CN108018074A - Improve the heavy oil hydrogenation treatment method of catalyst utilization - Google Patents
Improve the heavy oil hydrogenation treatment method of catalyst utilization Download PDFInfo
- Publication number
- CN108018074A CN108018074A CN201610968483.3A CN201610968483A CN108018074A CN 108018074 A CN108018074 A CN 108018074A CN 201610968483 A CN201610968483 A CN 201610968483A CN 108018074 A CN108018074 A CN 108018074A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- weighted bmo
- bmo spaces
- reaction zone
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
- C10G2300/206—Asphaltenes
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of heavy oil hydrogenation treatment method for improving catalyst utilization.After heavy oil feedstock oil is mixed with hydrogen, first by weighted BMO spaces area, hydrodemetallization and partial desulfurization reaction are carried out；Reaction effluent enters hydrotreating reaction area, carries out hydrodesulfurization and hydrodenitrogeneration reaction；Wherein the reaction temperature of weighted BMO spaces reaction zone is higher than the reaction temperature in hydrotreating reaction area.In the method for the present invention, weighted BMO spaces reaction zone is reacted at higher temperatures, the most of metal impurities that can be stripped of in material, so that the deactivation cause of desulfurization and/or denitrification catalyst is changed into only coking deactivation from conventional metal deposit and coking deactivation in hydrotreating reaction area, so that desulphurization catalyst and denitrification catalyst can carry out regeneration treatment after using a cycle, extend the service cycle of hydrogenation plant, so as to add the operational efficiency of device, economy is improved.
Description
Technical field
The present invention relates to petroleum refining field, more particularly to a kind of heavy-oil hydrogenation processing side for improving catalyst utilization
Method.
Background technology
At present, domestic and international refined products market will be in continuous upward trend to the demand of light, middle matter oil product, to fuel oil etc.
The demand of heavy oil product is then on a declining curve.Further, since the pressure of environmental protection increasingly increases, various countries generally improve oil
The quality criteria requirements of the especially automobile-used petrol and diesel oil product of product., can be with more economical rational generation under above-mentioned market trend
Valency realize heavy oil lighting and can make obtained product meet the oil Refining Technologies of constantly harsh petrol and diesel oil product specification into
One of technology of domestic and international oil Refining Technologies developer's focus development.
In the various processes of heavy oil product lighting, heavy oil product is subjected to hydrotreating first, is then hydrogenated with
It is a kind of preferable technical process that tail oil, which carries out catalyzed cracking processing,.By hydrogenation, significantly reduce metal in these raw materials,
Sulphur, nitrogen, asphalt content, improve hydrogen-carbon ratio, and then excellent raw material is provided for devices such as catalytic cracking and delayed cokings.At present
Main hydrogenation technique mainly has ebullated bed, suspension bed, moving bed and fixed-bed process, wherein suspension bed and moving bed process also
It is very immature, and cost is higher.Ebullated bed investment is higher, and operation difficulty is larger.Fixed bed is low, easy to operate because of cost
And security is small, technology maturation, thus develop very fast.
In the prior art, realized by being provided with multiple hydrogenation reactors of multiple hydrogenation catalyst beds to heavy oil product
Hydrotreating.But the usual viscosity of heavy oil product is larger, metal impurities or asphalitine are higher, in hydrogenation process, metal and
Coke can be gradually deposited on catalyst, easily make rapid catalyst deactivation, and bed blocks, pressure rise, this phenomenon is the
One hydrogenation reactor is especially serious, moreover, when the pressure drop in first reactor reaches or approaches the theoretical pressure drop upper limit, instead
Answer and easily occur hot spot in device, device can only be forced to stop work at this time, shorten the service cycle of heavy oil product hydrotreater.
It is former that CN1349554A discloses a kind of up-flow reactor system hydrotreating heavy with stratiform catalyst bed
The method of material.With the upflow fixed bed reactor hydrotreating metal of the catalyst of at least two different hydrogenation activities, sulphur and
The heavy charge of carbon containing residual matter pollution.But this method cycle of operation is short, it is usually no more than 1 year.
Itd is proposed in CN1484684A replaceable reactor and can short-circuit reaction device hydrotreatment of heavy hydrocarbon fraction method, should
It is traditional down-type fixed-bed reactor that reactor is protected in patent, if Ca, Fe content are higher in raw material, due to reaction
Logistics from top to bottom, if the gap between these solid impurity blocking catalysts, though in protective agent duct deposited metal energy
When power does not arrive saturation capacity, this reactor pressure decrease can also raise, so that another reactor must be switched to.
CN102453530A discloses a kind of method of hydrotreating of processing heavy oil product, heavy oil product feedstock oil and hydrogen mixing
Enter hydrogenation protecting reaction zone afterwards, then immediately proceed to hydrotreating reaction area, at least two parallel connections be set in hydrogenation protecting area
Can switch the up flow type hydrogenation protecting reactor used in turn.The invention is had using the method for four kinds of hydrogenation protecting agent gradings
Beneficial to removing metal, with the service life for preventing from blocking and improving major catalyst, extend the operation cycle of device.But this method is to device
The increase rate of the cycle of operation is still little.
The content of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of heavy oil hydrogenation treatment method for improving catalyst utilization,
Especially one kind can give full play to differential responses area catalyst performance, increase the heavy-oil hydrogenation processing side of device service cycle
Method.
A kind of heavy oil hydrogenation treatment method for improving catalyst utilization provided by the present invention, including herein below：
（1）At least one weighted BMO spaces reaction zone and a hydrotreating reaction area are provided；Bag in weighted BMO spaces reaction zone
Hydrogenation protecting catalyst and Hydrodemetalation catalyst are included, Hydrobon catalyst is included in hydrotreating reaction area and hydrogenation is de-
Nitrogen（Carbon residue converts）Catalyst；
（2）Heavy oil feedstock oil is mixed into weighted BMO spaces reaction zone with hydrogen first, is added under the conditions of weighted BMO spaces
Hydrogen reacts, and metal impurities are removed 40wt% ~ 90wt%, and sulphur is removed 20wt% ~ 70wt%, obtains the reaction stream of tenor reduction
Go out thing；
（3）Step（2）Obtained reaction effluent enters high-pressure separator, isolates gas, liquid two-phase；Separating obtained gas
Through desulfurization and compressor compresses Posterior circle to weighted BMO spaces reaction zone；
（4）Step（3）Isolated product liquid is mixed with the fraction of stream that hydrotreating zone is recycled back to, into mixed hydrogen tank into
Go and mix hydrogen, the miscella after the molten hydrogen of saturation enters liquid-phase hydrogenatin treatment reactor, under hydroprocessing conditions, is urged with hydrodesulfurization
Agent and hydrodenitrogenation catalyst carry out haptoreaction, obtain the reaction effluent of sulfur content and nitrogen content reduction；
（5）Step（4）An obtained liquid-phase hydrogenatin reaction effluent part is recycled to mixed hydrogen tank, and another part flows out after decompression
Device.
Hydrotreating method according to the present invention, wherein step（2）The average reaction temperature of weighted BMO spaces reaction zone compared with
Step（4）The average reaction temperature in hydrotreating reaction area wants 5~40 DEG C high, preferably 10~30 DEG C high.
Hydrotreating method according to the present invention, wherein, step（1）It is middle that more than two weighted BMO spaces reactions are provided
Area, which is usually arranged in parallel, the reaction zone of changeable operation.Therefore, it is of the invention
Method can also include step（6）, can be by it after one of weighted BMO spaces reaction zone cannot meet service requirement
Reaction process is cut out, and second weighted BMO spaces reaction zone is cut in technological process, the weighted BMO spaces reaction zone cut out
The displacement of catalyst can be carried out, that is, draws off the old catalyst of inactivation, reloads fresh and/or regenerated catalyst.
The weighted BMO spaces reaction zone cannot meet that service requirement refers to：The effluent of weighted BMO spaces reaction zone can not
Meet that the pressure drop of at least one catalyst bed in the feed needs or weighted BMO spaces reaction zone of downstream hydrogenation treatment region reaches
There is hot spot in the pressure drop upper limit or catalyst bed.
It is described can not meet downstream hydrogenation processing reaction zone the standards of feed needs can be：Weighted BMO spaces reaction zone
Tenor in outlet product liquid exceedes setting.Specifically, judging weighted BMO spaces reaction zone outlet product liquid is
The standard of the no feed needs for meeting downstream hydrogenation treatment region is the tenor in effluent liquid（Refer to W metal, V, Fe,
The summation of Na and Ca equal sizes）More than any point value in the μ g/g of 8 μ g/g~50, in the μ g/g of preferably more than 10 μ g/g~30
Any point value.
