CN101412923B - Hydro-upgrading combined method - Google Patents
Hydro-upgrading combined method Download PDFInfo
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- CN101412923B CN101412923B CN 200810134133 CN200810134133A CN101412923B CN 101412923 B CN101412923 B CN 101412923B CN 200810134133 CN200810134133 CN 200810134133 CN 200810134133 A CN200810134133 A CN 200810134133A CN 101412923 B CN101412923 B CN 101412923B
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Abstract
The invention discloses a hydroprocessing and upgrading integration method, in particular a wax oil hydroprocessing and diesel hydroupgrading integration process. The method comprises the following steps: raw wax oil passes through a first reaction zone in the presence of hydrogen first, liquid obtained after separation of products is taken as catalytic cracking raw material, and hydrogen-rich gas and/or partial light liquid is obtained after the separation; and diesel raw material passes through a second reaction zone in the presence of the hydrogen, gas obtained by separation of products of the second reaction zone is mixed with the gas obtained in the first reaction zone, the mixed gas is recycled after desulfurization, and liquid obtained through the separation is subjected to steam stripping to obtain hydrogenant naphtha and hydrogenant diesel. The method aims at technical characteristics of wax oil hydroprocessing and hydroupgrading, integrates the two technologies for application, simplifies process flow at the same time of meeting the same product requirements, ensures the pressure drop of a whole system, and reduces equipment, investment and operating cost.
Description
Technical field
The present invention relates to a kind of hydro-upgrading combined method, particularly wax oil hydrogenation is processed and the diesel oil hydrogenation modification combined method.
Background technology
The sustainable development of world economy and the increasingly stringent of environmental regulation need to produce a large amount of light clean fuels at present, and these all require existing oil Refining Technologies is improved, and produce satisfactory product with minimum cost.Along with the worsening shortages of crude resources and heaviness, in poor quality development, catalytic cracking (FCC) and coking become the important means of production light Fuel product, but the quality product that these two kinds of techniques obtain generally is difficult to the finger figureofmerit requirement that reaches strict.In the light Fuel quality product system, sulphur content is most important index, how to reduce sulphur content in the petroleum products and be one of most significant problems that current refining of petroleum industry faces, the cetane value of diesel product receives publicity always in addition, and its specification requirement is also more and more stricter.At present, be applied widely in Clean Fuel Production take desulfurization and upgrading as the main purpose hydrogenation technique.Such as the hydrogenation preconditioning technique of catalytically cracked material, light hydrocarbons (such as diesel oil distillate) hydro-upgrading technology etc.
Wherein diesel oil fraction hydrogenating modification technology main purpose is to improve the quality product of diesel oil, existing diesel oil hydrogenation modification such as CN1156752A and CN1289832A etc., although can increase substantially diesel-fuel cetane number and reduce the foreign matter contents such as sulphur, nitrogen, this technology is only applicable to the diesel raw material that cetane value is low, aromaticity content is high.
FCC raw material hydrogenation preconditioning technique can be avoided loss of octane number in the catalytic gasoline hydrogenation treating process, and has following advantage: the replacing speed that can reduce the FCC catalyzer; Reduce the FCC coke yield; Improving the FCC product distributes, improves the purpose product yield, reduces non-purpose product yield; Directly improve the FCC quality product, reduce the product sulphur content; Reduce the quantity discharged of FCC revivifier SOx, NOx etc., so FCC raw material hydrogenation pretreatment technology is widely used in modern refineries.Existing catalytically cracked material preconditioning technique mainly contains: US3983029 and US6793804 disclose hydroprocessing technique and catalyzer, CN1313379 discloses a kind of hydroprocessing process of poor-quality raw material for catalytic cracking, and CN1646665 discloses the hydrotreatment of hydrocarbon raw material.
Wax oil hydrogenation processing and two kinds of technological processs of diesel oil hydrogenation modification are independent operation in the prior art, although can satisfy the purpose requirement, because two cover processing unit (plant)s are fully independent, each own independently equipment and pipeline, certainly will cause total investment expenses high, the high deficiency of process cost.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind ofly for wax oil hydrogenation desulfurization and diesel oil hydrogenation modification combination process, can produce fine-quality diesel oil product and fine quality catalytic cracking raw material oil on the basis of reducing construction investment and reducing process cost.
