CN105542843A - Boiling bed residue oil hydrogenation method - Google Patents
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Abstract
The invention relates to a boiling bed residue oil hydrogenation method, which comprises that a residue oil raw material enters a boiling bed hydrogenation reactor, hydrogen gas is subjected to a hydrogenation reaction under the effect of a boiling bed hydrogenation catalyst to obtain hydrogenation generation oil, the obtained hydrogenation generation oil is subjected to gas liquid separation in a high-pressure separator, and the liquid phase separated by the high-pressure separator is subjected to fractionation in a fractionation tower to obtain gas, a naphtha distillate, a diesel oil distillate and a hydrogenation normal pressure residue oil. According to the present invention, the poor-quality residue oil raw material can be subjected to the hydrogenation reaction so as to remove most of sulfur, metals and other impurities in the raw material and substantially reduce the residual carbon value, and the obtained hydrogenation normal pressure residue oil can be adopted the catalytic cracking raw material so as to improve the poor-quality raw material oil utilization rate.
Description
Technical field
The present invention relates to a kind of employing boiling bed hydrogenation method, more particularly, is a kind of method that boiling bed residual oil hydrogenation produces catalytically cracked material.
Background technology
The efficiency utilization of heavy oil and clean processing are just becoming the staple of conversation that global Oil Refining Industry is paid close attention to.The technique such as coking, solvent deasphalting, because there being the generation of a large amount of low value by-product, affects utilising efficiency and the economic benefit of residual oil.Residual hydrogenation can meet heavy oil efficiency utilization simultaneously and meet environmental requirement.Residual hydrogenation has developed four kinds of technology types: fixed bed, ebullated bed, slurry bubble bed and moving-bed.In four kinds of technology types, fixed-bed process is ripe, and easy to operate, plant investment is relatively low; Hydrogenated residue can be used as RFCC charging.But the fixed bed operation cycle is larger by raw material impurity content influence, for the raw material that Ni, V metal content is very high, in hydrogenation process, metal can be deposited in catalyzer micropore, blocking catalyst micropore, cause catalyst deactivation, have a strong impact on the residual hydrogenation equipment operational cycle; For the calcium metal in raw material, the raw material that iron etc. are too high, calcium, iron are easy to be deposited in the space between the surface of catalyzer and granules of catalyst, blocking catalyst aperture, cause catalyst deactivation, and cause pressure drop of column to raise fast, the operational cycle is shorter.Along with crude oil heaviness, in poor quality, increasing residual oil has been unsuitable for processing via fixed bed residual hydrocracking.
The problem that the operational cycle that the pressure drop rise that can overcome boiling bed hydrogenation technique causes is too short.In ebullated bed reactor, catalyzer is boiling state, therefore there is not the problem of pressure drop rise.Simultaneously because catalyzer can draw off online and add, therefore can keep steady state, high metal content residual oil can be processed.
To boiling bed hydrogenation technique, boiling bed hydrogenation reactor be enable in the core of boiling bed hydrogenation, particularly reactor oil circulate to strengthen oil in reactor on flow be the key making catalyzer keep boiling state.In current increasing boiling bed hydrogenation reactor, the technology of the flow of oil has following several types: a kind of is utilize recycle pump to provide power to realize the circulation of oil in reactor, strengthens the flow of oily upward direction in reactor.Another utilizes outer jet pump to realize oil to come back to reactor and strengthen oil flow upwards in the reactor.
US Patent No. 3414386 describes and be provided with recycle pump bottom inside reactor, by reactor top, oil is directed to pump, then provide pressure head to make oil more upwards by distributing disc by pump, enable oil at reactor internal recycle, make catalyzer keep boiling fluidized state; But this technology has critical defect, once the recycle pump being in inside reactor has been broken, must stop work and open reactor and could keep in repair after drawing off catalyzer, idle cost is huge.
US Patent No. 5360535 proposes the circulation utilizing outer jet pump to realize oil, utilizes static equipment to replace dynamic equipment.Method is the high pressure facility arranging a squirt pump outside reactor, reactor effluent order enters the first high-pressure separator and the second high-pressure separator, oil is extracted out as injector power oil by high-pressure pump bottom the second high-pressure separator, the oils stream one of 1 ~ 10 times promoting to draw bottom the first high-pressure separator plays reactor bottom, together with fresh feed and hydrogen by distributing disc upwards, catalyst in reactor is made to keep boiling state.But the method still needs to build the squirt pump equipment of a set of external high pressure and high-pressure pump and needs more high pressure line and more tightness system, increases high-tension apparatus and investment.