The pressure drop upper limit designs 0.4~0.8 times, preferably 0.5~0.8 times of maximum pressure drop for reactor.Institute
State hot spot and reach 15~50 DEG C, preferably 15~30 DEG C for the radial temperature difference at least one catalyst bed.
In the heavy oil hydrogenation treatment method of the present invention, the heavy oil feedstock oil refers to by topped crude, petroleum residual oil, oil
The hydro carbons for the high asphalt content that sand, pitch, shale oil, liquefaction coal or reclaimed oil obtain.Heavy oil feedstock oil usually contains various
Pollutant, its carbon residue is high, and the impurity content such as sulphur and nitrogen is high, its tenor is typically larger than 30 μ g/g.The method of the present invention is especially
It is adapted to the heavy oil feedstock of processing high metal content, is especially suitable for processing metal (nickel+vanadium) content and is more than 60 μ g/g and/or iron content
More than 10 μ g/g and/or calcium content is more than the heavy oil feedstock of 10 μ g/g.
In the method for the present invention, the hydrogenation protecting catalyst that weighted BMO spaces reaction zone uses can be that residual hydrogenation is protected
Agent, or prepared according to feedstock property by this area conventional method.Residual hydrogenation protective agent is this area conventional catalyst, can be with
Using commercial goods.The hydrogenation protecting agent using porous refractory inorganic oxide such as aluminium oxide as carrier, group VIB and/or
One or more of oxides in VIII race's metal such as W, Mo, Co, Ni are the catalyst of active component, such as by China Petroleum
The FZC series residual hydrogenation protective agents of catalyst branch company of work limited company production.
The Hydrodemetalation catalyst can be residuum hydrogenating and metal-eliminating catalyst, or according to feedstock property by this
It is prepared by field conventional method.These catalyst are typically all the group VIB using porous refractory inorganic oxide such as aluminium oxide as carrier
And/or VIII one or more of oxides of race's metal such as W, Mo, Co, Ni etc. be active component, be selectively added other each
The catalyst of the elements such as kind auxiliary agent such as P, Si, F, B.The Hydrodemetalation catalyst, on the basis of the gross weight of catalyst,
And in terms of oxide, the content of molybdenum and/or tungsten is 0.5~15 weight %, the content of cobalt and/or nickel is 0.3~8 weight %, remaining
Measure as alumina support.The alumina support is a kind of bimodal porous aluminum oxide, its pore volume is 0.5~2.0 ml/g, than
Surface area is 120~350 meters2/ gram, aperture accounts for total pore volume 30~90% in 10-30 nanometers of pore volume, and aperture is received in 100-2000
The pore volume of rice accounts for total pore volume 10~50%, and bore dia is less than 10 nanometers, between 30-100 nanometers and more than 2000 nanometers
The sum of pore volume accounts for total pore volume below 20%.The diffusion process of reactant molecule and the active surface that reaction is required are arrived in order to balance,
The catalyst of bimodal pore distribution with macropore and mesoporous is shown preferably in weighted BMO spaces reaction zone reaction process
Performance.In weighted BMO spaces reaction zone, the admission space ratio of hydrogenation protecting catalyst and Hydrodemetalation catalyst is generally 5:
95~95:5, it is preferably 10:90~60:40.
Heavy oil hydrogenation treatment method according to the present invention, wherein in weighted BMO spaces reaction zone, preferably in the de- gold of hydrogenation
The downstream of metal catalyst can also include Hydrobon catalyst.The loadings of Hydrobon catalyst are hydrodemetallisation catalyst
0~30v% of agent loadings, preferably 5v%~30v%.
The Hydrobon catalyst can be the common residuum hydrodesulfurization catalyst in this area, or according to raw material
Property is prepared by this area conventional method.Catalyst is typically all using porous refractory inorganic oxide such as aluminium oxide as carrier the
The oxide of VI B races and/or VIII race's metal such as W, Mo, Co, Ni etc. are active component, are selectively added other various auxiliary agents such as
P, the catalyst of the element such as Si, F, B.Due to having stringent limit to tenor in weighted BMO spaces reaction zone product in this technology
System, in order to more preferably play the overall performance of catalyst system preferably using improved Hydrobon catalyst, the catalyst it is total
Body performance is between conventional Hydrodemetalation catalyst and Hydrobon catalyst, i.e. the aperture of the catalyst is more conventional to be added
Hydrogen desulphurization catalyst is bigger, have it is preferable hold metal ability, its more conventional Hydrodemetalation catalyst of activity is slightly higher, have compared with
Strong hydrodesulfurization ability.
The Hydrobon catalyst, on the basis of the gross weight of catalyst, and in terms of oxide, molybdenum and/or tungsten
Content is 10~25 weight %, and the content of cobalt and/or nickel is 1~6 weight %, and surplus is alumina support.The aluminium oxide
Pore volume is not less than 0.35 ml/g, and specific surface area is 150~350 meters2/ gram, aperture accounts for total pore volume in 6~15 nanometers of pore volume
More than 70%.
In the method for the present invention, reaction condition can be according to the reaction effect that the property and requirement of raw material reach by this area
General knowledge determines.In general the reaction condition of weighted BMO spaces reaction zone is that reaction pressure is 5MPa~35MPa, preferably
10MPa~20MPa, average reaction temperature are 340 DEG C~430 DEG C, and preferably 340 DEG C~420 DEG C, volume space velocity is 0.1h during liquid-1
~5.0h-1, it is preferably 0.3h-1~3.0h-1, hydrogen to oil volume ratio is 200~2000, is preferably 300~1500.
In the method for the present invention, the catalyst used in hydrotreating reaction area can be that the common heavy oil product in this area adds
Hydrogen handles catalyst, and optimum catalyst property can be optimized according to feedstock property.Catalyst generally comprises a variety of, such as hydrogenation
Desulphurization catalyst and hydrodenitrogenation catalyst etc..These catalyst be typically all using porous refractory inorganic oxide such as aluminium oxide as
The oxide of carrier, group VIB and/or VIII race's metal such as W, Mo, Co, Ni etc. are active component, are selectively added other each
The catalyst of the elements such as kind auxiliary agent such as P, Si, F, B.
In the hydrotreating reaction area, the admission space of Hydrobon catalyst and hydrodenitrogenation catalyst is than general
For 20:80~80:20, it is preferably 40:60~70:30.
The property of the hydrodenitrogenation catalyst is：On the basis of the gross weight of catalyst, in terms of oxide molybdenum and/or
The content of tungsten is 12~30 weight %, and the content of cobalt and/or nickel is 3~12 weight %, and surplus is alumina support.The oxidation
The pore volume of aluminium is not less than 0.35 ml/g, and specific surface area is 150~350 meters2/ gram, aperture accounts for always in 6~15 nanometers of pore volume
40~75 % of pore volume.
The method according to the invention, can also include a small amount of Hydrodemetalation catalyst wherein in hydrotreating reaction area,
Hydrodemetalation catalyst is seated in the upstream of Hydrobon catalyst, and the loadings of Hydrodemetalation catalyst are hydrotreating
0~30v% of reaction zone catalyst total filling amount, preferably 2v%~30v%.
In hydrotreating reaction area catalyst filling order be usually make reaction stream successively with hydrodemetallisation catalyst
Agent, Hydrobon catalyst and hydrodenitrogenation catalyst contact, also have the technology of these types of catalyst mixed packing certainly.On
State the technology contents that Catalyst packing technology is well known to those skilled in the art.Catalyst can use commercial goods, as in
The FZC series residuum hydrogenating and metal-eliminating catalysts of petrochemical industry Fushun Petrochemical Research Institute of state development and production, desulphurization catalyst and de-
Nitrogen catalyst, can also prepare according to this area existing method.
In the method for the present invention, the reaction condition in hydrotreating reaction area is that reaction pressure is 5MPa~35MPa, preferably
It is that 10MPa~20MPa, average reaction temperature are 320 DEG C~420 DEG C, preferably operates at 330 DEG C~410 DEG C, volume is empty during liquid
Speed is generally in 0.1h-1~5.0h-1, it is preferably 0.3h-1~3.0h-1, liquid phase circulation ratio（The quality of recycle oil/fresh feed oil
Than）For 0.1:1~10:1, preferably 0.2:1~3:1.
In the method for the present invention, weighted BMO spaces belong to serial operation, therefore two reactions with hydrotreating two reaction zones
The pressure in area is same pressure rating, because the presence of pressure drop might have difference slightly.
