CN103773458B - A kind of gas phase and liquid-phase mixing hydrogenation method - Google Patents
A kind of gas phase and liquid-phase mixing hydrogenation method Download PDFInfo
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Abstract
The invention discloses the circulation of a kind of gas phase and liquid phase circulation mixed hydrogenation technological process.The method comprises, poor ignition quality fuel and hydrogen carry out gas phase adverse current hydrogenation reaction, gained liquid generates after oil mixes with straight-run diesel oil and carries out saturated molten hydrogen, then enter liquid phase ring hydrogenator to react, liquid-phase hydrogenatin effluent is divided into two portions, a part goes out device and obtains low sulfur diesel product, another part circulation back-mixing hydrogen tank.Poor ignition quality fuel is after gas phase hydrogenation reaction, and aromatic hydrocarbons is saturated, and the hydrogen-consuming volume of reaction is very low further, and saturated molten hydrogen amount improves; Its liquid phase generates in oil and also dissolves a large amount of unreacting hydrogen simultaneously, in liquid phase hydrogenation reactor, deep desulfuration reaction provides abundant dissolved hydrogen, thus is conducive to the carrying out of deep hydrodesulfurizationof reaction.Present approach provides a kind of novel method being raw material production ultra-low-sulphur diesel with poor ignition quality fuel and straight-run diesel oil.
Description
Technical field
The present invention relates to a kind of hydrocarbon hydroprocessing technique, specifically a kind of gas phase circulation hydrogenation and liquid phase circulation hydrogenation process integration technology.
Background technology
Along with the raising of people's environmental consciousness and the increasingly stringent of environmental regulation, produce and use fuel for cleaning vehicle more and more to become a kind of development trend.And cleaning for diesel oil, desulfurization and Porous deproteinized bone are the keys that it cleans.
At present, in diesel deep desulfurization technology, hydrotreating techniques remains main, be also the most effective technique means.Hydrotreating techniques is also varied, has successively occurred the Technologies such as single hop hydrogenation, single hop serial hydrogenation and two-stage hydrogenation.In addition, along with the control of refinery to cost is more and more stricter, to invest the attention that the low liquid phase circulation hydrogen addition technology for distinguishing feature is more and more subject to refinery, so-called liquid phase circulation hydrogen addition technology is compared to conventional gas-phase circulation hydrogenation technique, liquid phase circulation hydrogenation technique reactive moieties does not arrange hydrogen gas circulating system, liquid-phase product a large amount of circulation time is relied on to carry dissolved hydrogen into reactive system to the hydrogen providing fresh feed to carry out required for hydrogenation reaction, owing to eliminating circulating hydrogen compressor, reduce plant investment and process cost.But while investment reduction, because liquid phase circulation hydrogen addition technology relies on the hydrogen be dissolved in reaction feed to provide reaction, therefore, the hydrogen amount that needs that can the hydrogen dissolved in charging meet chemical reaction affects huge on the result of use of liquid phase circulation hydrogenation technique.At present, usual employing liquid phase circulation hydrogenator effluent component loops back-mixing hydrogen tank and fresh feed are dissolved hydrogen to provide and are reacted required hydrogen in mixed hydrogen tank, due to containing foreign matter contents such as higher sulphur, nitrogen and aromatic hydrocarbons in the unconventional energy resource such as the diesel oil distillate of the secondary processing diesel oil such as catalytic diesel oil, coker gas oil and shale oil, coal tar, reaction hydrogen-consuming volume is very high, therefore, the hydrogen dissolved in oil product is difficult to meet reaction needed, in traditional liquid phase circulation hydrogenation process, be difficult to process the poor ignition quality fuel that high hydrogen consumes.
US Patent No. 6123835 discloses a kind of liquid phase circulation hydrogenation method, and in the method, stock oil is dissolved with the hydrogen of high density in mixed hydrogen tank by mixing/flash distillation hydrogen, and then carries out liquid-phase hydrogenatin process.Effluent after liquid-phase hydrogenatin is divided into two portions, before part direct circulation back-mixing hydrogen tank, another part is then introduced into high-pressure separator and isolates unnecessary waste gas, and gained liquid continues to enter flashing tower and isolates waste gas, and the liquid after flash distillation obtains liquid product through air lift again.But for the poor ignition quality fuel hydrogenation that high hydrogen consumes, liquid-phase hydrogenatin Technology due to the molten hydrogen amount of reaction oil limited, be difficult on the one hand meet the hydrogen needed for catalytic diesel oil reaction, reaction effect is poor; The sulphur content that raw material is higher on the other hand causes the hydrogen sulfide of accumulation high density in liquid phase circulation hydrogenation component loops oil, and inhibit the carrying out that deep desulfuration reacts, reaction effect is poor.
