CN1324918A - Simultaneous qualified coal and diesel oil producing process - Google Patents
Simultaneous qualified coal and diesel oil producing process Download PDFInfo
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- CN1324918A CN1324918A CN 00110442 CN00110442A CN1324918A CN 1324918 A CN1324918 A CN 1324918A CN 00110442 CN00110442 CN 00110442 CN 00110442 A CN00110442 A CN 00110442A CN 1324918 A CN1324918 A CN 1324918A
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Abstract
A hydrogenation refining process capable of simultaneously producing corrected gas fuel and diesel oil product from kerosene diesel oil fraction of sulfur-contained crude oil is characterized by adding a kerosene hydrogenation refining reactor and correspondent high-low pressure separators on the basis of existent diesel oil hydrogenation refining process, and making then share a set of new hydrogen and cycle hydrogen system to implement respective hydrogenatino treatments of kerosene and diesel oil so as to attain the goal of simultaneously producing corrected gas fuel and diesel oil product, and thus it can greatly reduce equipment investment, and can obviously reduce energy consumption of the system.
Description
The present invention relates to the treatment process of coal diesel oil distillate, especially coal diesel oil hydroprocessing method.
Continuous fast development along with Chinese national economy, all trades and professions are increasing for the demand of petroleum products, but be mostly sulphur-bearing crude because domestic crude production rate far can not satisfy the oil variety of market demand and the available purchase in international crude oil market, so the inlet part sulphur-bearing crude is just imperative.The coal sulphur content of diesel fraction height of these crude oil will be produced qualified product and must carry out hydrofining.Therefore; the situation that China's oil refining industry faces is that the coal of crude oil, the higher needs of sulphur content of diesel oil distillate are made with extra care on the one hand; and strengthen environmental protection is sought survival again and is produced the more light Fuel oil product of cleaning on the other hand, and the factor of this two aspect has determined coal, diesel oil hydrofining technology that huge demand is arranged at home.
Kerosene and diesel oil distillate carry out hydrorefined Technology maturation very respectively, the catalyzer of available use is brought in constant renewal in and is regenerated, level improves constantly, and these catalyzer have comprised with metals such as Mo-Co, Mo-Ni, Mo-Ni-Co, W-Mo-Ni as active ingredient, sphere or special-shaped Al
2O
3Do the various Hydrobon catalysts of carrier.With middle-eastern crude straight run coal, diesel oil hydrofining is example, and the hydrorefined reaction conditions of kerosene(oil)fraction is generally: pressure 1.0-4.0MPa, air speed 2.5-4.0h
-1, gas and oil volume ratio 200-300: 1, temperature of reaction 150-300 ℃; Diesel oil fraction hydrogenating purified reaction conditions is: pressure 3.0-6.0MPa, air speed 2.5-3.5h
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 300-370 ℃.Therefore, kerosene and diesel oil hydrofining can be operated under essentially identical operational condition, just the temperature of reaction difference that needs.
At present comparatively sophisticated coal, diesel oil hydrofining scheme have the kerosene used with Maoming petro-chemical corporation, diesel oil respectively carry out on two covering devices hydrofining be representative and the coal of using with West Pacific Ocean, Dalian petrochemical industry stock company, diesel oil respectively on a covering device blocked operation carry out the technological line that hydrofining is representative (referring to the 17th page to 22 pages of refining of petroleum and chemical industry 1999 the 1st phases).In the last scheme, the less full scale plant of two covers is all many than gross investment, process cost and the floor space of the big full scale plant of a cover, and economy is less better; Then in the scheme, a covering device switches reconstructed coal diesel oil not only fluctuation of service, the waste of kerosene product resource, and what is more important greatly reduces the utilization ratio of device.
For this reason, we have carried out the hydrorefined research of coal diesel oil mixed fraction in real work, and practice is found: when carrying out coal, the hydrofining of diesel oil mixed fraction, owing to will guarantee certain desulfurization depth, therefore just need higher temperature of reaction.Under the effect of catalyzer, the heavier cut generation hydrocracking reaction of part in the raw material and generated the lighter fraction that is rich in aromatic hydrocarbons and since the thermodynamics equilibrium limit lighter fraction at high temperature dehydrogenation of hydrocarbons generate the reinforcement of aromatic hydrocarbons tendency, the result has produced the problem that the kerosene(oil)fraction aromaticity content increases, smoke point descends.Though reached the purpose of desulfurization after the hydrofining, be difficult to produce qualified rocket engine fuel.