A kind of hydro-upgrading combined method, raw material comprise wax oil feedstock and diesel oil distillate oil raw material, comprise the steps:
A, under the hydrotreatment operational condition, wax oil feedstock oil is through the hydrotreating catalyst bed, and the hydrotreatment reaction effluent is isolated to gas phase and liquid phase, and gas phase comprises hydrogen-rich gas, liquid phase is the hydrogenation wax oil, and the hydrogenation wax oil is as the catalytic cracking unit raw material;
B, under the hydro-upgrading operational condition, diesel oil distillate stock oil is through the catalyst for hydro-upgrading bed, the hydro-upgrading reaction effluent separates and obtains hydrogen-rich gas, petroleum naphtha and diesel oil; Hydro-upgrading adopts the catalyst for hydro-upgrading that contains modified Y molecular sieve;
The hydrogen-rich gas mixing of the hydrogen-rich gas of c, step a gas phase and step b loops back step a and step b after removing hydrogen sulfide.
It is 350～620 ℃ of heavy endss that the described wax oil stock oil of step a generally comprises boiling range, as being one or more in the various vacuum gas oils (VGO) that obtain in the petroleum refining process, deasphalted oil (DAO), coker gas oil (CGO), heavy cycle oil (HCO) etc., also can be from coal tar, gelatin liquefaction wet goods.
The described hydrotreating catalyst of step a is conventional hydrotreating catalyst, can be various commercial catalysts, as Fushun Petrochemical Research Institute (FRIPP) development and production 3926,3936, the hydrotreating catalyst such as CH-20,3996, FF-14, FF-16, FF-18, FF-26, the catalyzer such as HR-416, HR-448 of Compaynie Francaise des Petroles (IFP), the TK-525 of Denmark Tuo Pusuo company (Topsor), TK-557 catalyzer, KF-752, the KF-840 of He Lan AKZO N. V (AKZO), KF-901, KF-907 etc.The FH-FS of bulk phase catalyst such as Fushun Petrochemical Research Institute (FRIPP) development and production etc.Above-mentioned hydrotreating catalyst also can be prepared by this area knowledge, common hydrotreating catalyst (loaded catalyst, active metallic content is relatively low, generally count 20%～45% with oxide compound) general first Kaolinite Preparation of Catalyst carrier, then use pickling process supported active metal component, bulk phase catalyst (active metallic content is high, generally counts 50%～85% with oxide compound) generally adopts the coprecipitation method preparation.
The described hydrotreatment operational condition of step a is: reaction pressure 3.0～20.0MPa, hydrogen to oil volume ratio are 200: 1～2500: 1, and volume space velocity is 0.1～8.0h
-1, 260 ℃～455 ℃ of temperature of reaction; Preferred operational condition is reaction pressure 4.0～18.0MPa, hydrogen to oil volume ratio 300: 1～2000: 1, volume space velocity 0.2～6.0h
-1, 280～444 ℃ of temperature of reaction.
The described diesel oil distillate raw material of step b can comprise one or more mixing oil of straight-run diesel oil, coker gas oil, catalytic diesel oil, liquefied coal coil light ends etc., also can comprise the light ends such as straight-run spirit, coker gasoline, the boiling range of diesel raw material is generally 64 ℃～390 ℃.
The described catalyst for hydro-upgrading bed of step b can be for using separately catalyst for hydro-upgrading, also can use with the Hydrobon catalyst grating, grating generally is that reaction mass contacts with Hydrobon catalyst first when using, and then contacts with catalyst for hydro-upgrading.Wherein catalyst for hydro-upgrading is the catalyst for hydro-upgrading that contains Modified Zeolite Y, and catalyzer contains WO by weight
315%～30%, NiO or CoO2%～15%, Modified Zeolite Y 10%～45% can contain auxiliary agent such as F simultaneously, and F content is 1%～9% by weight, and carrier is aluminum oxide and/or amorphous aluminum silicide.Wherein Modified Zeolite Y has following character: lattice constant is 2.436～2.444nm, and infrared total acid (160 ℃) is 0.5～1.1mmol/g.Catalyst for hydro-upgrading can the commodity in use catalyzer, such as 3963 catalyzer of Fushun Petrochemical Research Institute's development and production, FC-18 catalyzer etc., also can prepare by this area knowledge.Hydrobon catalyst can adopt the common Hydrobon catalyst in this area, also can adopt high-activity hydrofining catalyst, also can adopt common Hydrobon catalyst and high-activity hydrofining catalyst to be used in conjunction with by suitable way.Hydrobon catalyst can be selected the commercial catalysts that suits, such as Hydrobon catalysts such as FH-5A, the FDS-4A of Fushun Petrochemical Research Institute's development and production, FH-98, FH-DS, FH-UDS, or by the existing method preparation in this area.
