - Google Patents
System for preparing high quality diesel oil through limiting hydrogenation scale Download PDFInfo
- Publication number
- CN201506774U CN201506774U CN2009202228303U CN200920222830U CN201506774U CN 201506774 U CN201506774 U CN 201506774U CN 2009202228303 U CN2009202228303 U CN 2009202228303U CN 200920222830 U CN200920222830 U CN 200920222830U CN 201506774 U CN201506774 U CN 201506774U
- Authority
- CN
- China
- Prior art keywords
- oil
- extraction
- pipeline
- tower
- tons
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present utility model relates to a system for preparing high quality diesel oil through limiting hydrogenation scale. The system comprises an extraction apparatus and is characterized in that the top of the extraction apparatus is connected with a raffinate oil water scrubbing tower through a pipeline, the top of the raffinate oil water scrubbing tower is connected with a raffinate oil hydrogenation reaction system through a pipeline, the bottom of the hydrogenation reaction system is connected with a raffinate oil cutting tower through a pipeline, the bottom of the extraction apparatus is connected with a returning scrubbing tower through a pipeline, the top of the returning scrubbing tower is connected with an extract oil water scrubbing tower, the bottom of the returning scrubbing tower is connected with a reclaiming tower through a pipeline, and the top of the extract oil water scrubbing tower is connected with an extract oil cutting tower through a pipeline. The hydrogenation unit of the utility model only aiming at raffinate oil or extract oil under special requirements has a small scale and a low cost, according to the utility model, aromatic hydrocarbons can be separated from diesel oil, the cetane ratio of the diesel oil can be improved greatly, and the congealing point of the diesel oil can be reduced.
Description
Technical field
The utility model relates to a kind of preparation system of diesel oil, particularly a kind of system by restriction hydrogenation macro preparation 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 fractionated processing and treating method of separation column: a diesel quality that is this treatment process is produced has much room for improvement, and diesel-fuel cetane number is on the low side, and stability is undesirable; The 2nd, the needed hydrogenation scale of above-mentioned treatment process is bigger than normal, causes full factory hydrogen consumption too high; The 3rd, the diesel cetane-number of being produced is low excessively, can't satisfy market demands.The principal element that influences the diesel product quality is the sulphur content and the diesel-fuel cetane number of diesel oil.Diesel-fuel cetane number is the key problem of diesel quality, the major measure that increases the catalytic diesel oil cetane value at present is high-pressure hydrogenation and high-pressure hydrogenation combination technique, catalytic diesel oil cetane value after high-pressure hydrogenation and the processing of high-pressure hydrogenation combination technique has a more substantial increase, but the construction investment of this technology is huge, running cost is very high, be subjected to the hydrogen resource limit.
There is following point in above-mentioned measure: there is the irrational utilization of resource simultaneously in the restriction that 1. construction investment is huge, process cost is high, scale is subjected to raw material; 2. adopt new catalyst, can increase diesel-fuel cetane number, still, can cause increasing considerably of hydrogen consumption; 3. adjust diesel oil boiling range scope, increase the measure of diesel cetane-number, it is little to adjust remaining, also can cause the sulphur content in the diesel oil to increase.
Europe has come into effect new Europe VI diesel oil standard at present, wherein requires the sulphur content of diesel oil to be not more than 0.005% (wt), and aromaticity content is not more than 15%, and density is not more than 825kg/m
3, polycyclic aromatic hydrocarbons is not more than 2%.For the most refinery of China, equally also must require in the face of higher national IV diesel oil standard: sulphur content is not more than 0.005% (wt), and aromaticity content is not more than 15%.The diesel quality solution must be considered the transition from national III diesel oil standard to national IV diesel oil standard, and programme should be disposable according to national IV diesel oil standard programme preferably.
Because ratio and developed country's difference of each blend component are very big in China's diesel product, catalytic cracking diesel oil occupies very high ratio, and this situation is with long-term existence.Therefore, diesel quality upgrading problem of falling sulphur and raising cetane value to be solved needs to be resolved hurrily.
Therefore, provide the treatment system of the high blended diesel of a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content and cetane value just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides a kind of low cost, less energy-consumption, low hydrogen consumption, pollution-free preparation low sulfur content and improves the system of diesel cetane-number.