The object of the invention is on the basis of above two approach, and kerosene and diesel hydrotreating unit are carried out organic, rational combination, realizes that a covering device produces qualified rocket engine fuel and diesel oil simultaneously, and reduces the waste of investment or energy, general facilities expense.
The objective of the invention is to be achieved through the following technical solutions:
After the coal diesel oil distillate is not heated to temperature of reaction, under the condition of hydrogen and hydrogenation catalyst existence, in kerosene hydrogenation reactor and diesel oil hydrogenation reactor, carry out hydrogenation reaction respectively, reaction product enters respectively after separately separation system separates, fuel gas and sour water go out device respectively, hydrogen-containing gas passes through recycle system Returning reacting system with new hydrogen, the stripping tower that coal diesel oil distillate behind the hydrogenation enters respectively separately carries out stripping, qualified coal, diesel product is respectively by going out device at the bottom of the stripping tower separately, and the hydrogenation gas product is then by separately stripping tower liftout attachment; The temperature of reaction of described diesel oil distillate is to carry out heat exchange by the reaction product that diesel oil distillate and diesel oil hydrogenation reactor are come out, and then enter that process furnace heating reaches, the temperature of reaction of described kerosene(oil)fraction is to reach by the reaction product heat exchange that part or all of kerosene(oil)fraction and diesel oil hydrogenation reactor are come out, and described kerosene hydrogenation reactor and diesel oil hydrogenation reactor reaction product are through separating the hydrogen-containing gas that obtains through same recycle system Returning reacting system.
Described diesel oil distillate and kerosene(oil)fraction can be the straight run that hydro carbons distillations such as crude oil, shale oil, the dry distillation of coal, oil-sand directly obtain, and also can be the corresponding cuts that process secondary processing process such as hydrocracking, catalytic cracking, coking etc. obtain.
The hydrogenation conditions of described kerosene is generally:
Reaction pressure 1.0-4.0MPa, volume space velocity 1.0-4.0h during liquid
-1, gas and oil volume ratio 200-300, temperature of reaction 150-300 ℃; Optimum condition is: reaction pressure 3.0-4.0MPa, volume space velocity 2.5-3.5h during liquid
-1, gas and oil volume ratio 200-300: 1, temperature of reaction 150-250 ℃.
The reaction conditions of diesel oil fraction hydrogenating is generally reaction pressure 3.0-6.0MPa, volume space velocity 1.0-4.0h during liquid
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 300-370 ℃; Optimum condition is: reaction pressure 3.0-4.0MPa, volume space velocity 2.5-3.5h during liquid
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 320-370 ℃.
Described hydrogenation catalyst can be selected from industrial Hydrobon catalyst or deep hydrogenation saturation catalyst.As with metals such as Mo-Co, Mo-Ni, Mo-Ni-Co, W-Mo-Ni as active ingredient, sphere or special-shaped Al
2O
3Do carrier various Hydrobon catalysts or or the deep hydrogenation saturation catalyst, for example can adopt 481-3 (Wenzhou catalyst plant, Shenyang Catalyst Plant produce), FDS-4A (Wenzhou catalyst plant, Shenyang Catalyst Plant produce), FDS-4 (Fushun No.3 Petroleum Factory's catalyst plant is produced), FH-5 (Wenzhou catalyst plant, Shenyang Catalyst Plant produce), FH-5A (production of Wenzhou catalyst plant), FH-98 various commercial catalystss such as (productions of Wenzhou catalyst plant).Described kerosene hydrogenation can use identical Hydrobon catalyst with diesel oil hydrogenation, also can use different Hydrobon catalysts.