Summary of the invention
For the deficiency of existing liquid phase circulation hydrogenation technique by the molten hydrogen amount restriction of reaction feed, the invention provides the circulation of a kind of gas phase and liquid phase circulation mixed hydrogenation technological process.The investment of this process unit is little, and energy consumption reduces, and may be used for producing ultra-low-sulphur diesel.
A kind of gas phase of the present invention and liquid-phase mixing hydrogenation method comprise following content:
(1) first poor ignition quality fuel raw material enters an anti-gas phase circulation hydrogenator and carries out hydrofining reaction; Described gas phase hydrogenation reaction device is gas-liquid counter current hydrogenator, and poor ignition quality fuel raw material enters reactor from reactor top, and hydrogen enters reactor from reactor lower part;
(2) the vapor phase stream effluent that step (1) obtains leaves reactor from reactor head, and gained liquid phase generates oil and leaves reactor from reactor bottom;
(3) step (2) gained liquid generates after oil mixes with straight-run diesel oil and enters mixed hydrogen tank and carry out mixed hydrogen, and the mixing oil after saturated molten hydrogen enters liquid phase hydrogenation reactor and carries out hydrofining reaction; Step (2) gained gaseous effluent can enter circulating hydrogen compressor entrance and recycle after further purifying treatment;
(4) step (3) obtain hydrogenation reaction effluent a part through reducing valve decompression after bleeder, obtain ultra-low-sulphur diesel; Another part circulation back-mixing hydrogen tank mixes hydrogen.
In Unionfining technological process of the present invention, the described poor ignition quality fuel raw material of step (1) generally includes one or more in catalytic cracking diesel oil, coker gas oil, coal tar diesel oil and shale diesel oil.Straight-run diesel oil described in step (3) is conventional straight-run diesel oil raw material in the art, and it is done and is generally no more than 385 DEG C, is generally 330 DEG C ~ 370 DEG C.In step (3), described step (2) gained liquid generates oil and is generally 1:5 ~ 5:1, preferred 1:3 ~ 3:1 with the ratio of straight-run diesel oil.
One anti-gas phase circulation hydrogenator generally reacts under the temperature of reaction comparatively relaxed, low-speed and higher pressure, and two anti-liquid phase circulation hydrogenators are then at high temperature, high-speed and low pressing operation.High temperature described herein, low temperature, high-speed, low-speed and high pressure and low pressure are relative.
According to gas phase hydrogenation of the present invention and liquid-phase hydrogenatin Unionfining technological process, the catalyzer loaded in gas phase hydrogenation reaction device and liquid phase hydrogenation reactor can be identical catalyzer, also can load different catalyzer.In the inventive method, the catalyzer that in an anti-gas phase circulation hydrogenator, preferably filling hydrogenation capability is stronger, as an anti-Hydrobon catalyst can be selected with W-Ni or Mo-Ni for active metal, this catalyzer has stronger hydrotreated lube base oil ability.Two anticatalyzers preferred Mo-Co type Hydrobon catalyst, two anti-interior chemical reactions are based on hydrodesulfurization reaction, and chemical hydrogen consumption amount is lower.
Gas phase hydrogenation of the present invention and liquid-phase hydrogenatin Unionfining technological process, the operational condition of the gas-liquid counter current hydrogenator in step (1) is as follows: average reaction temperature 280 DEG C ~ 380 DEG C, preferably 300 DEG C ~ 340 DEG C; Reaction pressure 4.0 MPa ~ 15.0 MPa, preferably 6.0 MPa ~ 10.0MPa; Volume space velocity 0.2h during liquid
-1~ 3h
-1, preferred 0.5h
-1~ 1.5h
-1, hydrogen to oil volume ratio 80 ~ 800, preferably 100 ~ 300.