For achieving the above object, the utility model is taked following technical scheme:
A kind of system for preparing high-quality diesel comprises extraction plant; It is characterized in that: described extraction plant top is connected with the water wash column of raffinating oil by pipeline; The described water wash column top of raffinating oil is connected with the hydrogenation reaction system of raffinating oil by pipeline; Described hydrogenation reaction system bottom links to each other with the Cutting Tap of raffinating oil by pipeline; Described extraction plant bottom is connected with back scrubber by pipeline; Described back scrubber top is connected with the oily water wash column of extraction by pipeline; Described back scrubber bottom is connected with recovery tower by pipeline; Described extraction profit is washed top of tower and is connected with the oily Cutting Tap of extraction by pipeline; The oily Cutting Tap of described extraction top is connected with the bottom of recovery tower with described extraction plant and described back scrubber by pipeline; The oily Cutting Tap of described extraction bottom is by the direct extraction product of pipeline; Described recovery tower top is connected with the bottom of described extraction plant and the bottom of described back scrubber respectively by pipeline; Described recovery tower bottom is connected with the top of described extraction tower by pipeline.
Straight-run diesel oil of the present utility model, catalytic diesel oil and coker gas oil can be arbitrary proportions.
The used back scrubber of the utility model, water wash column, recovery tower and Cutting Tap are conventional back scrubber, water wash column, recovery tower and Cutting Tap.Used extraction plant is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The used hydrogenation reaction system of the utility model is existing hydrogenation system, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser, stabilizer tower etc.
Beneficial effect:
The advantage of the preparation low sulfur content of the present utility model and the system of low olefin-content diesel oil is: compare with the hydrorefined mode of ordinary diesel oil, hydrogenation unit of the present utility model only at raffinate oil or special requirement under extraction oil, small scale, cost is low; Simultaneously, straight-run diesel oil is not only handled in the raw material variation that the utility model is handled, can also handle catalytic diesel oil and and the mixture of coker gas oil; And the utility model is separated aromatic hydrocarbons from diesel oil, has improved diesel-fuel cetane number greatly, has reduced condensation point of diesel oil; At last, the utility model can under the situation that satisfies condensation point of diesel oil and aromaticity content, enter part or all of mediation of aromatic component in the diesel oil according to practical situation, increases production of diesel oil.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment.
Below by embodiment the utility model is described further, but and does not mean that restriction the utility model protection domain.
Embodiment
Fig. 1 is the schematic flow sheet of present embodiment, and some utility appliance such as separating tank, pump etc. among the figure do not mark, but this is known to those of ordinary skills.
As shown in Figure 1, be 160-423 ℃ with boiling range, sulphur content is 3500ppm, density is 813.7kg/m
3Aromaticity content is 28%, to be 46 straight-run diesel oil add extraction tower 1 with 100 tons/hour flow and solvent with 500 tons/hour flow with the mixture (feedstock property sees Table 1-1) of residual oil to cetane value 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 160-397 ℃, and sulphur content is 933.3ppm, and density is 798.9kg/m
3, aromaticity content is 7.3%, cetane value is 55.0; The boiling range that gained is extracted oil out is 160-449 ℃, and sulphur content is 11200ppm, and density is 861.6kg/m
3, aromaticity content is 90.2%, cetane value is 19.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 75 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 head temperature of water wash column 2-1 of raffinating oil is 60 ℃, roof pressure power is 0.4MPa, raffinating oil after the gained washing mixed 0.64 ton/hour hydrogen with 75 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 6.8 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 is 360 ℃, and reaction pressure is 4.0MPa, and hydrogen-oil ratio is 300, and air speed is 3.5h
-1, the gained hydrogenation is raffinated oil and is entered the Cutting Tap 4-1 that raffinates oil with 75 tons/hour flow and handle; The boiling range that described hydrogenation is raffinated oil is 160-394 ℃, and sulphur content is 160ppm, and density is 797.8kg/m
3, aromaticity content is 7.3%, cetane value is 55.9.The tower top temperature of the described Cutting Tap 4-1 that raffinates oil is 180 ℃, and column bottom temperature is 360 ℃, and working pressure is-0.06MPa.The Cutting Tap 4-1 cat head extraction flow of raffinating oil be 65.71 tons/hour diesel oil directly as product, the extraction flow is that 9.29 tons/hour solvent oil is directly as product at the bottom of the tower.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 525 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 75 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.The extraction of back scrubber 5 cat head extraction oil and the mixture that returns lotion enter by pipeline with 40 tons/hour flow and extract oily water wash column 2-2 middle part out, meanwhile, washing water enters for 7.6 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 4-2 processing of extraction by extracting the extraction of oily water wash column 2-2 cat head out, directly discharges bottom the oily water wash column 2-2 of extraction for 7.6 tons/hour through the washing water that uses.110 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 370 ℃, tower top pressure 0.15MPa, tower bottom pressure 0.18MPa, reflux ratio is 0.5.Flow be 15.0 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle (bottom that enters back scrubber 5 bottoms and extraction tower 1) after lotion mixes with returning of recovery tower 6 top extraction; BTX aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 25 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, tower top pressure 0.20MPa, tower bottom pressure 0.24MPa with 560 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 60 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 500 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 1-2,1-3,1-4.