In order to adjust the temperature in that kerosene(oil)fraction enters hydrofining reactor preferably, after can making kerosene(oil)fraction enter a control valve, be divided into two the tunnel, one the tunnel enters the heat-exchange system of diesel oil hydrogenation system, i.e. reactant heat exchange of coming out with the diesel oil hydrogenation reactor, obtain behind the required heat of reaction to be mixed into kerosene hydrogenation refining reaction device, adjust the temperature in of kerosene reactor by the ratio of adjusting the two-way logistics with another road raw material without heat exchange.After can certainly making kerosene(oil)fraction enter a control valve, be divided into three the tunnel, one the tunnel enters the heat-exchange system of diesel oil hydrogenation system, i.e. reactant heat exchange of coming out with the diesel oil hydrogenation reactor, one tunnel reactant heat exchange of coming out with the kerosene hydrogenation reactor, kerosene(oil)fraction after this two-way heat exchange and another road enter the kerosene hydrogenation reactor after mixing without the kerosene(oil)fraction raw material of heat exchange, adjust the temperature in of kerosene reactor by the ratio of adjusting three tunnel logistics; After perhaps also can making kerosene(oil)fraction enter a control valve, be divided into two the tunnel, one the tunnel enters the heat-exchange system of diesel oil hydrogenation system, i.e. reactant heat exchange of coming out with the diesel oil hydrogenation reactor, one tunnel reactant heat exchange of coming out with the kerosene hydrogenation reactor, the two-way raw material enters kerosene hydrogenation refining reaction device after mixing, and adjusts the temperature in of kerosene reactor by the ratio of adjusting this two-way logistics.
Recycle hydrogen and new hydrogen that hydrogen in kerosene and the diesel oil fraction hydrogenating reactive system is come out by separation system are formed.The composition of recycle hydrogen is generally (hydrogen 70-95v%, methane, ethane and heavier hydrocarbon gas 5-30v%); The composition of new hydrogen is generally (hydrogen 80-99v%, methane, ethane and heavier hydrocarbon gas 1-20v%), can be the reformation hydrogen that catalytic reforming unit produces, also industrial hydrogen such as the hydrogen of the hydrogen of refinery hydrogen preparing device, chemical plant installations by-product or electrolysis hydrogen.Recycle hydrogen mixes the back Returning reacting system by following hydrogen compressor and new hydrogen, they generally are to mix with reaction raw materials diesel oil or kerosene(oil)fraction earlier, heat together then reach temperature of reaction after, enter hydrogenator at last.
Described fuel gas is that organosulfur impurity in part kerosene(oil)fraction, the diesel oil distillate is through being converted into the micro-molecular gas hydrocarbon that inorganic sulfur-hydrogen sulfide and most hydrogenation reaction generate after the hydrotreatment, a part goes out device through separation system with device discharging hydrogen, its composition situation identical with recycle hydrogen (hydrogen 70-95v%, methane, ethane and heavier hydrocarbon gas 5-30v%); And another part is told the fuel gas system that enters the refinery at the light pressure separator of separation system, and its composition situation is: hydrogen 15-35v%, methane, ethane and heavier hydrocarbon gas 65-85v%).
Described sour water be organosulfur, nitrogen impurity in the raw material through the hydrogen sulfide that changes into after the hydrotreatment, ammonia is dissolved by the buck that injects from reactor exit becomes sour water, the self-separation device is discharged, and its composition is mainly water, ammonia, sodium sulphite and hydrogen sulfide.
Described kerosene(oil)fraction, diesel oil distillate raw material generally need enter stripping tower through behind the hydrogenation, with the C that accounts for raw material total amount 1-2w% of reaction production
3-C
6Lighter hydrocarbons such as low-carbon (LC) hydro carbons such as pentane are separated from cat head, and its composition situation is C
2-C
4Gas 30-40w%, C
5Above gasoline 60-70w%.At the bottom of tower, produce qualified kerosene, diesel product.
Certainly, in above-mentioned flow process, kerosene hydrogenation and diesel oil hydrogenation can be only shared hydrogen gas circulating systems, and not shared heat-exchange system device, that is the kerosene hydrogenation reactor reaction product of the coming out reaction product heat exchange of not coming out with the diesel oil hydrogenation reactor, and reach temperature of reaction (as establishing a kerosene(oil)fraction process furnace again by other conventional heating means, or the steam-heated method of employing refinery's pipe network, or kerosene(oil)fraction and the shared process furnace of diesel oil distillate, the reaction product heat exchange that described kerosene(oil)fraction and kerosene hydrogenation refining reaction device are come out, and then utilize other heating means etc.); It also can be the only shared cover heat exchange system of kerosene hydrogenation and diesel oil hydrogenation, that is the temperature of reaction of kerosene(oil)fraction is by the reaction product heat exchange of coming out of all or part of kerosene(oil)fraction and diesel oil hydrogenation reactor is reached, kerosene hydrogenation reactor and diesel oil hydrogenation reactant flow then are respectively through separately hydrogen recycle compressor Returning reacting system through the hydrogen-containing gas of resulting separation, not shared cover hydrogen gas circulating system.But take all factors into consideration from the angle of economy, the present invention preferentially selects the scheme of diesel oil hydrogenation and shared cover heat exchange system of kerosene hydrogenation and hydrogen gas circulating system.