The operational condition of the liquid phase circulation hydrogenator in step (3) is as follows: average reaction temperature 320 DEG C ~ 400 DEG C, preferably 340 DEG C ~ 380 DEG C; Reaction pressure 3.0 MPa ~ 10.0 MPa, preferably 4.0 MPa ~ 8.0MPa; Volume space velocity 2.0h during liquid
-1~ 8.0h
-1, preferred 3.0h
-1~ 6.0h
-1; Liquid phase circulation ratio (i.e. liquid-phase hydrogenatin treated oil turning oil/straight-run diesel oil mass ratio) is 1:5 ~ 5:1, preferential 1:2 ~ 3:1.
In present invention process method, step (1) and the middle Hydrobon catalyst used of step (3) can use commercially available prod as required, also can prepare by this area Conventional wisdom.Wherein step (1) gas phase hydrogenation reaction device inner catalyst is preferably W-Ni type or Mo-Ni type catalyzer, and catalyst hydrogenation saturability is stronger.The catalyzer wherein used in step (3) liquid phase hydrogenation reactor is preferably Mo-Co type catalyzer, and it is active that this catalyzer has higher direct desulfurization under high-speed.Wherein said Mo-Co type catalyzer with Mo, Co metal for active ingredient, with aluminum oxide or silicon-containing alumina for carrier; Described Mo-Ni or W-Ni type catalyzer with Mo, Ni or W, Ni metal for active ingredient, with aluminum oxide or silicon-containing alumina for carrier.Consisting of of described Mo-Co type catalyzer, Mo-Ni or W-Ni type catalyzer: with the weight of catalyzer for benchmark, tungsten or molybdenum with oxide basis content for 8wt% ~ 28wt%, cobalt or nickel with oxide basis content for 2wt% ~ 15wt%; The specific surface area of catalyzer is generally 100 ~ 650m
2/ g, pore volume is generally 0.15 ~ 0.8mL/g.
Compared with prior art, gas phase hydrogenation of the present invention and liquid-phase hydrogenatin Unionfining technological process have following characteristics:
The present invention fully takes into account the features of gas phase circulation hydrogenation technique and liquid phase circulation hydrogenation technique, reasonably two kinds of techniques are combined effectively: first the inferior feedstock oils such as coker gas oil, catalytic diesel oil, shale diesel oil, coal tar diesel oil distillate enter gas phase circulation hydrogenator and carry out hydrofining reaction, dose stronger W-Ni or the Mo-Ni type catalyzer of hydrogen saturability this reactor is in-built, and coordinate suitable operational condition to reach the objects such as deep hydrogenation denitrogenation, Tuo Fang and deoxidation.Meanwhile, part eliminates space steric effect containing sterically hindered sulfide after aromatic saturation, is conducive to it and carries out deep desulfuration further in two anti-liquid phase hydrogenation reactors.Gas-liquid counter current hydrogenation gained generates oil and straight-run diesel oil and is mixed into enter in liquid phase hydrogenation reactor after mixed hydrogen tank mixes and carries out deep desulfuration reaction.Due to after an anti-gas phase circulation hydrogenator reaction, the aromatic hydrocarbons in poor-quality diesel-oil by cut fraction is by fully saturated, and its hydrogen-consuming volume reacted further is very low, and saturated molten hydrogen amount also increases.Simultaneously, a large amount of unreacting hydrogens has been dissolved in one anti-reaction effluent, can be deep desulfuration reaction hydrogen supply in liquid phase hydrogenation reactor on the one hand, foreign matter content on the other hand after refining in poor ignition quality fuel significantly reduces, also optimize two anti-reaction feed character, be beneficial to the carrying out of two anti-deep desulfuration reactions.Two anti-chargings are the mixing oil of treated oil, straight-run diesel oil and turning oil after an anti-hydrogenation, reaction feed hydrogen-consuming volume is low, material dissolution hydrogen is utilized to react with liquid phase circulation hydrogenation reaction, and hydrogen meltage limited response hydrogen consumption should not be excessive feature adapt, be conducive to the effective use of liquid phase hydrogenation reactor.In addition, the hydrogen sulfide that one anti-gas-liquid counter current hydrogenation process generates is taken away by the hydrogen at upper reaches, decrease one and instead generate the hydrogen sulfide accumulation caused after oil enters Liquid-phase reactor, thus slow down the restraining effect that in liquid phase hydrogenation reactor, hydrogen sulfide reacts deep desulfuration, be conducive to the carrying out of deep desulfuration reaction equally.Filling Mo-Co type height hydrodesulfurization activity catalyzer in liquid phase circulation hydrogenator, carries out deep desulfuration reaction, thus finally obtains ultra-low-sulphur diesel under the reaction conditions of high-speed and high temperature.