In the method for the present invention, hydrodemetallization and partial hydro-desulfurization reaction are substantially carried out in weighted BMO spaces reaction zone,
It is operated at a higher temperature, is conducive to the progress of demetalization reaction, so that the activity of Hydrodemetalation catalyst can
It is fully used.The material for being stripped of a large amount of metal impurities is further reacted into hydrotreating reaction area.Due to
A large amount of metal impurities are stripped of, murder by poisoning of the material to hydrotreating zone catalyst into hydrotreating reaction area is greatly lowered,
The utilization rate of Hydrobon catalyst and hydrodenitrogenation catalyst can be significantly improved, extends the use of hydrotreating zone catalyst
Service life, and then effectively extend the service cycle of a whole set of hydrotreater.For the operation of Proper Match two reaction zones, hydrogenation
The average reaction temperature in pretreatment reaction area is 5~40 DEG C high compared with the average reaction temperature in hydrotreating reaction area, preferably high by 10~
30℃。
In the method for the present invention, the weighted BMO spaces reaction zone can set one or more hydrogenation protecting to react
Device, each hydrogenation protecting reactor is at least provided with a hydrogenation protecting catalyst bed, if being provided with multiple catalyst beds,
Quenching hydrogen can be squeezed between reaction bed, with controlling reaction temperature.
In the method for the present invention, hydrotreating reaction area can set a reactor, can also set more reactors,
2~5 are usually set, is preferably provided with 2~3 reactors.The number of each catalyst in reactor bed is generally 1~5,
It is preferred that 1~3, if setting more than two catalyst beds, the generation oil of the molten hydrogen of saturation can be squeezed between bed, can
Further to increase the dissolving hydrogen amount in reactor in liquid, the purpose of hydrodesulfurization, hydrodenitrogeneration is better achieved.It is being hydrogenated with
Handle in reaction zone, Hydrodemetalation catalyst is loaded successively along the flow direction of reaction stream（It is selectable）, hydrodesulfurization urges
Agent and hydrodenitrogenation catalyst.In the method for the present invention, the loadings of catalyst can be according to feed stock in each catalyst bed
The requirement of matter, selected catalyst and product property comes specifically chosen.
To reach more preferable effect, the changeable weighted BMO spaces reaction zone of two or more can be used.It is described changeable
Implication refers to be provided with multiple weighted BMO spaces reaction zones, and each weighted BMO spaces reaction zone can individually be connected into follow-up add
Hydrogen handles reaction zone, also can individually be cut out from hydrotreating reaction area.
Hydrotreating method according to the present invention, the purpose that multiple changeable weighted BMO spaces reaction zones are set be in order to
The catalyst in each reactor in hydrotreating reaction area is set to obtain lasting hydrogenation protecting by switching.Therefore, Mei Gejia
Hydrogen pretreatment reaction zone sets the number of reactor and as long as connection relation meets the purpose that switching uses.Preferably, institute
The quantity for stating weighted BMO spaces reaction zone is 2, and the weighted BMO spaces reaction zone sets 1 reactor, preferably with
Mode in parallel connects, and two weighted BMO spaces reaction zones one and only one be in on-line machining state.Weighted BMO spaces
The agent of order filling hydrogenation protecting, Hydrodemetalation catalyst and Hydrobon catalyst, all kinds of protective agents and catalysis in reaction zone
The grading mode of agent can be determined according to the property of raw material by this area Conventional wisdom.
The present invention method in, described two weighted BMO spaces reaction zones one and only one be online it is specific
It is meant that, when the first weighted BMO spaces reaction zone can not meet the feed needs or the first weighted BMO spaces of downstream hydrogenation treatment region
The pressure drop of at least one catalyst bed reaches in reaction zone when there is hot spot in the pressure drop upper limit or catalyst bed, by first plus
All reactors in hydrogen pretreatment reaction zone are cut out, while the reactor of the second weighted BMO spaces reaction zone is cut.When
Two weighted BMO spaces reaction zones can not meet the feed needs or the second weighted BMO spaces reaction zone of downstream hydrogenation processing reaction zone
In the pressure drop of at least one catalyst bed reach and occur hot spot in the pressure drop upper limit or catalyst bed and can not continue to operate
When, protective agent and catalyst whole in all reactors are replaced after can stopping work with device.Can also be according to hydrotreating reaction
The situation of catalyst activity cuts out the reactor of the second weighted BMO spaces reaction zone in area, while will replace protective agent and urged
Reactor incision in first weighted BMO spaces reaction zone of agent, so circulation, until the catalyst in hydrotreating reaction area
It can not meet running requirements.
There is no particular limitation for flow direction of the invention to raw material in hydrogenation protecting area and hydrotreating zone, weighted BMO spaces
Each reactor in reaction zone and hydrotreating reaction area can be up-flow reactor or be downflow reactor.
In the prior art, in heavy oil hydroprocessing units according to Flow of Goods and Materials direction, despite the presence of the influence of cold hydrogen, still
Low early and high after trend is generally presented in reaction temperature, i.e., in from start of run to the whole cycle in operating latter stage, hydrogenation is protected
Protect a few class catalyst beds such as catalyst, Hydrodemetalation catalyst, Hydrobon catalyst and/or hydrodenitrogenation catalyst
Average reaction temperature is elevated successively.Meanwhile setting of the existing catalyst grade with system is with all anti-when operating latter stage
Device is answered to reach synchronous inactivation, synchronously change for the purpose of agent.Therefore, in operation process, when first reactor pressure drop rise or
When there is hot spot, or hydrogenation products cannot meet that needs horse back whole device out of service is to replace during downstream unit requirement
Some catalyst.Catalyst in the hydrodesulfurization swum in such a case the lower and/or denitrification reactor also " has lost substantially
It is living ".Therefore the operation cycle of package unit is limited be subject to first catalyst reactor service life.And even for adding
Hydrogen protection uses the hydroprocessing technique of reactor handover operation（Such as CN1484684A and CN102453530A）For, it is a whole set of
The service cycle of device is similarly subjected to the limitation of first catalyst reactor service life.
After substantial amounts of research has been carried out to existing hydrotreating method, present inventor is surprised to find that：It is existing
In technology, after hydrotreater is stopped work because of hot spot and/or the pressure drop of hydrogenation protecting catalyst bed, device rear portion（Under
Trip）Although the desulphurization catalyst and denitrification catalyst that use also have inactivated, but its deactivation cause is more because catalyst
Caused by the metal that the aperture in duct is deposited blocks, and the metal of deposition is really and few inside catalyst duct.Make a concrete analysis of it
Reason, applicant think：In the middle and later periods of device operating, the metal in feedstock oil " penetrated " completely hydrogenation protecting catalyst and
Catalyst for demetalation bed, and it has been directly entered the desulphurization catalyst and denitrification catalyst bed at rear portion.Due to desulphurization catalyst
And/or the aperture of denitrification catalyst is smaller, the metal of removing cannot be introduced into duct inside so being deposited on catalyst aperture
Near, so as to cause the inactivation of desulphurization catalyst and denitrification catalyst.In this condition, Hydrobon catalyst and/or add
The inactivation of hydrogen denitrification catalyst be not fully because the carbon distribution of catalyst in itself is excessive and caused by, and be more because raw material
After oil penetrates hydrogenation protecting catalyst bed and Hydrodemetalation catalyst bed so that more hydrodesulfurizations should be undertaken
And/or the desulfurization of denitrification functions and/or denitrification catalyst are undertaken caused by the function of hydrodemetallization.Meanwhile design originally
After catalyst for desulfurization, denitrogenation and/or de- carbon residue undertakes partial hydrogenation demetalization function, due to its catalyst pore structure
Limitation, cannot also realize demetalization function well, while also create desulfurization, denitrogenation and/or the reduction of de- carbon residue ability, and
The waste of catalyst function is caused, so that the activity of hydrodesulfurization and/or hydrodenitrogenation catalyst cannot obtain sufficient profit
With.