The above-described technical scheme according to the present invention, can be on the basis of existing diesel oil hydrofining technical process, increase a kerosene hydrogenation refining reaction device and corresponding high and low pressure separator, shared cover new hydrogen and a recycle hydrogen system is implemented in the hydrogenation purpose of producing qualified rocket engine fuel and diesel product simultaneously respectively of coal, diesel oil in the device.
Compared with prior art, outstanding feature of the present invention is as follows:
1, in the diesel oil hydrofining technical process, increased kerosene(oil)fraction hydrofining system, use a new hydrogen of cover and a recycle hydrogen system, saved the investment aspect the hydrogen gas compressor (in the gross investment at hydrogenation unit, the shared ratio of hydrogen gas compressor is 8-15%);
2, the raw material of kerosene hydrogenation refining system provides reaction required heat by the high temperature heat source that utilizes the diesel oil hydrofining part by the interchanger heat exchange, saved a process furnace, also reclaimed the heat (in the gross investment of hydrogenation unit, the shared ratio of process furnace is 6-10%) of main flow preferably;
3, coal, diesel oil hydrofining are system independently separately, can continue to keep normal operation under the situation that the kerosene hydrogenation refining system is stopped using as the diesel oil hydrofining system of main flow;
4, independently coal, diesel oil hydrofining system have good handiness, can carry out hydrofining under suitable separately reaction conditions, produce qualified product;
5, compare with building independently coal, diesel oil hydrofining two covering devices respectively, can save soil and investment;
Fig. 1 is the schema of the preferential diesel oil hydrogenation of recommending of the present invention and shared cover heat exchange system of kerosene hydrogenation and hydrogen gas circulating system scheme.
Below in conjunction with accompanying drawing 1 and embodiment process of the present invention is further described.
In the diesel oil hydrofining main flow, straight-run diesel oil raw material 1 through the reactant flow heat exchange of heat-exchange system 4 with the diesel oil hydrofining reactor, enters reactor 3 through process furnace 2 with after hydrogen from hydrogen gas system 8 mixes again in pipeline.Reaction product is through heat exchange and cooling, and in the separation of separation system 5 realization recycle hydrogens, sour water 17, hydrogenated diesel oil, behind hydrogenated diesel oil process stripping tower 6 strippings, qualified diesel product goes out device at the bottom of the tower, and overhead product 19 (is generally C
2-C
4Gas and C
5Above gasoline) then go out device.In the kerosene hydrogenation refining system, virgin kerosene raw material 9 is divided into two-way through control valve 15, one the tunnel enters the heat-exchange system 4 of diesel oil hydrofining system, obtain behind the required heat of reaction to be mixed into kerosene hydrogenation refining reaction device 10, adjust the temperature in of kerosene reactor by the ratio of regulating the two-way logistics with another road raw material without heat exchange.Equally, behind reaction product process separation system 11, stripping tower 12 strippings, rocket engine fuel qualified at the bottom of the tower goes out device, and overhead product 18 (is generally C
2-C
4Gas and C
5Above gasoline) go out device, sour water 16 self-separation systems go out device.Fuel gas 20 can give off device from two cover separation systems.New hydrogen 14 and all enter after hydrogen gas system handles from the recycle hydrogens of two cover separation systems 5 and 11 is as the recycle hydrogen and the cold hydrogen source of two cover hydrofining systems, the H that reaction generates
2S21 also uses solvent (diethanolamine) to dissolve absorption in hydrogen gas system and tells.