The described hydrofining operational condition of step b is generally: reaction pressure 4.0MPa～18.0MPa, temperature of reaction is 260 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～6.0h
-1, hydrogen to oil volume ratio is 100: 1～2000: 1.The hydrogenation process of step a and step b adopts same pressure rating, common desulphurization of recycle hydrogen system easy to use and common recycle hydrogen compressor.
Among the step a, the separation of reaction effluent can be adopted high pressure hot separator, and the high pressure hot separator working pressure is identical with reacting system pressure, and service temperature is generally 180～410 ℃, is preferably 220～390 ℃.Contain the light hydrocarbons that the wax oil hydrogenation treating processes produces in the isolated gas phase of high pressure hot separator, such as diesel oil distillate and gasoline fraction, the isolated gas phase of high pressure hot separator can be mixed with step b diesel oil fraction hydrogenating modification reaction effluent, isolate hydrogen-rich gas, hydrogen-rich gas further removes and uses with additional new hydrogen mixed cycle after hydrogen sulfide increases by circulating hydrogen compressor again.Step a reaction effluent also can adopt cold high pressure separator, the cold high pressure separator working pressure is identical with system pressure, temperature is generally 20～70 ℃, and the isolated gas phase of cold high pressure separator is hydrogen-rich gas, can separate with step b to remove hydrogen sulfide after the hydrogen-rich gas that obtains mixes.
Compared with prior art, the present invention is by optimization technological process and optimize suitable catalyzer grating and operational condition, and different inferior raw materials are improved the quality of products under optimum, has finally obtained desirable comprehensive process effect.In technical process, the inventive method and two kinds of raw materials add respectively man-hour relatively: the advantage such as have saving equipment (gas-liquid separation equipment, stripping apparatus, compressor etc.), technical process is short, facility investment is low, process cost is low.Two cover systems share hydrogen gas system and desulphurization system simultaneously, can save make-up hydrogen compressor, circulating hydrogen compressor and a cover desulphurization system, in addition owing to adopting parallel-connection flow, can greatly reduce the Pressure Drop of system, and can further improve the reaction effect of diesel oil fraction hydrogenating modification, further improve the quality of products.
Description of drawings
Fig. 1 is one embodiment of the present invention schematic flow sheets.
Embodiment
At first wax oil hydrogenation is processed stock oil 1 and is mixed into hydrotreating reactor 3 with hydrogen 2, obtains the low hydrotreatment resultants 4 of impurity such as sulfur-bearing, nitrogen.Hydrotreatment resultant 4 separates in high-pressure separator 5 and obtains liquid hydrogenation wax oil 6 and directly enter catalytic cracking unit, can separate in the high-pressure separator 5 and obtain gas phase 7 and comprise hydrogen-rich gas and light ends, gas phase 7 enters separator 12 jointly with hydro-upgrading resultant 11, also can adopt cold high pressure separator, the gas phase of separation is that hydrogen-rich gas 23 directly enters circulation gas desulphurization system 14; Diesel raw material 8 is mixed into hydro-upgrading reactor 10 with hydrogen 9, obtaining hydro-upgrading produces thing 11 and separates the gas 13 that obtains remove hydrogen sulfide through desulphurization of recycle hydrogen 14 in separator 12, obtain take off rear recycle hydrogen 15 through circulating hydrogen compressor 16 increase pressure and with recycle after new hydrogen 17 mixes, separate the liquid 18 that obtains and enter stripping tower 19 (if gasoline fraction is more in 18, can change separation column into), then obtain gas products 20, gasoline (or petroleum naphtha) 21 and diesel product 22.
Use the main character of stock oil to see Table 1, hydrotreatment operational condition and the results are shown in Table 2, hydrofining operational condition and structure see Table 3.Catalyzer is the commercial catalyst of Fushun Petrochemical Research Institute's development and production.