The present inventor has found that package unit can be divided into weighted BMO spaces reaction zone and hydrogenation by numerous studies
Reaction zone is handled, wherein weighted BMO spaces reaction zone operates under of a relatively high reaction temperature, and hydrotreating reaction area is in phase
To being operated under relatively low reaction temperature.The tenor of weighted BMO spaces reaction zone outlet material is controlled in technical solution first,
Most of metal impurities i.e. in weighted BMO spaces reaction zone removes feedstock oil, only the metal of remaining a small amount of more difficult removing is miscellaneous
Matter, while realize partial hydro-desulfurization.And weighted BMO spaces reaction zone reaction stream enter hydrotreating reaction area be
Operated at relatively low temperature, i.e., carry out hydrodesulfurization and hydrogenation saturated reaction, such metal at relatively low temperature
Impurity can be in the case where being not involved in reaction directly by desulphurization catalyst and/or denitrification catalyst, so as to avoid catalyst
The permanent deactivation caused by metal deposit.Meet the feed needs of downstream unit by scheme optimization product.With it is existing
Technology is compared, and method of the invention changes existing catalyst system and operator scheme, i.e., by the prior art according to logistics direction
Low early and high after trend is presented in reaction temperature, changes into trend low after height before being presented according to logistics orienting response temperature, this hair
Bright method can make full use of the activity of all catalyst, so as to increase the operational efficiency of device, improve its economy.The application
Inventor complete the present invention on this basis.
Compared with prior art, the method have the advantages that：
1st, by the way that heavy oil hydroprocessing units are divided into weighted BMO spaces reaction zone and hydrotreating reaction area, in weighted BMO spaces
Most of metal impurities in reaction zone removing material, make poison of the material to hydrotreating zone catalyst for entering hydrotreating zone
Evil is greatly lowered, and can make full use of the activity of all catalyst in hydrotreating zone, compared with prior art, the operating of device
Cycle can extend 30~100%, so as to add the operational efficiency of device, improve economy.
2nd, reactor is protected using switchable type in weighted BMO spaces reaction zone, substantially increases the demetalization energy of device
Power, so as to process the raw material of tenor higher.
3rd, the most of metal impurities being stripped of due to weighted BMO spaces reaction zone in material so that hydrotreating reaction area
The deactivation cause of middle desulphurization catalyst and/or denitrification catalyst is changed into only carbon deposit mistake from conventional metal deposit and coking deactivation
It is living, so that desulphurization catalyst and denitrification catalyst can carry out regeneration treatment after using a cycle, greatly save and urge
Agent buying expenses.
4th, hydrotreating zone uses liquid-phase hydrogenatin, on the one hand plays the purpose for reducing catalyst bed temperature rise, can be effective
Avoid the generation of hot spot, at the same also eliminate between bed and/or between reactor quenching hydrogen injection, on the other hand by hydrogenation
Recycle oil causes part aromatic hydrocarbons to obtain saturation, have the function of increase hydrogen supply, can inhibit the formation of coke, avoid catalyst because
Coking deactivation, and then extend the service life of catalyst.
5th, the activity of the catalyst in hydrotreating reaction area is made full use of, improves the treating capacity of device, or is reduced
Equipment investment.
Brief description of the drawings
Fig. 1 is a kind of process flow diagram for the heavy oil hydrogenation treatment method for improving catalyst utilization of the present invention.
Fig. 2 is the process flow diagram of comparative example 2 and 3.
Embodiment
The embodiment of the present invention is described in detail below in conjunction with attached drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
Attached drawing is that a kind of heavy oil hydrogenation treatment method principle process for improving catalyst utilization provided by the present invention shows
It is intended to, some ancillary equipments in figure（Heat exchanger, pump etc.）Do not mark, but this is known for those of ordinary skill in the art
's.
A kind of flow of heavy oil hydrogenation treatment method for improving catalyst utilization provided by the present invention is as follows：
After first coming from fresh feed residual oil, the recycle hydrogen from pipeline 26 and the new hydrogen from pipeline 25 mixing of pipeline 27,
Enter through pipeline 10 in the reactor 1 of first weighted BMO spaces reaction zone, carry out hydrodesulfurization and hydrogenation in the presence of a catalyst
Demetalization is reacted, and hydrogenation products enter high pressure from the top of reactor 1 of the first weighted BMO spaces reaction zone through pipeline 9 and pipeline 13
Separator 5 carries out gas-liquid separation, and separating obtained hydrogen-rich gas 14 is anti-to weighted BMO spaces through desulfurization and the compression Posterior circle of compressor 8
Area is answered, separating obtained product liquid 15 is mixed with the hydrotreating zone liquid-phase hydrogenatin reaction effluent recycle oil 23 from pipeline 23
Afterwards, into mixed hydrogen tank 6, the hydrogen introduced with pipeline 17 carries out mixing molten hydrogen, and the exess of H2 gas is discharged through pipeline 16, the molten hydrogen of saturation
Miscella afterwards enters liquid phase hydrogenation reactor 3 through pipeline 18 and carries out hydrogenation reaction, and reaction effluent enters mixed hydrogen through pipeline 19
Tank 7, the hydrogen introduced with pipeline 21 carry out mixing molten hydrogen, and the exess of H2 gas is discharged through pipeline 20, the miscella warp after the molten hydrogen of saturation
Pipeline 22 enters liquid phase hydrogenation reactor 4 and carries out hydrogenation reaction, and a gained reaction effluent part is recycled to mixed hydrogen through pipeline 23
Tank 6, another part is through 24 bleeder of pipeline.
When the reactor 1 of the first weighted BMO spaces reaction zone can not meet feed needs or the reaction of downstream hydrogenation treatment region
The pressure drop of at least one catalyst bed reaches in device 1 when there is hot spot in the pressure drop upper limit or catalyst bed, is cut out, and
Cut the reactor 2 of the second weighted BMO spaces reaction zone（Material enters reactor 2 through pipeline 12 at this time, is flowed out instead through pipeline 11
Answer device 2）To continue to complete hydroprocessing processes, while the catalyst in the first weighted BMO spaces reaction zone reactor 1 is replaced, weight
New loading fresh catalyst is stand-by.When the reactor 2 of the second weighted BMO spaces reaction zone can not meet downstream hydrogenation processing reaction
The pressure drop of at least one catalyst bed reaches in the pressure drop upper limit or catalyst bed and occurs in the feed needs or reactor 2 in area
When can not continue the hot spot of operation, cut out, while the reactor 1 for cutting the first weighted BMO spaces reaction zone continues to complete
Hydroprocessing processes, while the catalyst in the reactor 2 of the second weighted BMO spaces reaction zone is replaced, reload fresh catalyst
Agent is stand-by.So circulation, the service life of the catalyst until reaching hydrotreating zone.
Limited below in conjunction with specific embodiment is further to the method for the present invention.Original used in embodiment and comparative example
The property of material oil is listed in table 1, and the property of used catalyst is listed in table 2.In table 2, A is hydrogenation protecting catalyst, and B is the de- gold of hydrogenation
Metal catalyst, C are Hydrobon catalyst, and D is hydrodenitrogeneration（Carbon residue converts）Catalyst.
1 raw material oil nature of table
2 catalyst property of table
Embodiment 1
According to the technological process described in Fig. 1, the first weighted BMO spaces that weighted BMO spaces reaction zone includes changeable operation react
Area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone set a reactor 1, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and the reaction being arranged in series
Device 4.According to Flow of Goods and Materials direction, weighted BMO spaces reaction zone（It is online to only have a weighted BMO spaces reaction zone in operation process）
Catalyst A, catalyst B and catalyst C are filled with reactor, the admission space ratio of each catalyst is 2: 7: 1.Hydrotreating is anti-
Answer and catalyst B and catalyst C is housed in area's reactor 3, the admission space ratio of two kinds of catalyst is 1: 9, and is only filled in reactor 4
Fill out catalyst D.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is high compared with hydrotreating zone, and specific reaction condition is shown in Table
3.Feedstock oil A controls followed by reactor 1, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4
Weighted BMO spaces reaction zone exports the metal of effluent（Ni+V）Content is not higher than 12 μ g/g.Hydrogenated back end hydrogenation handles reaction zone
Sulfur content is 0.20 weight % in effluent, nitrogen content is 1712 μ g/g, carbon residue is 4.42 weight %, metal（Ni+V）Content is
7.0µg/g.After operating 6 months, the reactor 1 of the first weighted BMO spaces reaction zone exports the metal of effluent（Ni+V）Content surpasses
The pressure drop for crossing at least one catalyst bed in 12 μ g/g or reactor 1 reaches appearance heat in the pressure drop upper limit or catalyst bed
Point, is cut out, and the reactor 2 for cutting the second weighted BMO spaces reaction zone continues to complete hydroprocessing processes（It is former at this time
Expect oil A followed by reactor 2, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4）, device is still flat
Steady operation, generation oil quality disclosure satisfy that downstream RFCC feed needs.When the reactor 2 of the second weighted BMO spaces reaction zone exports
The metal of effluent（Ni+V）Pressure drop of the content more than at least one catalyst bed in 12 μ g/g or reactor 2 reaches in pressure drop
When occurring the hot spot that can not continue operation in limit or catalyst bed, cut out, while cut the reaction of the first weighted BMO spaces
The reactor 1 in area continues to complete hydroprocessing processes, while replaces urging in the reactor 2 of the second weighted BMO spaces reaction zone
Agent, it is stand-by to reload fresh catalyst.So circulation, the final device have operated 24 months, since product quality is deteriorated
Stopped work, operating present invention device 1 and reactor 2 load and unload agent 2 times respectively.