Embodiment 1-5
Embodiment 1-5 is the test of carrying out on the 100ml small test device, and used flow process is a flow process shown in Figure 1.The used catalyzer of kerosene and diesel oil hydrofining is the Co-Mo type FDS-4 Hydrobon catalyst of Fushun Petrochemical Research Institute's exploitation, No.3 Petroleum Factory, Fushun Petroleum Chemical Industry Co.'s catalyst plant production, used stock oil is coal, the diesel oil distillate of Saudi Arabia's light crude, main character is listed in table 1, and the main character of test conditions and product is listed in respectively in the table 2,3.
The stock oil character that table 1 embodiment uses
| Feedstock property | Kerosene | Diesel oil |
| Density (20 ℃), g/cm 3Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP sulphur, the w% mercaptan sulfur, μ g/g nitrogen, μ g/g aromaticity content, the v% smoke point, mm cetane index freezing point/zero pour, ℃ | ????0.7823 ????143/162 ????174/187 ????203/227 ????240/258 ????0.165 ????63 ????3 ????16.7 ????26 ????- ????-53/- | ????0.8429 ????237/261 ????274/290 ????311/338 ????349/354 ????0.99 ????- ????90 ????- ????- ????55 ????-11 |
The reaction conditions of table 2 diesel oil hydrofining system and product main character
| Embodiment |
| 1 | | | Embodiment 4 | | ||
| Reaction conditions hydrogen dividing potential drop, MPa air speed, h -1Hydrogen-oil ratio, the v temperature of reaction, ℃ | ?3.4 ?2.5 ?300∶1 ?320 | ?3.0 ?3.0 ?300∶1 ?330 | ?3.0 ?3.0 ?300∶1 ?340 | ?3.4 ?3.0 ?300∶1 ?350 | ?3.4 ?3.5 ?300∶1 ?360 | The solar oil specification |
| Product property density (20 ℃), g/cm 3Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP sulphur, w% nitrogen, μ g/g cetane index condensation point, ℃ | ?0.8302 ?213/253 ?269/285 ?305/334 ?345/352 ?0.0754 ?42 ?61 ?-8 | ?0.8331 ?233/253 ?270/285 ?306/334 ?345/352 ?0.1154 ?58 ?60 ?-10 | ?0.8326 ?228/253 ?270/285 ?306/334 ?345/352 ?0.0883 ?46 ?60 ?-9 | ?0.8314 ?218/253 ?269/285 ?305/334 ?345/352 ?0.0427 ?38 ?61 ?-8 | ?0.8305 ?217/253 ?269/285 ?305/334 ?345/352 ?0.0387 ?26 ?61 ?-8 | ＜0.2 (in the recent period)＜0.05 (future)＞45 |
The reaction conditions of table 3 kerosene hydrogenation refining system and product main character
| Embodiment |
| 1 | | | Embodiment 4 | | ||
| Reaction conditions hydrogen dividing potential drop, MPa air speed, h -1Hydrogen-oil ratio, the v temperature of reaction, ℃ | ????3.4 ????2.5 ????300∶1 ????160 | ????3.0 ????3.0 ????300∶1 ????170 | ????3.4 ????3.0 ????300∶1 ????179 | ????3.4 ????3.0 ????300∶1 ????200 | ????3.4 ????3.5 ????300∶1 ????230 | 3# rocket engine fuel specification |
| Product property density (20 ℃), g/cm 3Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP sulphur, the w% mercaptan sulfur, μ g/g aromaticity content, the v% smoke point, the mm freezing point, ℃ | ????0.7821 ????150/161 ????173/188 ????203/228 ????240/256 ????0.150 ????31 ????15.4 ????26 ????-52 | ????0.7824 ????150/161 ????173/188 ????203/228 ????240/256 ????0?153 ????29 ????15.4 ????26 ????-52 | ????0.7820 ????150/161 ????173/188 ????203/228 ????240/256 ????0.144 ????20 ????15.0 ????27 ????-52 | ????0.7790 ????150/161 ????171/187 ????202/226 ????240/256 ????0.102 ????6 ????13.9 ????28 ????-51 | ????0.7795 ????150/161 ????171/187 ????202/226 ????240/256 ????0.081 ????14.0 ????28 ????-51 | ????＞0.775 ????＜0.2 ????＜20 ????＜20 ????＞25 ????＜47 |
Claims (18)
1. produce qualified coal simultaneously for one kind, the method of diesel product, with coal, after diesel oil distillate is not heated to temperature of reaction, under the condition of hydrogen and hydrogenation catalyst existence, in kerosene hydrogenation reactor and diesel oil hydrogenation reactor, carry out hydrogenation reaction respectively, reaction product enters respectively after separately separation system separates, fuel gas, sour water goes out device, recycle hydrogen enters reactive system with new hydrogen through the recycle system, coal after the hydrofining, the stripping tower that diesel oil distillate does not enter separately carries out stripping, qualified coal, diesel product is respectively by going out device at the bottom of the stripping tower separately, and the hydrogenation gas product is then by separately stripping tower liftout attachment; The temperature of reaction that it is characterized in that described diesel oil distillate is to enter heat exchange by the reaction product that diesel oil distillate and diesel oil hydrogenation reactor are come out, and then enter that process furnace heating reaches, the temperature of reaction of described kerosene(oil)fraction is to reach by the reaction product heat exchange that part or all of kerosene(oil)fraction and diesel oil hydrogenation reactor are come out, and described kerosene hydrogenation reactor and diesel oil hydrogenation reactor reaction product are through separating the hydrogen-containing gas that obtains through same recycle system Returning reacting system.