Table 1 stock oil character
| The stock oil title | Stock oil-1 | Stock oil-2 | Stock oil-3 | Stock oil-4 |
| The source | Diesel oil 1 | |
Coking gasoline and diesel | Wax oil |
| Density (20 ℃)/gcm -3 | 0.8762 | 0.9541 | 0.8201 | 0.9126 |
| The boiling range scope, ℃ | 175～370 | 165～375 | 64～357 | 340～550 |
| Sulphur content, wt% | 2.05 | 0.78 | 0.95 | 2.74 |
| Nitrogen content, wt% | 0.06 | 0.09 | 0.07 | 0.09 |
| Cetane value | 37.1 | 19.5 | ||
| Aromaticity content, wt% | 42.3 | 75.1 | 15.9 | 52.5 |
Table 2 hydrotreatment operational condition and result
| Numbering | Embodiment 1 | |
|
Embodiment 4 |
| Stock oil | Stock oil-4 | Stock oil-4 | Stock oil-4 | Stock oil-4 |
| Catalyzer | FF-14 | FF-14 | FF-18 | FF-18 |
| Reaction pressure/MPa | 8.0 | 6.0 | 15.0 | 12.0 |
| Average reaction temperature/℃ | 370 | 360 | 365 | 350 |
| LHSV/h -1 | 1.5 | 1.2 | 0.8 | 1.8 |
| Hydrogen to oil volume ratio (v/v) | 500∶1 | 700∶1 | 1300∶1 | 800∶1 |
| The high pressure hot separator temperature, ℃ | 260 | 200 | 400 | 300 |
| The wax oil yield, wt% | 93.5 | 94.2 | 88.9 | 91.4 |
| Sulphur content/μ gg -1 | 2000 | 3000 | 300 | 800 |
Table 3 hydro-upgrading operational condition and result
| Numbering | Embodiment 1 | |
|
Embodiment 4 |
| Stock oil | Stock oil-1 | Stock oil-1 | Stock oil-2 | Stock oil-3 |
| Catalyzer | FH-98/ 3963 | FC-18 | FH-98/ 3963 | FH-98/ FC-18 |
| Catalyst ratio (v/v) | 40/60 | / | 50/50 | 20/80 |
| Reaction pressure/MPa | 8.0 | 6.0 | 15.0 | 12.0 |
| Temperature of reaction/℃ | 350 | 340 | 370 | 345 |
| LHSV/h -1 | 2.0 | 1.5 | 1.5 | 3.5 |
| Hydrogen to oil volume ratio (v/v) | 300∶1 | 600∶1 | 800∶1 | 400∶1 |
| ＜145 ℃ of naphtha fractions | ||||
| Sulphur content/μ gg -1 | 65 | 50 | ＜10 | ＜1 |
| 〉=145 ℃ of diesel oil distillates | ||||
| Density (20 ℃)/gcm -3 | 0.8246 | 0.8322 | 0.8411 | 0.8182 |
| Sulphur content/μ gg -1 | ＜10 | ＜10 | ＜10 | ＜10 |
| Cetane value | 55.1 | 52.4 | 51.1 | 56.8 |
From above embodiment, can find out, the maximum characteristics of this combination process are, rationally utilize the features of hydroprocessing technique and hydrogenation modifying process, when keeping the different device desulfurization to require, owing to having adopted combination process, having greatly reduced facility investment and the process cost of device.Because two series adopt parallel-connection flow, can greatly lower the Pressure Drop of whole system simultaneously, save process cost and prolong the cycle of operation.