Summary of the invention
The object of the invention is to overcome in existing boiling bed residual oil method of hydrotreating, working method is complicated, and the defect that facility investment is high, provides a kind of new boiling bed residual oil method of hydrotreating.
The invention provides a kind of boiling bed residual oil method of hydrotreating, comprise, residual oil raw material enters boiling bed hydrogenation reactor and hydrogen carries out hydrogenation reaction under the effect of boiling bed hydrogenation catalyst, obtain hydrogenated oil, gained hydrogenated oil carries out gas-liquid separation in high-pressure separator, and the fractionation in separation column of the high-pressure separator isolated liquid phase of institute is gas, naphtha fraction, diesel oil distillate and hydrogenation long residuum;
Described boiling bed hydrogenation reactor, there is reactor cylinder shape housing 1, upper cover and lower cover, gas-liquid separator 3 is set gradually in reactor, vertical oil guide pipe 4 and distributing disc 9, at reactor upper cover, place arranges oil gas vent 2, the entrance of high pressure oil guide pipe 5, the entrance of hydrogen feed tube 10 is set at reactor lower cover place, in reactor, the lower end of gas-liquid separator 3 is connected with the entrance of vertical oil guide pipe 4, the bottom of vertical oil guide pipe 4 is connected with distributing disc 9, the exit of vertical oil guide pipe 4 is positioned at the below of distributing disc 9, on reactor top, high pressure oil guide pipe 5 is set, the exit end of its mesohigh oil guide pipe 5 is positioned at vertical oil guide pipe 4, the distance in axial direction of high pressure oil guide pipe 5 exit end and vertical oil guide pipe 4 inlet end and the ratio of vertical oil guide pipe 4 length are 0.1 ~ 8:10.
Method provided by the present invention, can process residual oil raw material inferior, be stripped of most sulphur, the metal impurities in raw material, carbon residue significantly reduces, and gained hydrogenation long residuum can be used as catalytically cracked material, improves inferior feedstock oil utilization ratio.In boiling bed hydrogenation method provided by the present invention, driving oil higher than reactor pressure is injected in vertical oil guide pipe by high pressure oil guide pipe, by forming oil stream at a high speed during ejection, drive the circulation of more substantial liquid in reactor, thus promotion catalyzer, and maintain catalyzer and be in ebullated bed state.Compared with the existing ebullated bed reactor with internal circulation pump, outer circulation pump, the boiling bed hydrogenation structure of reactor in method of hydrotreating of the present invention is simple, is convenient to realize internal recycle, and eliminates dynamic equipment, save investment cost and process cost.
Accompanying drawing explanation
Fig. 1 is boiling bed hydrogenation structure of reactor schematic diagram in method of hydrotreating provided by the invention.
Accompanying drawing illustrates:
1-reactor cylinder shape housing, 2-oil gas vent, 3-gas-liquid separator, 4-vertically oil guide pipe, 5-high pressure oil guide pipe, the diameter shrinkage part of 6-high pressure oil guide pipe exit end, 7-catalyst charge pipe, 8-catalyzer downstream line, 9-distributing disc, 10-hydrogen feed tube.
Embodiment
Below in conjunction with drawings and Examples, the present invention is described, for purposes of clarity, accompanying drawing and eliminate expression and the description of unrelated to the invention, parts known to persons of ordinary skill in the art and process in illustrating.
Residual oil raw material enters boiling bed hydrogenation reactor after heat exchange and process furnace heating, and hydrogen also enters this boiling bed hydrogenation reactor after heat exchange or heating; Under the effect of boiling bed hydrogenation catalyst, residual oil crude oil carries out hydrogenation reaction, remove sulphur, metal, the bituminous matter of the overwhelming majority, the carbon residue of residual oil raw material also significantly reduces simultaneously, after gained hydrogenated oil is extracted out from boiling bed hydrogenation reactor, gas-liquid separation is carried out through high-pressure separator, the separating obtained circulation gas being rich in hydrogen returns boiling bed hydrogenation reactor after circulator compresses and after mixing with new hydrogen to be continued to use, and the fractionation in separation column of the high-pressure separator isolated liquid phase of institute is gas, naphtha fraction, diesel oil distillate and hydrogenation long residuum.