2. according to the described method of producing qualified coal, diesel product simultaneously of claim 1, it is characterized in that the reaction conditions of described kerosene hydrogenation is: reaction pressure 1.0-4.0MPa, volume space velocity 2.5-4.0h during liquid
-1, gas and oil volume ratio 200-300: 1, temperature of reaction 150-300 ℃.
3. according to the described method of producing qualified coal, diesel product simultaneously of claim 1, it is characterized in that the reaction conditions of described diesel oil hydrogenation is: reaction pressure 3.0-6.0MPa, volume space velocity 2.5-3.5h during liquid
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 300-370 ℃.
4. according to the described method of producing qualified coal, diesel product simultaneously of claim 1, it is characterized in that described hydrogenation catalyst is to be selected from industrial Hydrobon catalyst or deep hydrogenation saturation catalyst.
5. according to the described method of producing qualified coal, diesel product simultaneously of claim 1, the temperature of reaction that it is characterized in that described kerosene(oil)fraction is after making kerosene(oil)fraction enter a control valve, be divided into two-way, one the tunnel enters the heat-exchange system of diesel oil hydrogenation system, obtain behind the required heat of reaction to be mixed into the kerosene hydrogenation reactor, adjust the temperature in of kerosene reactor by the ratio of adjusting the two-way logistics with another road raw material without heat exchange.
6. method of producing qualified coal, diesel product simultaneously, after the coal diesel oil distillate is not heated to temperature of reaction, under the condition of hydrogen and hydrogenation catalyst existence, in kerosene hydrogenation reactor and diesel oil hydrogenation reactor, carry out hydrogenation reaction respectively, reaction product enters respectively after separately separation system separates, fuel gas, sour water go out device respectively, hydrogen-containing gas passes through same recycle system Returning reacting system with new hydrogen, by going out device at the bottom of the stripping tower separately, the hydrogenation gas product goes out device by cat head separately respectively for qualified coal, diesel product; The temperature of reaction that it is characterized in that described diesel oil distillate is to enter heat exchange by the reaction product that diesel oil distillate and diesel oil hydrogenation reactor are come out, and then enter that process furnace heating reaches, the temperature of reaction of described kerosene(oil)fraction is to reach by the reaction product heat exchange that part or all of kerosene(oil)fraction and diesel oil hydrogenation reactor are come out, described kerosene hydrogenation reactor and diesel oil hydrogenation reactor reaction product through separation the hydrogen-containing gas that obtains be respectively through separately the recycle system with new hydrogen Returning reacting system.
7. according to the described method of producing qualified coal, diesel product simultaneously of claim 6, it is characterized in that described kerosene hydrogenation purified reaction conditions is: reaction pressure 1.0-4.0MPa, volume space velocity 2.5-4.0h during liquid
-1, gas and oil volume ratio 200-300: 1, temperature of reaction 150-300 ℃.
8. according to the described method of producing qualified coal, diesel product simultaneously of claim 6, it is characterized in that the reaction conditions of described diesel oil hydrofining is: reaction pressure 3.0-6.0MPa, volume space velocity 2.5-3.5h during liquid
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 300-370 ℃.
9. according to the described method of producing qualified coal, diesel product simultaneously of claim 6, it is characterized in that described Hydrobon catalyst is selected from industrial Hydrobon catalyst or deep hydrogenation saturation catalyst.