Comparative example 1
According to the technological process described in Fig. 1, the first weighted BMO spaces that weighted BMO spaces reaction zone includes changeable operation react
Area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone set a reactor 1, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction, weighted BMO spaces reaction zone reactor（It is online to only have a reactor in operation process）In be filled with catalyst A, catalysis
Agent B and catalyst C, the admission space ratio of each catalyst is 2: 7: 1.In hydrotreating reaction area reactor 3 equipped with catalyst B and
Catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, and a loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is less than hydrotreating zone, and specific reaction condition is shown in Table
3.Feedstock oil A is not controlled followed by reactor 1, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4
The metal of weighted BMO spaces reaction zone outlet processed effluent（Ni+V）Content.Sulphur in hydrogenated back end hydrogenation processing reaction zone effluent
Content is 0.22 weight %, nitrogen content is 1829 μ g/g, carbon residue is 4.58 weight %, metal（Ni+V）Content is 8.3 μ g/g.Fortune
Turn 10 months after, in the reactor 1 of the first weighted BMO spaces reaction zone the pressure drop of at least one catalyst bed reach in pressure drop
There is hot spot in limit or catalyst bed, cut out, and the reactor 2 for cutting the second weighted BMO spaces reaction zone has continued
Into hydroprocessing processes（Feedstock oil A is followed by reactor 2, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 at this time
With reactor 4）, device still even running, generates oil quality and disclosure satisfy that downstream RFCC feed needs.After switching reactor 2,
Device has operated 8 months again, is stopped work since product quality is deteriorated, and the final device has operated 18 months.
Embodiment 2
According to the technological process described in Fig. 2, a weighted BMO spaces reaction zone is only set, is set in this weighted BMO spaces reaction zone
A reactor 1 is put, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series, and weighted BMO spaces reaction zone
Loaded catalyst accounts for the 36% of device catalyst total filling amount.According to Flow of Goods and Materials direction, weighted BMO spaces reaction zone reactor
Catalyst A, catalyst B and catalyst C are filled with 1, the admission space ratio of three kinds of catalyst is 2: 6: 2.Hydrotreating reaction
Catalyst B and catalyst C is housed, the admission space ratio of two kinds of catalyst is 3: 7, filling catalysis in reactor 4 in area's reactor 3
Agent C and catalyst D, the admission space ratio of two kinds of catalyst is 3: 7.The condition and result of the test of reactor hydrotreating are listed in table
2。
In operation process, the reaction temperature of weighted BMO spaces reaction zone is high compared with hydrotreating zone, and specific reaction condition is shown in Table
3.Feedstock oil A controls weighted BMO spaces reaction zone outlet effluent followed by reactor 1, reactor 3 and reactor 4
Metal（Ni+V）Content is not higher than 29 μ g/g.Sulfur content is 0.23 weight %, nitrogen in hydrogenated back end hydrogenation processing reaction zone effluent
Content is 2186 μ g/g, carbon residue is 4.80 weight %, metal（Ni+V）Content is 8.7 μ g/g.After operating 12 months, due to production
Quality is deteriorated and is stopped work, and the pressure drop of reactor 1 at this time has reached the 85% of the pressure drop upper limit.
Comparative example 2
According to the technological process described in Fig. 2, a weighted BMO spaces reaction zone is only set, is set in this weighted BMO spaces reaction zone
A reactor 1 is put, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series, and weighted BMO spaces reaction zone
Loaded catalyst accounts for the 24% of device catalyst total filling amount.According to Flow of Goods and Materials direction, weighted BMO spaces reaction zone reactor
Catalyst A and catalyst B are filled with 1, the admission space ratio of two kinds of catalyst is 3: 7.In hydrotreating reaction area reactor 3
Equipped with catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 3: 7, loading catalyst C and catalyst in reactor 4
D, the admission space ratio of two kinds of catalyst is 2: 8.The condition and result of the test of hydrotreating are listed in table 2.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is less than hydrotreating zone, and specific reaction condition is shown in Table
3.Feedstock oil A does not control weighted BMO spaces reaction zone to export effluent followed by reactor 1, reactor 3 and reactor 4
Metal（Ni+V）Content.Sulfur content is 0.24 weight %, nitrogen content 2276 in hydrogenated back end hydrogenation processing reaction zone effluent
μ g/g, carbon residue are 4. 85 weight %, metal（Ni+V）Content is 8.8 μ g/g.After operating 12 months, since product quality is deteriorated
Stopped work, the pressure drop of reactor 1 at this time has reached the 85% of the pressure drop upper limit.
Embodiment 3
According to the technological process described in Fig. 1, the first weighted BMO spaces that weighted BMO spaces reaction zone includes changeable operation react
Area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone set a reactor 1, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction, weighted BMO spaces reaction zone（It is online to only have a weighted BMO spaces reaction zone in operation process）It is filled with and urges in reactor
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst is 3: 6: 1.Filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 3: 7, loading catalyst C and catalyst D in reactor 4,
The admission space ratio of two kinds of catalyst is 2: 8.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is high compared with hydrotreating zone, and specific reaction condition is shown in Table
Continuous 3.Feedstock oil B is controlled followed by reactor 1, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4
The metal of weighted BMO spaces reaction zone outlet processed effluent（Ni+V）Content is not higher than 20 μ g/g.Hydrogenated back end hydrogenation processing reaction
Sulfur content is 0.21 weight % in area's effluent, nitrogen content is 1424 μ g/g, carbon residue is 3.81 weight %, metal（Ni+V）Content
For 9.5 μ g/g.After operating 3 months, the reactor 1 of the first weighted BMO spaces reaction zone exports the metal of effluent（Ni+V）Content
Pressure drop more than at least one catalyst bed in 20 μ g/g or reactor 1, which reaches, there is heat in the pressure drop upper limit or catalyst bed
Point, is cut out, and the reactor 2 for cutting the second weighted BMO spaces reaction zone continues to complete hydroprocessing processes（It is former at this time
Expect oil B followed by reactor 2, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4）, device is still flat
Steady operation, generation oil quality disclosure satisfy that downstream RFCC feed needs.When the reactor 2 of the second weighted BMO spaces reaction zone exports
The metal of effluent（Ni+V）Pressure drop of the content more than at least one catalyst bed in 20 μ g/g or reactor 2 reaches in pressure drop
When occurring the hot spot that can not continue operation in limit or catalyst bed, cut out, while cut the reaction of the first weighted BMO spaces
The reactor 1 in area continues to complete hydroprocessing processes, while replaces urging in the reactor 2 of the second weighted BMO spaces reaction zone
Agent, it is stand-by to reload fresh catalyst.So circulation, the final device have operated 12 months, since product quality is deteriorated
Stopped work, operating present invention device 1 and reactor 2 load and unload agent 2 times respectively.
Comparative example 3
According to the technological process described in Fig. 2, a weighted BMO spaces reaction zone is only set, is set in this weighted BMO spaces reaction zone
A reactor 1 is put, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials direction,
Catalyst A and catalyst B are filled with weighted BMO spaces reaction zone reactor 1, the admission space ratio of two kinds of catalyst is 3: 7.
Catalyst B and catalyst C is housed, the admission space ratio of two kinds of catalyst is 5: 5, reaction in hydrotreating reaction area reactor 3
Loading catalyst C and catalyst D in device 4, the admission space ratio of two kinds of catalyst is 4: 6.The condition and experiment knot of hydrotreating
Fruit is listed in table 2.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is less than hydrotreating zone, and specific reaction condition is shown in continuous
Table 3.Feedstock oil B does not control weighted BMO spaces reaction zone outlet outflow followed by reactor 1, reactor 3 and reactor 4
The metal of thing（Ni+V）Content.In hydrogenated back end hydrogenation processing reaction zone effluent sulfur content be 0.26 weight %, nitrogen content be
1687 μ g/g, carbon residue are 4.23 weight %, metal（Ni+V）Content is 15.5 μ g/g.After operating 6 months, due to product quality
Variation is stopped work, and the pressure drop of reactor 1 at this time has reached the 85% of the pressure drop upper limit.