The structure of the boiling bed hydrogenation reactor that the present invention adopts as shown in Figure 1, has reactor cylinder shape housing 1, upper cover and lower cover.The aspect ratio of described reactor cylinder shape housing is 0.8:1 ~ 100:1.Gas-liquid separator 3, vertically oil guide pipe 4 and distributing disc 9 is set gradually in boiling bed hydrogenation reactor.The lower end of described gas-liquid separator 3 is connected with the entrance of vertical oil guide pipe 4, the bottom of vertical oil guide pipe 4 is connected with distributing disc 9, the exit of vertical oil guide pipe 4 is positioned at the below of distributing disc 9, and described reactor cylinder shape housing 1, gas-liquid separator 3, vertical oil guide pipe 4 and distributing disc 9 are coaxial each other.
The entrance of oil gas vent 2 and high pressure oil guide pipe 5 is set at boiling bed hydrogenation reactor upper cover place, the entrance of hydrogen feed tube 10 is set at reactor lower cover place.Described hydrogen feed tube 10 enters reactor by reactor lower cover, is positioned at the below of distributing disc 9.
In boiling bed hydrogenation reactor, on reactor top, high pressure oil guide pipe 5 is set, the exit end of its mesohigh oil guide pipe 5 is positioned at vertical oil guide pipe 4, and straight down, and high pressure oil guide pipe 5 exit end is coaxial each other with vertical oil guide pipe 4 in the direction of described high pressure oil guide pipe 5 exit end.The ratio of high pressure oil guide pipe 5 exit end and vertical oil guide pipe 4 inlet end distance in axial direction and vertical oil guide pipe 4 length is 0.1 ~ 2:10.
The exit end of described high pressure oil guide pipe 5 is positioned at vertical oil guide pipe 4, and the distance radially of high pressure oil guide pipe 5 exit end outer wall and vertical oil guide pipe 4 inwall and the ratio of vertical oil guide pipe 4 internal diameter are 0.05 ~ 0.5:1.
Described high pressure oil guide pipe 5 has well-balanced wall thickness, preferably arranges diameter shrinkage part 6 in the exit of high pressure oil guide pipe 5, and the internal diameter of described diameter shrinkage part 6 reduces gradually along the axis of high pressure oil guide pipe 5, and minimum at the internal diameter of the exit end of high pressure oil guide pipe 5.Described diameter shrinkage part 6 is coaxial each other with vertical oil guide pipe 4.
The maximum inner diameter of diameter shrinkage part 6 and the ratio of minimum diameter in described high pressure oil guide pipe 5 exit are 20 ~ 2:1.
The maximum inner diameter part of the diameter shrinkage part 6 in described high pressure oil guide pipe 5 exit is positioned at vertical oil guide pipe 4, and the ratio of the outer wall of its correspondence and the distance radially of vertical oil guide pipe 4 inwall and vertical oil guide pipe 4 internal diameter is 0.05 ~ 0.5:1.
In this ebullated bed reactor, drive the pressure of oil higher than reactor internal pressure in high pressure oil guide pipe 5, when driving oil in high pressure oil guide pipe 5 flows out from exit (or diameter shrinkage part 6), pressure is converted into kinetic energy, make to drive oil to flow downward along vertical oil guide pipe 4 with speed faster, and the gap location between the exit end of diameter shrinkage part 6 and the inwall of vertical oil guide pipe 4, form the region that a pressure is relatively low, and therefore flow to this gap place after attracting the oil on gas-liquid separator 3 top in reactor to enter vertical oil guide pipe 4, and under the drive of the driving oil stream of diameter shrinkage part 6 exit end ejection, flow downward along vertical oil guide pipe 4 together.From high pressure oil guide pipe 5 and through diameter shrinkage part 6 the driving oil sprayed and the oil mixing coming gas-liquid separator 3 top in autoreactor, and turn back upwards after vertical oil guide pipe 4 arrives reactor bottom together, after mixing with the hydrogen from hydrogen feed tube 10, and continue upwards to flow by distributing disc 9.The gas-liquid of inside reactor promotes to make catalyzer be boiling state, can control suitable process conditions and make the charge level of catalyzer in boiling bed hydrogenation reactor raise and maintain certain height.