Embodiment 2
Shown in Figure 1, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
As shown in Figure 1, be 160-424 ℃ with boiling range, sulphur content is 4200ppm, density is 866.2kg/m
3Aromaticity content is 45%, to be 34.8 straight-run diesel oil add extraction tower 1 with 100 tons/hour flow and solvent with 740 tons/hour flow with the mixture (feedstock property sees Table 2-1) of residual oil to cetane value 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 160-399 ℃, and sulphur content is 1333.3ppm, and density is 849.8kg/m
3, aromaticity content is 17.3%, cetane value is 45.7; The boiling range that gained is extracted oil out is 160-447 ℃, and sulphur content is 9081.1ppm, and density is 895.6kg/m
3, aromaticity content is 92.1%, cetane value is 16.2.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 63 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 5.8 tons/hour flow, the service temperature of water wash column 2-1 of raffinating oil is 80 ℃, working pressure is 0.55MPa, raffinating oil after the gained washing mixed 0.79 ton/hour hydrogen with 63 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 5.8 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 is 330 ℃, 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 entered the Cutting Tap 4-1 that raffinates oil with 63 tons/hour flow and handle; The tower top temperature of the described Cutting Tap 4-1 that raffinates oil is 190 ℃, and column bottom temperature is 370 ℃, and working pressure is-0.05MPa.The Cutting Tap 4-1 cat head extraction flow of raffinating oil be 54.96 tons/hour diesel oil directly as product, the extraction flow is that 8.04 tons/hour solvent oil is directly as product at the bottom of the tower.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 777 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 111 tons/hour the lotion that returns enters by back scrubber 5 bottoms, the service temperature of back scrubber 5 is 100 ℃, working pressure is 0.65MPa, returns and washes than 0.7.64.75 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 11.3 tons/hour extracts oily water wash column 2-2 top out, the service temperature of the oily water wash column 2-2 of described extraction is 80 ℃, and working pressure is 0.65MPa.Extraction oil after the washing enters the oily Cutting Tap 4-2 of extraction by the extraction of the oily water wash column 2-2 cat head of extraction, directly discharges bottom the oily water wash column 2-2 of extraction for 11.3 tons/hour through the washing water that uses.125 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 380 ℃, tower top pressure 0.18MPa, tower bottom pressure 0.21MPa, reflux ratio is 1.0.Flow be 27.75 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; BTX aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 37.0 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 0.17MPa with 823.25 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 83.25 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 740 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 2-2,2-3,2-4.
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment, some utility appliance among the figure such as jar, pump, interchanger, condenser etc. do not mark, but this is known to those of ordinary skills.