Claims (8)
1. hydro-upgrading combined method, raw material comprise wax oil feedstock and diesel oil distillate oil raw material, comprise the steps:
A, under the hydrotreatment operational condition, wax oil feedstock oil is through the hydrotreating catalyst bed, and the hydrotreatment reaction effluent is isolated to gas phase and liquid phase, and gas phase comprises hydrogen-rich gas, liquid phase is the hydrogenation wax oil, and the hydrogenation wax oil is as the catalytic cracking unit raw material;
B, under the hydro-upgrading operational condition, diesel oil distillate stock oil is through the catalyst for hydro-upgrading bed, the hydro-upgrading reaction effluent separates and obtains hydrogen-rich gas, petroleum naphtha and diesel oil; Hydro-upgrading adopts the catalyst for hydro-upgrading that contains modified Y molecular sieve;
The hydrogen-rich gas mixing of the hydrogen-rich gas of c, step a gas phase and step b loops back step a and step b after removing hydrogen sulfide;
Wherein the described hydrotreatment operational condition of step a is: reaction pressure 3.0～20.0MPa, hydrogen to oil volume ratio are 200: 1～2500: 1, and volume space velocity is 0.1～8.0h
-1, 260 ℃～455 ℃ of temperature of reaction;
Wherein the described hydrofining operational condition of step b is: reaction pressure 4.0MPa～18.0MPa, temperature of reaction is 260 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～6.0h
-1, hydrogen to oil volume ratio is 100: 1～2000: 1.
2. in accordance with the method for claim 1, it is characterized in that the described wax oil feedstock of step a comprises one or more in vacuum gas oil, deasphalted oil, coker gas oil, the heavy cycle oil, perhaps from coal tar or liquefied coal coil.
3. in accordance with the method for claim 1, it is characterized in that the described operational condition of step a is: reaction pressure 4.0～18.0MPa, hydrogen to oil volume ratio 300: 1～2000: 1, volume space velocity 0.2～6.0h
-1, 280～444 ℃ of temperature of reaction.
4. in accordance with the method for claim 1, it is characterized in that the described diesel oil distillate raw material of step b comprises one or more in straight-run diesel oil, coker gas oil, catalytic diesel oil, the liquefied coal coil light ends.
5. in accordance with the method for claim 4, it is characterized in that also containing straight-run spirit or coker gasoline in the described diesel oil distillate raw material.
6. in accordance with the method for claim 1, it is characterized in that in the described catalyst for hydro-upgrading that contains modified Y molecular sieve of step b, Modified Zeolite Y content is 10%～45% by weight, carrier is aluminum oxide and/or amorphous aluminum silicide, wherein Modified Zeolite Y has following character: lattice constant is 2.436～2.444nm, and infrared total acid is 0.5～1.1mmol/g.
7. in accordance with the method for claim 1, it is characterized in that the hydrogenation process of step a and step b adopts same pressure rating, use common desulphurization of recycle hydrogen system, and the common recycle hydrogen compressor.
8. in accordance with the method for claim 1, high pressure hot separator is adopted in the separation that it is characterized in that reaction effluent among the step a, the isolated gas phase of high pressure hot separator can be mixed with step b diesel oil fraction hydrogenating modification reaction effluent, isolate hydrogen-rich gas, hydrogen-rich gas further removes and uses with additional new hydrogen mixed cycle after hydrogen sulfide increases by circulating hydrogen compressor again; Perhaps step a reaction effluent adopts cold high pressure separator, and the isolated gas phase of cold high pressure separator is hydrogen-rich gas, separates the hydrogen-rich gas mixing that obtains with step b and removes hydrogen sulfide.
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102329640B (en) * | 2010-07-13 | 2014-08-20 | 中国石油化工股份有限公司 | Integrated hydrocracking method |
| CN102329639B (en) * | 2010-07-13 | 2014-07-23 | 中国石油化工股份有限公司 | Integrated hydroprocessing method |
| CN102465030B (en) * | 2010-11-05 | 2014-07-23 | 中国石油化工股份有限公司 | Hydrogenation process combination method |
| CN103074103A (en) * | 2011-10-26 | 2013-05-01 | 中国石油化工股份有限公司 | Combined hydrotreating method |
| CN103773430B (en) * | 2012-10-24 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of wax oil hydrogenation treatment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1156752A (en) * | 1995-11-22 | 1997-08-13 | 中国石油化工总公司 | Diesel oil fraction hydrogenation converting process |
| US6793804B1 (en) * | 2001-11-07 | 2004-09-21 | Uop Llc | Integrated hydrotreating process for the dual production of FCC treated feed and an ultra low sulfur diesel stream |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1156752A (en) * | 1995-11-22 | 1997-08-13 | 中国石油化工总公司 | Diesel oil fraction hydrogenation converting process |
| US6793804B1 (en) * | 2001-11-07 | 2004-09-21 | Uop Llc | Integrated hydrotreating process for the dual production of FCC treated feed and an ultra low sulfur diesel stream |
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