When boiling bed hydrogenation reactor carries out hydrogenation reaction, for convenience of in process of production can more catalyst changeout online, arrange catalyst addition tube 7 on the top of described boiling bed hydrogenation reactor, described catalyst addition tube 7 is through gas-liquid distributor 3, and its outlet is positioned at the below of gas-liquid separator 3.The bottom of boiling bed hydrogenation reactor arranges catalyzer downstream line 8, and described catalyzer downstream line 8 is through distributing disc 9, and its entrance is positioned at the top of distributing disc 9.Catalyst addition tube 7 and catalyzer downstream line 8 make reactor to carry out catalyst replacement by adding online and drawing off catalyzer and need not stop work in normal production, keep monolith activity stabilized.If do not need the displacement catalyzer when operating, catalyst addition tube 7 and catalyzer downstream line 8 also can be saved.
Pressure height 0.5-10MPa in pressure ratio reactor in described high pressure oil guide pipe 5.
In the preferred embodiment of the present invention, the hydrogenation long residuum component loops of gained returns boiling bed hydrogenation reactor, carries out hydrogenation reaction again together with residual oil raw material.
The present invention another preferred embodiment in, the hydrogenation long residuum part of gained carries out underpressure distillation, gained hydrogenation decompressed wax oil together with remainder hydrogenation long residuum as catalytically cracked material; Underpressure distillation gained hydrogenation vacuum residuum loops back boiling bed hydrogenation reactor, carries out hydrogenation reaction again together with residual oil raw material.
The reaction conditions of boiling bed residual oil hydrogenation of the present invention is: hydrogen dividing potential drop 2.0 ~ 22.0MPa, temperature of reaction 300 ~ 450 DEG C, volume space velocity 0.1 ~ 5.0 hour
-1, hydrogen to oil volume ratio 100 ~ 2000Nm
3/ m
3.
Described boiling bed hydrogenation catalyst take porous inorganic oxide as carrier, one or more the catalyzer being active ingredient with one or more the oxide compound in group VIB and/or group VIII metal.Other various auxiliary agent is optionally added as P, Si, F and B in described catalyzer.
In described support selected from alumina, silicon-dioxide, amorphous aluminum silicide or zeolite any one or appoint several.The combination of the preferred nickel-tungsten of metallic element of described active constituent, nickel-tungsten-cobalt, nickel-molybdenum, cobalt-molybdenum or nickel-cobalt-molybdenum.
Residual oil raw material of the present invention is one or more in the secondary processing distillate of oil at the bottom of heavy crude, acid-containing raw oil, long residuum, normal pressure wax oil, vacuum residuum, wax tailings, tank, shale oil, coal direct liquefaction oil, deasphalted oil, viscous crude, hydrocracking tail oil and hydrocracking tail oil.
The present invention can allow the residual oil raw material of high metal or the residual oil raw material of high calcium content carry out hydrogenation reaction, be stripped of most sulphur, the metal impurities in raw material, carbon residue significantly reduces, and gained hydrogenation long residuum can be used as catalytically cracked material, improves inferior feedstock oil utilization ratio.
One of advantage of ebullated bed reactor described in method of hydrotreating of the present invention is with oil when the spray formation at a high speed oil stream of less pressure higher than reactor pressure, more substantial oil is driven to realize the circulation of oil in reactor, promote catalyzer and maintain catalyst bubbling bed state, be static equipment, structure is simple, and reliability is high.
Two of advantage allly makes catalyzer be in ebullated bed status component to be all positioned at reactor, and form an Open architecture, do not need sealing, do not need to bear high pressure, reduce investment outlay.
Be below for better describing embodiment provided by the present invention, but do not limit the present invention because of following embodiment.
Embodiment 1
Feed residue F1 is a kind of long residuum of high Ca content, and its character is in table 1.Structure ebullated bed reactor is as shown in Figure 1 adopted to carry out hydrogenation reaction.Wherein, the exit of high pressure oil guide pipe 5 arranges diameter shrinkage part 6, and the maximum inner diameter of diameter shrinkage part 6 and the ratio of minimum diameter are 7:1.The maximum inner diameter part of diameter shrinkage part 6 is positioned at vertical oil guide pipe 4, and the ratio of the outer wall of its correspondence and the distance radially of vertical oil guide pipe 4 inwall and vertical oil guide pipe 4 internal diameter is 0.2:1.The ratio of high pressure oil guide pipe 5 exit end and vertical oil guide pipe 4 inlet end distance in axial direction and vertical oil guide pipe 4 length is 1:10.