Embodiment 4
According to the technological process described in Fig. 1, the first weighted BMO spaces that weighted BMO spaces reaction zone includes changeable operation react
Area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone set a reactor 1, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction, weighted BMO spaces reaction zone reactor（It is online to only have a reactor in operation process）In be filled with catalyst A, catalysis
Agent B and catalyst C, the admission space ratio of each catalyst is 4: 5: 1.In hydrotreating reaction area reactor 3 equipped with catalyst B and
Catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, a loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is high compared with hydrotreating zone, and specific reaction condition is shown in continuous
Table 3.Feedstock oil C is controlled followed by reactor 1, high-pressure separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4
The metal of weighted BMO spaces reaction zone outlet processed effluent（Ni+V+Fe+Ca）Content is not higher than 10 μ g/g.At hydrogenated back end hydrogenation
Sulfur content is 0.16 weight % in reason reaction zone effluent, nitrogen content is 2292 μ g/g, carbon residue is 3.52 weight %, metal（Ni+
V）Content is 4.8 μ g/g, and metal Ca contents are 0.5 μ g/g, and metal Fe contents are 0.2 μ g/g.After operating 4 months, the first hydrogenation
The reactor 1 in pretreatment reaction area exports the metal of effluent（Ni+V+Fe+Ca）Content more than in 10 μ g/g or reactor 1 extremely
The pressure drop of a few catalyst bed, which reaches in the pressure drop upper limit or catalyst bed, there is hot spot, is cut out, and cut second
The reactor 2 of weighted BMO spaces reaction zone continues to complete hydroprocessing processes（Feedstock oil C is followed by reactor 2, height at this time
Press separator 5, mixed hydrogen tank 6, reactor 3, mixed hydrogen tank 7 and reactor 4）, device still even running, generating oil quality can expire
Foot trip RFCC feed needs.When the reactor 2 of the second weighted BMO spaces reaction zone exports the metal of effluent（Ni+V+Fe+
Ca）Pressure drop of the content more than at least one catalyst bed in 10 μ g/g or reactor 2 reaches the pressure drop upper limit or catalyst bed
Interior appearance can not continue operation hot spot when, cut out, at the same cut the first weighted BMO spaces reaction zone reactor 1 come after
It is continuous to complete hydroprocessing processes, while the catalyst in the reactor 2 of the second weighted BMO spaces reaction zone is replaced, reload new
Fresh catalyst is stand-by.So circulation, the final device have operated 16 months, are stopped work, operated since product quality is deteriorated
Present invention device 1 and reactor 2 load and unload agent 2 times respectively.
Comparative example 4
According to the technological process described in Fig. 2, a weighted BMO spaces reaction zone is only set, is set in this weighted BMO spaces reaction zone
A reactor 1 is put, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials direction,
Catalyst A and catalyst B are filled with weighted BMO spaces reaction zone reactor 1, the admission space ratio of two kinds of catalyst is 4: 6.
Catalyst B and catalyst C is housed, the admission space ratio of two kinds of catalyst is 1: 9, reaction in hydrotreating reaction area reactor 3
Loading catalyst C and catalyst D in device 4, the admission space ratio of two kinds of catalyst is 1: 9.The condition and experiment knot of hydrotreating
Fruit is listed in table 2.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is less than hydrotreating zone, and specific reaction condition is shown in continuous
Table 3.Feedstock oil C does not control weighted BMO spaces reaction zone outlet outflow followed by reactor 1, reactor 3 and reactor 4
The metal of thing（Ni+V+Fe+Ca）Content.Sulfur content is 0.21 weight % in hydrogenated back end hydrogenation processing reaction zone effluent, nitrogen contains
It is 3.98 weight %, metal to measure as 2936 μ g/g, carbon residue（Ni+V）Content is 6.3 μ g/g, and metal Ca contents are 1.8 μ g/g, gold
It is 0.5 μ g/g to belong to Fe contents.After operating 8 months, since the pressure drop of reactor 1 reaches the pressure drop upper limit, device is forced to stop work.
The condition and result of the test of 3 hydrotreating of table
| Embodiment 1 | Comparative example 1 | Embodiment 2 | Comparative example 2 | |
| Feedstock oil | Feedstock oil A | Feedstock oil A | Feedstock oil A | Feedstock oil A |
| Pretreating zone operator scheme | Switching | Switching | Do not switch | Do not switch |
| Process conditions | ||||
| Hydrogen dividing potential drop, MPa | 14.5 | 14.5 | 14.5 | 14.5 |
| Reaction temperature, DEG C | ||||
| Reactor 1 | 390 | 373 | 385 | 373 |
| Reactor 2 | 390 | 373 | ||
| Reactor 3 | 372 | 376 | 375 | 379 |
| Reactor 4 | 376 | 383 | 378 | 385 |
| CAT | 378 | 378 | 380 | 380 |
| Weighted BMO spaces area volume space velocity, h-1 | 0.83 | 0.83 | 0.56 | 0.83 |
| Hydrotreating zone volume space velocity, h-1 | 0.40 | 0.40 | 0.31 | 0.26 |
| Weighted BMO spaces area hydrogen to oil volume ratio, Nm3/m3 | 700 | 700 | 700 | 700 |
| Hydrotreating zone liquid phase circulation ratio, % | 0.6:1 | 0.6:1 | - | - |
| Reaction generation oil nature | ||||
| Sulphur, weight % | 0.20 | 0.22 | 0.23 | 0.24 |
| Nitrogen, μ g/g | 1712 | 1829 | 2186 | 2276 |
| Carbon residue, weight % | 4.42 | 4.58 | 4.80 | 4.85 |
| Nickel+vanadium, μ g/g | 7.0 | 8.3 | 8.7 | 8.8 |
| Calcium, μ g/g | ||||
| Iron, μ g/g | ||||
| Service cycle, the moon | 24 | 18 | 12 | 12 |
| Reactor 1 fills agent number, secondary | 2 | 1 | 1 | 1 |
| Reactor 2 fills agent number, secondary | 2 | 1 | - | - |
| Reactor 3 and 4 fills agent number, secondary | 1 | 1 | 1 | 1 |
The condition and result of the test of 3 hydrotreating of continued
| Embodiment 3 | Comparative example 3 | Embodiment 4 | Comparative example 4 | |
| Feedstock oil | Feedstock oil B | Feedstock oil B | Feedstock oil C | Feedstock oil C |
| Pretreating zone operator scheme | Switching | Do not switch | Switching | Do not switch |
| Process conditions | ||||
| Hydrogen dividing potential drop, MPa | 14.5 | 14.5 | 14.5 | 14.5 |
| Reaction temperature, DEG C | ||||
| Reactor 1 | 390 | 380 | 386 | 373 |
| Reactor 2 | 390 | 386 | ||
| Reactor 3 | 374 | 384 | 375 | 378 |
| Reactor 4 | 378 | 389 | 377 | 382 |
| CAT | 380 | 385 | 378 | 378 |
| Weighted BMO spaces area volume space velocity, h-1 | 0.71 | 0.83 | 0.89 | 0.83 |
| Hydrotreating zone volume space velocity, h-1 | 0.60 | 0.26 | 0.52 | 0.26 |
| Weighted BMO spaces area hydrogen to oil volume ratio, Nm3/m3 | 700 | 700 | 700 | 700 |
| Hydrotreating zone liquid phase circulation ratio, % | 1:1 | 1:1 | ||
| Reaction generation oil nature | ||||
| Sulphur, weight % | 0.21 | 0.26 | 0.16 | 0.21 |
| Nitrogen, μ g/g | 1424 | 1687 | 2292 | 2936 |
| Carbon residue, weight % | 3.81 | 4.23 | 3.52 | 3.98 |
| Nickel+vanadium, μ g/g | 9.5 | 15.5 | 4.8 | 6.3 |
| Calcium, μ g/g | 0.5 | 1.8 | ||
| Iron, μ g/g | 0.2 | 0.5 | ||
| Service cycle, the moon | 12 | 6 | 16 | 8 |
| Reactor 1 fills agent number, secondary | 2 | 1 | 2 | 1 |
| Reactor 2 fills agent number, secondary | 2 | - | 2 | - |
| Reactor 3 and 4 fills agent number, secondary | 1 | 1 | 1 | 1 |
In order to further investigate influence of the technology to hydrotreating reaction area catalyst of the present invention, respectively to embodiment 1,
Catalyst C and catalyst D after comparative example 1, embodiment 2 and the operating of comparative example 2 are dissected, and the results are shown in Table 4 and table 5.