10. according to the described method of producing qualified coal, diesel product simultaneously of claim 6, the temperature of reaction that it is characterized in that described kerosene(oil)fraction is after making kerosene(oil)fraction enter a control valve, be divided into two-way, one the tunnel enters the heat-exchange system of diesel oil hydrogenation system, obtain behind the required heat of reaction to be mixed into the kerosene hydrogenation reactor, adjust the temperature in of kerosene reactor by the ratio of adjusting the two-way logistics with another road raw material without heat exchange.
11. method of producing qualified coal, diesel product simultaneously, after the coal diesel oil distillate is not heated to temperature of reaction, under the condition of hydrogen and hydrogenation catalyst existence, in kerosene hydrogenation reactor and diesel oil hydrogenation reactor, carry out hydrogenation reaction respectively, after reaction product enters the separation system separation respectively, qualified coal, diesel product and fuel gas, sour water go out device respectively, and hydrogen-containing gas loops back reactive system; It is characterized in that described kerosene hydrogenation reactor and diesel oil hydrogenation reactor reaction product are through separating the hydrogen-containing gas that obtains through same recycle system Returning reacting system.
12., it is characterized in that described kerosene hydrogenation purified reaction conditions is: reaction pressure 1.0-4.0MPa, volume space velocity 2.5-4.0h during liquid according to the described method of producing qualified coal, diesel product simultaneously of claim 11
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 150-300 ℃.
13. according to the described method of producing qualified coal, diesel product simultaneously of claim 11, it is characterized in that the reaction conditions of described diesel oil hydrofining is: reaction pressure 3.0-6.0MPa, volume space velocity 2.5-3.5h during liquid
-1, gas and oil volume ratio 250-400: 1, temperature of reaction 300-370 ℃.
14., it is characterized in that described Hydrobon catalyst is selected from industrial Hydrobon catalyst or deep hydrogenation saturation catalyst according to the described method of producing qualified coal, diesel product simultaneously of claim 11.
15., it is characterized in that described kerosene(oil)fraction temperature of reaction is to reach by making kerosene(oil)fraction enter independent process furnace heating according to the described method of producing qualified coal, diesel product simultaneously of claim 11.
16., it is characterized in that described kerosene(oil)fraction temperature of reaction reaches by utilizing refinery's pipe network steam heating kerosene(oil)fraction according to the described method of producing qualified coal, diesel product simultaneously of claim 11.
17., it is characterized in that described kerosene(oil)fraction temperature of reaction makes kerosene(oil)fraction reach by entering process furnace with diesel oil distillate according to the described method of producing qualified coal, diesel product simultaneously of claim 11.
18. according to claim 15 or 16 or 17 described methods of producing qualified coal, diesel product simultaneously, it is characterized in that described kerosene(oil)fraction temperature of reaction is the reaction product heat exchange by described kerosene(oil)fraction and kerosene hydrogenation refining reaction device are come out, and then utilize other heating means to reach.
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| CNB00110442XA CN1162519C (en) | 2000-05-19 | 2000-05-19 | Simultaneous qualified coal and diesel oil producing process |
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|---|---|---|---|
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448956C (en) * | 2005-10-19 | 2009-01-07 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN101445747B (en) * | 2007-11-28 | 2012-07-04 | 中国石油化工集团公司 | Hydrofining process integration method |
| CN101724455B (en) * | 2008-10-29 | 2012-09-12 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN103374412A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Combination method for producing high-quality kerosene through hydrogenation |
| CN104611057A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Direct distillation kerosene hydrogenation method |
-
2000
- 2000-05-19 CN CNB00110442XA patent/CN1162519C/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448956C (en) * | 2005-10-19 | 2009-01-07 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN101445747B (en) * | 2007-11-28 | 2012-07-04 | 中国石油化工集团公司 | Hydrofining process integration method |
| CN101724455B (en) * | 2008-10-29 | 2012-09-12 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN103374412A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Combination method for producing high-quality kerosene through hydrogenation |
| CN103374412B (en) * | 2012-04-29 | 2015-05-13 | 中国石油化工股份有限公司 | Combination method for producing high-quality kerosene through hydrogenation |
| CN104611057A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Direct distillation kerosene hydrogenation method |
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