Boiling bed hydrogenation catalyst is the RMS-30 that development Sinopec catalyzer Chang Ling branch office of Research Institute of Petro-Chemical Engineering produces, and makes the cylindrical shape of diameter 0.8mm for adapting to boiling bed hydrogenation reactor catalyst.RMS-30 catalyzer 1.5 liters is encased in boiling bed hydrogenation reactor, and catalyzer charge level height is 50% of ebullated bed reactor height.
In boiling bed hydrogenation reactor, pass into residual oil raw material by high pressure oil guide pipe 5, and in reactor, pass into hydrogen by hydrogen feed tube 10.The residual oil flow that passes into is 500g/h, and namely residual oil volume space velocity is 0.5h relative to catalyst loading volume
-1, hydrogen flowing quantity is 165L/h under standard state.All the other operational conditions are the pressure in high pressure oil guide pipe 5 is 19.8MPa, reactor pressure is 15.0MPa, temperature of reaction 400 DEG C, driving oil in high pressure oil guide pipe 5 is sentenced at outlet diameter shrinkage part and is flowed out at a high speed, the more oil on gas-liquid separator 3 top is driven to turn back upwards after vertical oil guide pipe 4 times to reactor bottom, mix merga pass distributing disc 9 upwards with hydrogen, promote catalyzer and make catalyzer be boiling state.Measure the charge level of catalyzer in boiling bed hydrogenation reactor by radiometry method, catalyzer charge level height is 1.25 times of loading height, and catalyzer rate of expansion is 25%.
Generation oil after hydrogenation reaction carries out being separated and fractionation, obtains gas, naphtha fraction, diesel oil distillate and hydrogenation long residuum.Product slates is in table 2, and hydrogenation long residuum character is in table 3.
The sulphur of hydrogenation long residuum product, acid number, metal and carbon residue content comparatively Feedstock Atmospheric residual oil significantly degree of falling as seen from Table 3, can be used as qualified catalytically cracked material and enters catalytic cracking unit processing.
Table 1
| Project | F1 |
| Density (20 DEG C), g/cm 3 | 0.9613 |
| Carbon residue content, % by weight | 11.0 |
| Constituent content, % by weight | |
| Sulphur | 2.2 |
| Nitrogen | 0.48 |
| Metal content, μ g/g | |
| Nickel | 47.6 |
| Vanadium | 5.1 |
| Iron | 18.6 |
| Calcium | 42.0 |
| Sodium | 5.1 |
Table 2
| Project | Yield, % by weight |
| H 2S+NH 3 | 2.0 |
| C1～C4 | 1.9 |
| Naphtha fraction | 2.0 |
| Diesel oil distillate | 11.1 |
| Hydrogenation long residuum | 83.0 |
Table 3
| Project | |
| Density (20 DEG C), g/cm 3 | 0.9350 |
| Carbon residue content, % by weight | 6.0 |
| Constituent content, % by weight | |
| Sulphur, % by weight | 0.48 |
| Nitrogen, % by weight | 0.34 |
| Nickel+vanadium, μ g/g | 18 |
Embodiment 2
Feed residue F2 is a kind of long residuum of high Ni, V content, and its character is in table 4.Structure ebullated bed reactor is as shown in Figure 1 adopted to carry out hydrogenation reaction.Catalyzer is the RDM-33 that development Sinopec catalyzer Chang Ling branch office of Research Institute of Petro-Chemical Engineering produces, and makes the cylindrical shape of diameter 0.7mm for adapting to boiling bed hydrogenation reactor catalyst.RDM-33 catalyzer 1.5 liters is encased in boiling bed hydrogenation reactor, and catalyzer charge level height is 50% of ebullated bed reactor height.
In boiling bed hydrogenation reactor, pass into residual oil raw material and fractionating system by high pressure oil guide pipe 5 to circulate the hydrogenation vacuum residuum of coming, pass into residual oil raw material flow be 400g/h, hydrogenation vacuum residuum flow is 160g/h, and in reactor, passes into hydrogen by hydrogen feed tube 10.Hydrogen flowing quantity is 170L/h under standard state.All the other operational conditions are the pressure in high pressure oil guide pipe 5 is 19.0MPa, reactor pressure is 14.5MPa, temperature of reaction 410 DEG C, oil in high pressure oil guide pipe 5 is sentenced at outlet diameter shrinkage part and is flowed out at a high speed, the more oil on gas-liquid separator 3 top is driven to turn back upwards after vertical oil guide pipe 4 times to reactor bottom, mix merga pass distributing disc 9 upwards with hydrogen, promote catalyzer and make catalyzer be boiling state.Measure the charge level of catalyzer in boiling bed hydrogenation reactor by radiometry method, catalyzer charge level height is 1.26 times of loading height, and catalyzer rate of expansion is 26%.
Gained hydrogenated oil carries out being separated and fractionation, obtains gas, naphtha fraction, diesel oil distillate, hydrogenation long residuum; A part for gained hydrogenation long residuum carries out underpressure distillation, and gained hydrogenation vacuum residuum loops back feed circuit, and residual oil raw material mixes and carries out hydrogenation reaction into boiling bed hydrogenation reactor.Underpressure distillation gained hydrogenation wax oil product and do not carry out underpressure distillation hydrogenation long residuum mixing as catalytically cracked material.Product yield is in table 5, and catalytically cracked material character is in table 6.The sulphur of catalytically cracked material, acid number, metal and carbon residue content comparatively Feedstock Atmospheric residual oil significantly degree of falling as seen from Table 6, can enter catalytic cracking unit processing separately or as catalytic cracking blended feedstock.
Table 4
| Stock oil | F2 |
| Density (20 DEG C), g/cm 3 | 0.9625 |
| Carbon residue content, % by weight | 10.6 |
| Constituent content, % by weight | |
| Sulphur | 3.1 |
| Nitrogen | 0.43 |
| Metal content, μ g/g | |
| Nickel | 50.5 |
| Vanadium | 151 |
Table 5
| Project | Yield, % by weight |
| H 2S+NH 3 | 3 |
| C1～C4 | 2.2 |
| Petroleum naphtha | 2.2 |
| Diesel oil | 12.7 |
| Catalytically cracked material | 79.9 |
Table 6
| Project | |
| Density (20 DEG C), g/cm 3 | 0.9295 |
| Carbon residue content, % by weight | 5.4 |
| Sulphur, % by weight | 0.55 |
| Nitrogen, % by weight | 0.30 |
| Nickel+vanadium, μ g/g | 30 |
Claims (17)
1. a boiling bed residual oil method of hydrotreating, residual oil raw material enters boiling bed hydrogenation reactor and hydrogen carries out hydrogenation reaction under the effect of boiling bed hydrogenation catalyst, obtain hydrogenated oil, gained hydrogenated oil carries out gas-liquid separation in high-pressure separator, and the fractionation in separation column of the high-pressure separator isolated liquid phase of institute is gas, naphtha fraction, diesel oil distillate and hydrogenation long residuum;
Described boiling bed hydrogenation reacting appliance responds device cylinder shell (1), upper cover and lower cover, gas-liquid separator (3) is set gradually in reactor, vertical oil guide pipe (4) and distributing disc (9), it is characterized in that, at reactor upper cover place, oil gas vent (2) is set, the entrance of high pressure oil guide pipe (5), the entrance of hydrogen feed tube (10) is set at reactor lower cover place, in reactor, the lower end of gas-liquid separator (3) is connected with the entrance of vertical oil guide pipe (4), the bottom of vertical oil guide pipe (4) is connected with distributing disc (9), the exit of vertical oil guide pipe (4) is positioned at the below of distributing disc (9), high pressure oil guide pipe (5) is set on reactor top, the exit end of its mesohigh oil guide pipe (5) is positioned at vertical oil guide pipe (4), the distance in axial direction of high pressure oil guide pipe (5) exit end and vertical oil guide pipe (4) inlet end and the ratio of vertical oil guide pipe (4) length are 0.1 ~ 8:10.
2. method of hydrotreating according to claim 1, it is characterized in that, the top of described boiling bed hydrogenation reactor arranges catalyst addition tube (7), and described catalyst addition tube (7) exit is positioned at the below of gas-liquid separator (3).
3. method of hydrotreating according to claim 1, it is characterized in that, the bottom of described boiling bed hydrogenation reactor arranges catalyzer downstream line (8), described catalyzer downstream line (8) is through distributing disc (9), and its ingress is positioned at the top of distributing disc (9).