4 catalyst C of table operatings are front and rear to dissect result
| Specific surface area, m2·g-1 | Pore volume, cm3·g-1 | Average pore size, nm | Carbon deposition quantity, g/100mL | Metal deposition capability, g/100mL | |
| Fresh dose | 180.0 | 0.55 | 12.2 | - | - |
| Deactivator | |||||
| Embodiment 1 | 110.2 | 0.20 | 7.3 | 20.16 | - |
| Comparative example 1 | 115.2 | 0.22 | 7.6 | 18.38 | - |
| Embodiment 2 | 124.1 | 0.29 | 9.3 | 10.26 | - |
| Comparative example 2 | 125.2 | 0.28 | 8.9 | 12.31 | - |
| Regenerative agent | |||||
| Embodiment 1 | 167.6 | 0.49 | 11.7 | 0.09 | 1.11 |
| Comparative example 1 | 147.5 | 0.40 | 10.8 | 0.21 | 5.36 |
| Embodiment 2 | 170.1 | 0.50 | 11.8 | 0.12 | 2.23 |
| Comparative example 2 | 145.3 | 0.38 | 10.5 | 0.26 | 6.11 |
5 catalyst D of table dissects result
| Specific surface area, m2·g-1 | Pore volume, cm3·g-1 | Average pore size, nm | Carbon deposition quantity, g/100mL | Metal deposition capability, g/100mL | |
| Fresh dose | 225.0 | 0.48 | 8.5 | - | - |
| Deactivator | |||||
| Embodiment 1 | 117.7 | 0.16 | 5.4 | 26.14 | - |
| Comparative example 1 | 122.6 | 0.17 | 5.5 | 24.53 | - |
| Embodiment 2 | 129.2 | 0.21 | 6.5 | 15.36 | - |
| Comparative example 2 | 130.1 | 0.20 | 6.1 | 18.24 | - |
| Regenerative agent | |||||
| Embodiment 1 | 214.8 | 0.44 | 8.2 | 0.18 | 0.79 |
| Comparative example 1 | 204.5 | 0.40 | 7.8 | 0.35 | 3.44 |
| Embodiment 2 | 217.2 | 0.45 | 8.3 | 0.22 | 1.45 |
| Comparative example 2 | 188.4 | 0.36 | 7.6 | 0.44 | 4.10 |
As seen from the above analysis, by varying catalyst system and operator scheme, i.e., by the prior art according to logistics direction
Low early and high after trend is presented in reaction temperature（Comparative example 2）, change into low after height before being presented according to logistics orienting response temperature
Trend（Embodiment 2）, while product quality is ensured, the activity of all catalyst can be made full use of, due to being hydrogenated with pre- place
Reason reaction zone is stripped of most of metal impurities in material so that desulphurization catalyst and/or denitrogenation in hydrotreating reaction area
The deactivation cause of catalyst is effectively carried from being changed into only coking deactivation using the metal deposit and coking deactivation of existing process technology
The high utilization rate of desulphurization catalyst and/or denitrification catalyst, while also so that desulphurization catalyst and denitrification catalyst can make
With regeneration treatment is carried out after a cycle, reuse, saved catalyst buying expenses, improved economy, when hydrogenation is pre-
Handle reaction zone and carry out changeable operation（Embodiment 1）Afterwards, the advantage of the method for the present invention is more obvious, can greatly increase device
The cycle of operation.
Further, since the sulfur content, carbon residue and tenor in this technology product are low compared with existing process technology, this
The not only product quality of positive influences downstream RFCC devices, but also because reducing the tenor in RFCC chargings, additionally it is possible to it is big
Width reduces the catalyst agent consumption of RFCC devices, and additional economic income is brought to enterprise.
Claims (21)
1. a kind of heavy oil hydrogenation treatment method for improving catalyst utilization, including herein below：
（1）At least one weighted BMO spaces reaction zone and a hydrotreating reaction area are provided；Bag in weighted BMO spaces reaction zone
Hydrogenation protecting catalyst and Hydrodemetalation catalyst are included, Hydrobon catalyst is included in hydrotreating reaction area and hydrogenation is de-
Nitrogen catalyst；
（2）Heavy oil feedstock oil enters weighted BMO spaces reaction zone after being mixed first with hydrogen, is carried out under the conditions of weighted BMO spaces
Metal impurities are removed 40wt% ~ 90wt% by hydrogenation reaction, and sulphur is removed 20wt% ~ 70wt%, obtains the reaction of tenor reduction
Effluent；
（3）Step（2）Obtained reaction effluent enters high-pressure separator, isolates gas, liquid two-phase；Separating obtained gas
Through desulfurization and compressor compresses Posterior circle to weighted BMO spaces reaction zone；
（4）Step（3）Obtain product liquid and mixed with the fraction of stream that hydrotreating zone is recycled back to, mixed into mixed hydrogen tank
Hydrogen, the miscella after the molten hydrogen of saturation enter liquid-phase hydrogenatin treatment reactor, under hydroprocessing conditions, are contacted with catalyst
Reaction, obtains the liquid phase effluent of sulfur content and nitrogen content reduction；
（5）Step（4）An obtained liquid phase effluent part is recycled to mixed hydrogen tank, another part bleeder after decompression.
2. in accordance with the method for claim 1, it is characterised in that step（2）The average response temperature of weighted BMO spaces reaction zone
Degree is compared with step（3）The average reaction temperature in hydrotreating reaction area will be higher by 5 DEG C~40 DEG C.
3. in accordance with the method for claim 2, it is characterised in that step（2）The average response temperature of weighted BMO spaces reaction zone
Degree is compared with step（3）The average reaction temperature in hydrotreating reaction area will be higher by 10 DEG C~30 DEG C.
4. in accordance with the method for claim 1, it is characterised in that contain hydrodesulfurization in the weighted BMO spaces reaction zone
Catalyst, the loadings of Hydrobon catalyst account for 0v%~30v% of loaded catalyst in pretreatment reaction area.
5. in accordance with the method for claim 4, it is characterised in that in the weighted BMO spaces reaction zone, according to material
Engagement sequence, Hydrobon catalyst is seated in the downstream of hydrogenation protecting catalyst and Hydrodemetalation catalyst.
6. in accordance with the method for claim 1, it is characterised in that contain hydrodemetallization in the hydrotreating reaction area
Catalyst, the loadings of Hydrodemetalation catalyst usually account for 5v%~30v% of loaded catalyst in hydroconversion reaction zone.
7. in accordance with the method for claim 6, it is characterised in that according to the engagement sequence with material, hydrodemetallisation catalyst
Agent is seated in the upstream of Hydrobon catalyst and hydrodenitrogenation catalyst.
8. in accordance with the method for claim 1, it is characterised in that step（1）The middle more than two weighted BMO spaces of offer are anti-
Area is answered, which is to be arranged in parallel and is changeable operation.
9. in accordance with the method for claim 8, it is characterised in that further include step（5）, when one of weighted BMO spaces are anti-
After answering area to meet service requirement, by short circuit, cut out reaction process, and second weighted BMO spaces reaction zone is cut into work
In skill flow, the weighted BMO spaces reaction zone cut out can carry out the displacement of catalyst, that is, draw off the old catalyst of inactivation, again
Load fresh and/or regenerated catalyst；After second weighted BMO spaces reaction zone of incision cannot meet service requirement,
By in the weighted BMO spaces reaction zone incision technological process for having carried out catalyst replacement, and by second weighted BMO spaces reaction zone
Short circuit, cuts out, and carries out the displacement of catalyst.
10. in accordance with the method for claim 9, it is characterised in that the weighted BMO spaces reaction zone cannot meet that operation will
Seeking Truth refers to：The effluent of weighted BMO spaces reaction zone can not meet the feed needs of downstream hydrogenation treatment region, or weighted BMO spaces
The pressure drop of at least one catalyst bed reaches the pressure drop upper limit in reaction zone, or occurs hot spot in catalyst bed.
11. in accordance with the method for claim 10, it is characterised in that it is described can not meet downstream hydrogenation processing reaction zone into
Expect that required standard is：Tenor in weighted BMO spaces reaction zone effluent liquid has exceeded between the μ g/g of 8 μ g/g~50
Any number；The pressure drop upper limit designs 0.4~0.8 times of maximum pressure drop for reactor；The hot spot refers at least
Radial temperature difference in one catalyst bed reaches 15~50 DEG C.