Accompanying drawing explanation
Fig. 1 is the principle process schematic diagram of diesel hydrogenation process of the present invention.
Embodiment
Below in conjunction with Fig. 1, diesel hydrogenation method of the present invention is described in detail.
As shown in Figure 1, hydrogen and poor-quality diesel-oil by cut fraction stock oil are respectively via pipeline 1 and through pipeline 2, enter countercurrent hydrogenation reactor 3 with the gas-liquid counter current way of contact and carry out hydrofining reaction, countercurrent hydrogenation reactor 3 gained gaseous effluent leaves reactor through pipeline 5, recycle hydrogen can be used as use after processing further, gained liquid generates oil through pipeline 4, after mixing with the turning oil of the straight-run diesel oil introduced through pipeline 6 and pipeline 11, enter mixed hydrogen tank 7 to carry out mixing molten hydrogen together with the hydrogen introduced through pipeline 8, mixing oil after saturated molten hydrogen can after excess hydrogen be discharged by pipeline 9, enter liquid phase hydrogenation reactor 10 and carry out hydrofining reaction, part reaction effluent can as diesel product through pipeline 12 bleeder after reducing valve decompression, another part reaction effluent then returns mixed hydrogen tank 7 through pipeline 11.
Below by specific embodiment, technical scheme of the present invention and effect are described.
Embodiment 1 ~ 4
Embodiment 1 ~ 4 adopts the flow process shown in Fig. 1 of the present invention.Use the composition of catalyzer and character in table 1 in following examples.One anti-gas phase hydrogenation device is raw materials used for table 2 Raw is according to the stock oil of urging bavin/burnt bavin=60/40 ratio mixing, and the straight-run diesel oil feed properties of two anti-liquid-phase hydrogenatin devices is as shown in table 3.Wherein the ratio of straight-run diesel oil and an anti-high score effluent oil is 1:1, and embodiment 1 ~ 4 processing condition used list in table 4.The evaluation result of embodiment 1 ~ 4 is in table 5.
The composition of table 1 embodiment used catalyst and main character.
| Project | One anti-finishing agent | Two anti-finishing agents |
| Chemical constitution, wt% | ||
| MoO 3 | 20.3 | 18.2 |
| NiO | 6.2 | — |
| CoO | — | 6.5 |
| Carrier | Silicon-containing alumina | Silicon-containing alumina |
Table 2 stock oil character.
| Project | Catalytic diesel oil | Coker gas oil | Mixing raw material oil |
| Density (20 DEG C), g/cm 3 | 0.9308 | 0.8502 | 0.8905 |
| Boiling range, DEG C | 190～360 | 185～370 | 185～370 |
| Sulphur content, μ g/g | 12000 | 9000 | 10500 |
| Nitrogen content, μ g/g | 700 | 1000 | 850 |
| Aromaticity content, wt% | 70 | 30 | 50 |
The anti-straight-run diesel oil charging of table 3 two.
| Project | Straight-run diesel oil |
| Density (20 DEG C), g/cm 3 | 0.8308 |
| Boiling range, DEG C | 170～340 |
| Sulphur content, μ g/g | 3000 |
| Nitrogen content, μ g/g | 50 |
Table 4 embodiment operational condition.
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| One is anti- | ||||
| Temperature of reaction, DEG C | 300 | 320 | 320 | 300 |
| Reaction pressure, MPa | 6.0 | 6.0 | 8.0 | 8.0 |
| Volume space velocity, h -1 | 0.5 | 1.0 | 0.8 | 1.2 |
| Hydrogen to oil volume ratio | 200 | 200 | 300 | 300 |
| Two is anti- | ||||
| Temperature of reaction, DEG C | 360 | 360 | 370 | 370 |
| Reaction pressure, MPa | 6.0 | 6.0 | 4.0 | 4.0 |
| Volume space velocity, h -1 | 4.0 | 4.0 | 6.0 | 6.0 |
| Liquid phase circulation ratio | 1：2 | 1：2 | 1：1 | 1：1 |
Table 5 embodiment 1 ~ 4 evaluation result
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Sulphur content, μ g/g | 9 | 11 | 5 | 7 |
| Nitrogen content, μ g/g | <1 | <1 | <1 | <1 |
Claims (7)
1. gas phase and a liquid-phase mixing hydrogenation method, comprises following content:
(1) first poor ignition quality fuel raw material enters an anti-gas phase circulation hydrogenator and carries out hydrofining reaction; Described gas phase circulation hydrogenator is gas-liquid counter current hydrogenator; The average reaction temperature of described gas phase circulation hydrogenator is 280 DEG C ~ 340 DEG C;
(2) the vapor phase stream effluent that step (1) obtains leaves reactor from reactor head, and gained liquid generates oil and leaves reactor from reactor bottom;
(3) step (2) gained liquid generates after oil mixes with straight-run diesel oil and enters mixed hydrogen tank and carry out mixed hydrogen, and the mixing oil after saturated molten hydrogen enters liquid phase circulation hydrogenator and carries out hydrofining reaction; The average reaction temperature of liquid phase circulation hydrogenator is 340 DEG C ~ 400 DEG C; Doing of described straight-run diesel oil is 330 DEG C ~ 370 DEG C; It is 1:5 ~ 5:1 that described liquid generates oil with the ratio of straight-run diesel oil;
(4) step (3) obtain hydrogenation reaction effluent a part through reducing valve decompression after bleeder, obtain ultra-low-sulphur diesel; Another part circulation back-mixing hydrogen tank mixes hydrogen.
2. in accordance with the method for claim 1, it is characterized in that, the described poor ignition quality fuel raw material of step (1) comprises one or more in catalytic cracking diesel oil, coker gas oil, coal tar diesel oil distillate or shale diesel oil.
3. in accordance with the method for claim 1, it is characterized in that, in step (1), the operational condition of gas-liquid counter current hydrogenator is as follows: reaction pressure 4.0 MPa ~ 15.0 MPa, volume space velocity 0.2h during liquid
-1~ 3h
-1, hydrogen to oil volume ratio 80 ~ 800.
4. in accordance with the method for claim 1, it is characterized in that, in step (3), the operational condition of liquid phase circulation hydrogenator is as follows: reaction pressure 3.0 MPa ~ 10.0 MPa, volume space velocity 2.0h during liquid
-1~ 8.0h
-1, liquid phase circulation is than being 1:5 ~ 5:1.
5. in accordance with the method for claim 1, it is characterized in that, the catalyzer in step (1) gas phase circulation hydrogenator is W-Ni type or Mo-Ni type catalyzer, and the catalyzer used in step (3) liquid phase circulation hydrogenator is Mo-Co type catalyzer.
6. in accordance with the method for claim 5, it is characterized in that, consisting of of described Mo-Ni type or W-Ni type catalyzer: with the weight of catalyzer for benchmark, molybdenum or tungsten with oxide basis content for 8wt% ~ 28wt%, nickel with oxide basis content for 2wt% ~ 15wt%.
7. in accordance with the method for claim 5, it is characterized in that, consisting of of described Mo-Co type catalyzer: with the weight of catalyzer for benchmark, molybdenum with oxide basis content for 8wt% ~ 28wt%, cobalt with oxide basis content for 2wt% ~ 15wt%.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5252198A (en) * | 1989-05-10 | 1993-10-12 | Davy Mckee (London) Ltd. | Multi-step hydrodesulphurisation process |
| CN101942327A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Hydrotreatment combination technology for producing ultra low sulfur diesel |
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2012
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5252198A (en) * | 1989-05-10 | 1993-10-12 | Davy Mckee (London) Ltd. | Multi-step hydrodesulphurisation process |
| CN101942327A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Hydrotreatment combination technology for producing ultra low sulfur diesel |
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