4. method of hydrotreating according to claim 1, is characterized in that, the hydrogen feed tube (10) of described boiling bed hydrogenation reactor is positioned at the below of distributing disc (9).
5. method of hydrotreating according to claim 1, is characterized in that, the aspect ratio of the reactor cylinder shape housing of boiling bed hydrogenation reactor is 0.8:1 ~ 100:1.
6. method of hydrotreating according to claim 1, it is characterized in that, in boiling bed hydrogenation reactor, described reactor cylinder shape housing (1), gas-liquid separator (3), vertically oil guide pipe (4) and distributing disc (9) are coaxial each other.
7. method of hydrotreating according to claim 1, is characterized in that, straight down, and high pressure oil guide pipe (5) exit end is coaxial each other with vertical oil guide pipe (4) in the direction of described high pressure oil guide pipe (5) exit end.
8. the method for hydrotreating according to claim 1 or 7, it is characterized in that, the ratio of high pressure oil guide pipe (5) the exit end outer wall of boiling bed hydrogenation reactor and the distance radially of vertical oil guide pipe (4) inwall and vertical oil guide pipe (4) internal diameter is 0.05 ~ 0.5:1.
9. the method for hydrotreating according to claim 1 or 7, it is characterized in that, the high pressure oil guide pipe (5) of boiling bed hydrogenation reactor has well-balanced wall thickness, the exit of high pressure oil guide pipe (5) arranges diameter shrinkage part (6), the internal diameter of described diameter shrinkage part (6) reduces gradually along the axis of high pressure oil guide pipe (5), and the internal diameter of the exit end of high pressure oil guide pipe (5) is minimum.
10. method of hydrotreating according to claim 9, is characterized in that, the maximum inner diameter of diameter shrinkage part (6) and the ratio of minimum diameter in high pressure oil guide pipe (5) exit are 20 ~ 2:1.
11. method of hydrotreating according to claim 9 or 10, it is characterized in that, the maximum inner diameter part of the diameter shrinkage part (6) in high pressure oil guide pipe (5) exit is positioned at vertical oil guide pipe (4), and the ratio of the outer wall of its correspondence and the distance radially of vertical oil guide pipe (4) inwall and vertical oil guide pipe (4) internal diameter is 0.05 ~ 0.5:1.
12. method of hydrotreating according to claim 1, the pressure height 0.5-10MPa in the pressure ratio reactor in high pressure oil guide pipe (5).
13. method of hydrotreating according to claim 1, the hydrogenation long residuum component loops of gained returns boiling bed hydrogenation reactor, carries out hydrogenation reaction again together with residual oil raw material.
14. method of hydrotreating according to claim 1, the hydrogenation long residuum part of gained carries out underpressure distillation, gained hydrogenation decompressed wax oil together with remainder hydrogenation long residuum as catalytically cracked material; Underpressure distillation gained hydrogenation vacuum residuum loops back boiling bed hydrogenation reactor, carries out hydrogenation reaction again together with residual oil raw material.
15. method of hydrotreating according to claim 1, the reaction conditions of boiling bed residual oil hydrogenation is: hydrogen dividing potential drop 2.0 ~ 22.0MPa, temperature of reaction 300 ~ 450 DEG C, volume space velocity 0.1 ~ 5.0 hour
-1, hydrogen to oil volume ratio 100 ~ 2000Nm
3/ m
3.
16. method of hydrotreating according to claim 1, described boiling bed hydrogenation catalyst take porous inorganic oxide as carrier, one or more the catalyzer being active ingredient with one or more the oxide compound in group VIB and/or group VIII metal.
17. according to the method for hydrotreating in claim 1-16 described in any one, wherein, described residual oil raw material is one or more in the secondary processing distillate of oil at the bottom of heavy crude, acid-containing raw oil, long residuum, normal pressure wax oil, vacuum residuum, wax tailings, tank, shale oil, coal direct liquefaction oil, deasphalted oil, viscous crude, hydrocracking tail oil and hydrocracking tail oil.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110591759A (en) * | 2019-07-03 | 2019-12-20 | 上海竣铭化工工程设计有限公司 | Processing technology for producing olefin and aromatic hydrocarbon from inferior heavy oil |
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| CN103228355A (en) * | 2010-12-20 | 2013-07-31 | 雪佛龙美国公司 | Hydroprocessing catalyst and method for making thereof |
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