With boiling range is 160-424 ℃, and sulphur content is 1600ppm, and density is 836.5kg/m
3Aromaticity content is 31%, cetane value is that the mixture (feedstock property sees Table 3-1) of 41.3 straight-run diesel oil, residual oil, catalytic diesel oil, slurry oil adds extraction tower 1 with 100 tons/hour flow and solvent together with 500 tons/hour flow and carries out extracting, the temperature of extraction tower 1 is 90 ℃, and pressure is 0.65MPa, and solvent ratio is 2, solvent for use is a dimethyl sulfoxide (DMSO), the boiling range that gained is raffinated oil is 160-401 ℃, and sulphur content is 426.7ppm, and density is 819.8kg/m
3, aromaticity content is 10.8%, cetane value is 49.9; The boiling range that gained is extracted oil out is 160-445 ℃, and sulphur content is 5120ppm, and density is 891.0kg/m
3, aromaticity content is 91.6%, cetane value is 15.6.Gained is raffinated oil and is entered the water wash column 2-1 middle part of raffinating oil with 75 tons/hour the flow top by extraction tower 1, simultaneously, washing water enters the water wash column 2-1 top of raffinating oil with 6.9 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 0.29 ton/hour hydrogen with 75 tons/hour flow by water wash column 2-1 top and entered hydrogenation reaction system 3 and carry out hydrogenating desulfurization, directly discharges by the water wash column bottom of raffinating oil with 6.9 tons/hour flow through the washing water that uses.The temperature of reaction of the hydrogenator in the described hydrogenation reaction system 3 is 300 ℃, 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 entered the Cutting Tap 4-1 that raffinates oil with 75 tons/hour flow and handle; The tower top temperature of the described Cutting Tap 4-1 that raffinates oil is 200 ℃, and column bottom temperature is 380 ℃, and working pressure is-0.04MPa.The Cutting Tap 4-1 cat head extraction flow of raffinating oil be 64.6 tons/hour diesel oil directly as product, the extraction flow is that 10.4 tons/hour solvent oil is directly as product at the bottom of the tower.The extraction oil that obtains from extraction tower 1 and the mixture of solvent enter back scrubber 5 with 525 tons/hour flow at the bottom of by extraction tower 1 tower, the while flow is that 75 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 1.0.47.5 tons/hour in the extraction of back scrubber 5 cat head extraction oil and the mixture that returns lotion enter by pipeline and extract oily water wash column 2-2 middle part out, meanwhile, washing water enters for 7.7 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 0.8MPa.Extraction oil after the washing enters the oily Cutting Tap 4-2 of extraction by the extraction of the oily water wash column 2-2 cat head of extraction, directly discharges bottom the oily water wash column 2-2 of extraction for 7.7 tons/hour through the washing water that uses.140 ℃ of the oily Cutting Tap 4-2 of described extraction tower top temperatures, column bottom temperature is 390 ℃, tower top pressure 0.20MPa, tower bottom pressure 0.25MPa, reflux ratio is 2.0.Flow be 22.5 tons/hour return lotion from the oily Cutting Tap 4-2 of described extraction top extraction, recycle after lotion mixes with returning of recovery tower 6 top extraction; BTX aromatics from the bottom of the oily Cutting Tap 4-2 of described extraction tower with 25.0 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 0.14MPa with 552.5 tons/hour flow at the bottom of back scrubber 5 towers.The lotion that returns of recovery tower 6 cat head extraction enters the bottom of back scrubber 5 bottoms and extraction tower 1 with 52.5 tons/hour flow, and the solvent of extraction enters extraction tower 1 top with 500 tons/hour flow at the bottom of recovery tower 6 towers.The character of products obtained therefrom sees Table 3-2,3-3,3-4.
Table 1 embodiment 1 raw material and product property table
Table 1-1 feedstock property
Table 1-2 hydrogenated diesel oil product property table
| Project | Unit | Numerical value | Method |
| Output | Ton/hour | 65.71 | |
| Sulphur content | ppm | 97.4 | GB/T261 |
Table 1-3 hydrogenation solvent oil product property table
Table 1-4 BTX aromatics product is mainly followed the GB252-2000 standard, and specific nature is as follows:
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 hydrogenated diesel oil product property table
Table 2-3 hydrogenation solvent oil product property table
Table 2-4 BTX aromatics product is mainly followed the GB252-2000 standard, and specific nature is as follows:
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
| Cetane value | 41.3 | GB/T510 | |
| Density | (20℃)kg/m3 | 836.5 | GB/T1885 |
Table 3-2 hydrogenated diesel oil product property table
Table 3-3 hydrogenation solvent oil product property table
Table 3-4 BTX aromatics product is mainly followed the GB252-2000 standard, and specific nature is as follows:
Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Diesel cetane-number is tested with GB/T386; The density of diesel oil is tested with GB/T1884-1885; Diesel oil boiling range scope is tested with GB/T6536.
Claims (1)
1. a system for preparing high-quality diesel comprises extraction plant; It is characterized in that: described extraction plant top is connected with the water wash column of raffinating oil by pipeline; The described water wash column top of raffinating oil is connected with the hydrogenation reaction system of raffinating oil by pipeline; Described hydrogenation reaction system bottom links to each other with the Cutting Tap of raffinating oil by pipeline; Described extraction plant bottom is connected with back scrubber by pipeline; Described back scrubber top is connected with the oily water wash column of extraction by pipeline; Described back scrubber bottom is connected with recovery tower by pipeline; Described extraction profit is washed top of tower and is connected with the oily Cutting Tap of extraction by pipeline; The oily Cutting Tap of described extraction top is connected with the bottom of recovery tower with described extraction plant and described back scrubber by pipeline; The oily Cutting Tap of described extraction bottom is by the direct extraction product of pipeline; Described recovery tower top is connected with the bottom of described extraction plant and the bottom of described back scrubber respectively by pipeline; Described recovery tower bottom is connected with the top of described extraction tower by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202228303U CN201506774U (en) | 2009-09-18 | 2009-09-18 | System for preparing high quality diesel oil through limiting hydrogenation scale |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202228303U CN201506774U (en) | 2009-09-18 | 2009-09-18 | System for preparing high quality diesel oil through limiting hydrogenation scale |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201506774U true CN201506774U (en) | 2010-06-16 |
Family
ID=42467902
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202228303U Expired - Lifetime CN201506774U (en) | 2009-09-18 | 2009-09-18 | System for preparing high quality diesel oil through limiting hydrogenation scale |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201506774U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102021023A (en) * | 2009-09-18 | 2011-04-20 | 北京金伟晖工程技术有限公司 | System and method for preparing high-quality diesel oil by limiting hydrogenation scale |
-
2009
- 2009-09-18 CN CN2009202228303U patent/CN201506774U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102021023A (en) * | 2009-09-18 | 2011-04-20 | 北京金伟晖工程技术有限公司 | System and method for preparing high-quality diesel oil by limiting hydrogenation scale |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105567321B (en) | A kind of method for refining production oil product altogether with oil for coal | |
| CN101333448B (en) | Direct liquefaction process of coal by replacing circling solvent with petroleum or petroleum refining byproduct | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| CN101831317A (en) | Hydrogenation method of hydrocarbon with high contents of aryl and nitrogen | |
| CN102021010A (en) | Processing method of middle and low temperature coal tar | |
| CN101914389B (en) | Method for preparing high-quality diesel by double-hydrogenation system | |
| CN104004541B (en) | A kind of preparation method of coal-based high arene underwater content stock oil | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN201506771U (en) | System for preparing high-quality diesel at low cost | |
| CN201506772U (en) | System of double hydrogenation device for preparing high-quality diesel oil | |
| CN201512505U (en) | System for preparing high quality diesel oil | |
| CN201506774U (en) | System for preparing high quality diesel oil through limiting hydrogenation scale | |
| CN102433156B (en) | A kind of different boiling ranges height aromatic hydrocarbons high-density hydrocarbon oil hydrogenation transforms combined method | |
| CN104611005B (en) | A kind of process increasing production coker gas oil | |
| CN101921622B (en) | Method for preparing high-quality diesel by raffinate oil hydrogenation | |
| CN201506775U (en) | System for preparing high-quality diesel oil by hydrogenation of raffinate oil | |
| CN102517074B (en) | Production method of environmentally-friendly rubber filling oil | |
| CN102021024B (en) | System for producing diesel of high quality and method thereof | |
| CN201506773U (en) | System provided with double hydrogenation units for preparing high-quality diesel | |
| CN201506776U (en) | Extracted oil hydrogenation system for preparing high-quality diesel oil | |
| WO2010083642A1 (en) | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons | |
| CN101921624B (en) | Method for preparing high-quality diesel by extract oil hydrogenation | |
| CN201506778U (en) | Preparation system for high-quality diesel | |
| CN201506777U (en) | System provided with double hydrogenation systems for preparing high-quality diesel | |
| CN102021023B (en) | System and method for preparing high-quality diesel oil by limiting hydrogenation scale |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20100616 Effective date of abandoning: 20090918 |
|
| RGAV | Abandon patent right to avoid regrant |