12. in accordance with the method for claim 1, it is characterised in that the free topped crude of heavy oil feedstock grease separation, oil
One group of material that the hydro carbons for the high asphalt content that residual oil, oil-sand, pitch, shale oil, liquefaction coal or reclaimed oil obtain is formed；Weight
The tenor of oily feedstock oil is more than 30 μ g/g.
13. in accordance with the method for claim 12, it is characterised in that the content of nickel+vanadium is more than in the heavy oil feedstock oil
60 μ g/g and/or iron content are more than 10 μ g/g and/or calcium content is more than 10 μ g/g.
14. in accordance with the method for claim 1, it is characterised in that the property of the Hydrodemetalation catalyst is, with catalysis
On the basis of the gross weight of agent, using the content that oxide is counted as 0.5~15 weight %, the content of cobalt and/or nickel is for molybdenum and/or tungsten
0.3~8 weight %, surplus are alumina support；The alumina support is a kind of bimodal porous aluminum oxide, its pore volume is 0.5
~2.0 mls/g, specific surface area is 120~350 meters2/ gram, aperture accounts for total pore volume 30~90% in 10~30 nanometers of pore volume,
Aperture accounts for total pore volume 10~50% in 100~2000 nanometers of pore volume, bore dia be less than 10 nanometers, between 30-100 nanometers with
And the sum of pore volume more than 2000 nanometers accounts for total pore volume below 20%.
15. in accordance with the method for claim 1, it is characterised in that in weighted BMO spaces reaction zone, hydrogenation protecting catalyst
Admission space ratio with Hydrodemetalation catalyst is 5:95~95:5.
16. in accordance with the method for claim 1, it is characterised in that in weighted BMO spaces reaction zone, Hydrobon catalyst
Loadings are 5v%~30v% of Hydrodemetalation catalyst loadings.
17. in accordance with the method for claim 1, it is characterised in that the property of the Hydrobon catalyst is, with catalysis
On the basis of the gross weight of agent, molybdenum and/or tungsten and using the content that oxide is counted as 10~25 weight %, the content of cobalt and/or nickel is 1
~6 weight %, surplus are alumina support.
18. according to any methods of claim 1-3, it is characterised in that the reaction condition of weighted BMO spaces reaction zone is,
Reaction pressure is 5MPa~35MPa, and average reaction temperature is 340 DEG C~430 DEG C, and volume space velocity is 0.1h during liquid-1~5.0h-1,
Hydrogen to oil volume ratio is 200~2000.
19. in accordance with the method for claim 1, it is characterised in that in the hydrotreating reaction area, hydrodesulfurization catalytic
The admission space of agent and hydrodenitrogenation catalyst ratio is 20:80~80:20.
20. according to any methods of claim 1-3, it is characterised in that the reaction condition in hydrotreating reaction area is, instead
It is 5MPa~35MPa to answer pressure, and average reaction temperature is 320 DEG C~420 DEG C, and volume space velocity is 0.1h during liquid-1~5.0h-1, liquid
Mutually circulation mass ratio 0.1:1~10:1.
21. in accordance with the method for claim 1, it is characterised in that the weighted BMO spaces reaction zone set one or
Multiple hydrogenation protecting reactors, each hydrogenation protecting reactor is at least provided with a hydrogenation protecting catalyst bed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610968483.3A CN108018074B (en) | 2016-11-01 | 2016-11-01 | Heavy oil hydrotreating method for improving catalyst utilization rate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610968483.3A CN108018074B (en) | 2016-11-01 | 2016-11-01 | Heavy oil hydrotreating method for improving catalyst utilization rate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108018074A true CN108018074A (en) | 2018-05-11 |
| CN108018074B CN108018074B (en) | 2020-10-16 |
Family
ID=62084554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610968483.3A Active CN108018074B (en) | 2016-11-01 | 2016-11-01 | Heavy oil hydrotreating method for improving catalyst utilization rate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108018074B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109652122A (en) * | 2018-12-31 | 2019-04-19 | 中海油天津化工研究设计院有限公司 | A kind of method of poor quality high nitrogen heavy distillate deep hydrogenation denitrogenation |
| CN113046117A (en) * | 2019-12-26 | 2021-06-29 | 中国石油化工股份有限公司 | Heavy oil hydrotreating process |
| WO2022089521A1 (en) | 2020-10-28 | 2022-05-05 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reaction system and heavy oil hydrogenation method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993720A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Liquid phase hydrogenating method of hydrocarbon oil |
| CN102453530A (en) * | 2010-10-26 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrogenation method for processing heavy oil |
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN103540350A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Hydrotreating combined process for inferior heavy oil and residual oil |
| CN103540348A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Efficient hydrotreating process for inferior heavy oil and residual oil |
| CN103540349A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Low-quality heavy oil and residual oil hydrotreatment combined process capable of prolonging service life of catalyst |
-
2016
- 2016-11-01 CN CN201610968483.3A patent/CN108018074B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993720A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Liquid phase hydrogenating method of hydrocarbon oil |
| CN102453530A (en) * | 2010-10-26 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrogenation method for processing heavy oil |
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN103540350A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Hydrotreating combined process for inferior heavy oil and residual oil |
| CN103540348A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Efficient hydrotreating process for inferior heavy oil and residual oil |
| CN103540349A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Low-quality heavy oil and residual oil hydrotreatment combined process capable of prolonging service life of catalyst |
Non-Patent Citations (1)
| Title |
|---|
| 李大东: "《加氢处理工艺与工程》", 31 December 2004, 中国石化出版社 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109652122A (en) * | 2018-12-31 | 2019-04-19 | 中海油天津化工研究设计院有限公司 | A kind of method of poor quality high nitrogen heavy distillate deep hydrogenation denitrogenation |
| CN109652122B (en) * | 2018-12-31 | 2021-02-23 | 中海油天津化工研究设计院有限公司 | Deep hydrogenation denitrification method for inferior high-nitrogen heavy distillate oil |
| CN113046117A (en) * | 2019-12-26 | 2021-06-29 | 中国石油化工股份有限公司 | Heavy oil hydrotreating process |
| CN113046117B (en) * | 2019-12-26 | 2023-01-10 | 中国石油化工股份有限公司 | Heavy oil hydrotreating process |
| WO2022089521A1 (en) | 2020-10-28 | 2022-05-05 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reaction system and heavy oil hydrogenation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108018074B (en) | 2020-10-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102876377B (en) | Hydrotreatment and catalytic cracking combined method of heavy hydrocarbon raw material | |
| CN103059938B (en) | A kind of heavy hydrocarbon hydroprocessing method | |
| CN101591565A (en) | A kind of hydrofinishing process of inferior patrol | |
| CN100526431C (en) | Single-section two-catalyst hydrocracking method | |
| CN106701190B (en) | A kind of process handling low grade oils | |
| CN102899081A (en) | Wax oil hydrotreating method | |
| CN108018074A (en) | Improve the heavy oil hydrogenation treatment method of catalyst utilization | |
| CN108018084A (en) | A kind of heavy oil hydrogenation treatment method for improving catalyst utilization | |
| CN1990830B (en) | hydrorefining method for coker gasoline | |
| CN101434867A (en) | Suspension bed residual oil hydrogenation-catalytic cracking combined technological process | |
| CN101376841A (en) | Heavy fraction oil hydrotreating method | |
| CN108003919A (en) | A kind of heavy oil hydrogenation treatment method for lifting catalyst utilization | |
| CN114644940B (en) | Method for producing bunker fuel oil by hydrogenation | |
| CN110408429B (en) | Method for treating heavy oil by combined process | |
| CN106701189B (en) | A kind of hydrogenation and catalystic cracking combined process for residual oil | |
| CN110408431B (en) | Method for treating inferior oil product by combined process | |
| CN110408432B (en) | Method for treating inferior residual oil by combined process | |
| CN108003928A (en) | A kind of Heavy oil hydrogenation method for improving catalyst utilization | |
| CN108003924A (en) | Improve the Heavy oil hydrogenation method of catalyst utilization | |
| CN112210401B (en) | Tandem and alternative residual oil hydrotreating-catalytic cracking combined process method and system | |
| CN107875978B (en) | Grading filling method and application of hydrogenation catalyst | |
| CN112210400B (en) | Combined process method and system capable of changing residual oil hydrotreating-catalytic cracking | |
| CN110408428B (en) | Method for treating residual oil by combined process | |
| CN110408430A (en) | A kind of method of group technology processing heavy hydrocarbon | |
| CN111676058B (en) | Residual oil hydrogenation reactor with alternately changed material flow directions, residual oil hydrogenation system comprising reactor and residual oil hydrogenation process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |