CN109722284A - A kind of pretreated method of heavy oil - Google Patents
A kind of pretreated method of heavy oil Download PDFInfo
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- CN109722284A CN109722284A CN201711020632.4A CN201711020632A CN109722284A CN 109722284 A CN109722284 A CN 109722284A CN 201711020632 A CN201711020632 A CN 201711020632A CN 109722284 A CN109722284 A CN 109722284A
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Abstract
The invention discloses a kind of pretreated methods of heavy oil.This method comprises the following steps: a) heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；B) composite modifier is added in the visbreaking residue that step a) is obtained, continuous sedimentation then is carried out to mixture, top obtains overflow material, and lower part obtains underflow materials；Composite modifier composition is as follows: polyacrylamide, bis- salicylidene propane diamine of aluminium polychloride, 2,6- di-tert-butyl-4-methy phenol and N, N'-, and weight ratio is (10 ~ 40): (30 ~ 70): (10 ~ 100): (0.5 ~ 3)；The additional amount of composite modifier accounts for the 0.01% ~ 0.2% of step a) heavy oil feedstock weight.The method of the present invention has many advantages, such as that equipment operation expense is low, separative efficiency is high, while can be improved the yield of overflow component, and is conducive to weaken the influence in subsequent fixed bed hydroprocessing treatment process to catalyst activity stability.
Description
Technical field
The present invention relates to located in advance before a kind of pretreated method of heavy oil, the especially processing of inferior heavy oil fixed bed hydrogenation
The method of reason.
Background technique
Crude resources gradually tends to heaviness, in poor quality in world wide, it is contemplated that heavy crude reserves account for entirely after the year two thousand twenty
Ball can adopt 50% of crude oil reserve or so, and the utilization of heavy oil highly-efficient processing is the significant challenge that oil refining industry faces.According to technique mistake
The difference of journey, existing processing of heavy oil technique can be generalized into three classes in the world at present: (1) stream based on coking
Journey；(2) process based on solvent deasphalting；(3) process based on hydrotreating.
Coking is most thorough decarbonizing process, and can directly process the technology of all inferior heavy oils at present, but
It is the low value coke that coking can generate 30% or so, i.e., oil is partially converted into coke, the light Fuel of coking is also necessary
By further refining the product that could become qualified.The economic benefit of refinery is not only influenced in this way, but also wastes a large amount of treasured
Expensive petroleum resources.Solvent de-asphalting process belongs to physical process, predominantly catalytic cracking and be hydrocracked etc. techniques provide it is former
Material, or a necessary links as lubricating oil processing.Solvent de-asphalting process does not generate light Fuel, and technique directly
It is complicated for operation, energy consumption is higher, so not obtaining extensive development as processing of heavy oil means, main application fields are limited in life
Produce crude lube stock.Heavy-oil hydrogenation processing is the important means of heavy oil modification and lighting, has good product quality, light oil yield
The advantages that higher, combining with catalytic cracking process can be by heavy oil drastic cracking at light Fuel.Technology development in recent years is very
Fastly, become the heavy oil deep processing method run neck and neck with catalytic cracking.
No matter we are intended to the maximum amount of lighting of heavy oil, the fixed bed hydrogenation of technology maturation using which kind of technology
Technology be can yet be regarded as optimal selection at this stage.But restriction of the application by raw material oil nature of the technology is not capable of processing metal, residual
The higher heavy charge of carbon content.By taking fixed bed heavy-oil hydrogenation technology as an example, tenor can only be processed lower than 150 μ g/g, residual
Charcoal is lower than 15% heavy oil.In fact when tenor is higher than 150 μ g/g, the service life of catalyst has just been seriously affected.It wants
Want to allow fixed bed hydrogenation technology that can process more inferior heavy oils, generally there are two approach: first is that developing completely new catalysis
Agent increases substantially the appearance metal ability of catalyst, extends the service life of catalyst；Second is that being located in advance to inferior heavy oil
Reason, improves the property of inferior heavy oil, is allowed to meet the feed needs of fixed bed hydrogenation technology.
As that studies inferior heavy oil deepens continuously, people are gradually had found, seriously affect inferior heavy oil quality metal,
The heteroatomic distribution such as sulphur, nitrogen, oxygen has certain rule, i.e., most sulphur, nitrogen, oxygen and most metals are concentrated
In the asphalitine of decompression residuum.So poor residuum can be separated into using means appropriate and meet fixed bed hydrogenation skill
The raw material of art.Solvent deasphalting is exactly one of the technological means using this principle, but solvent de-asphalting process is complicated, energy consumption
Height realizes difficulty, and deasphalted oil viscosity is big, needs to mix light-end products to reduce viscosity, thus reduces fixed bed dress
The efficiency set.
CN 103102934A discloses a kind of pretreated method of inferior heavy oil, and wherein inferior heavy oil raw material enters visbreaking
Cracking unit carries out appropriate visbreaking, then mixes with light naphtha after reducing viscosity, will by centrifugal force into centrifugal separating device
Visbreaking generates oil and is separated into overflow component and underflow component, and overflow component mixes the charging as fixed bed hydrogenation device.The party
Method can effectively pre-process inferior heavy hydrocarbon raw material, to obtain the acceptable material of fixed bed hydrogenation device.But the party
Method needs to be added a large amount of light solvents and is diluted, and visbreaking residue is still in more stable balance each other, low separation efficiency,
To reach higher separation rate, it is necessary to which plural serial stage increases equipment investment and energy consumption.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of preprocess methods of heavy oil.The method of the present invention is especially suitable
For the preprocess method of inferior heavy oil, this method has many advantages, such as that equipment operation expense is low, separative efficiency is high, while can mention
The yield of high overflow material, and be conducive to weaken the shadow in subsequent fixed bed hydroprocessing treatment process to catalyst activity stability
It rings.
The pretreated method of heavy oil of the present invention, comprising:
A) heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；
B) composite modifier is added in the visbreaking residue that step a) is obtained, continuous sedimentation then is carried out to mixture, on
Portion obtains overflow material, and lower part obtains underflow materials；
Wherein, composite modifier composition is as follows: polyacrylamide (CPAM), aluminium polychloride (PAC), 2,6- di-t-butyl -4-
Bis- salicylidene propane diamine of methylphenol (BHT) and N, N'-, weight ratio are (10 ~ 40): (30 ~ 70): (10 ~ 100):
(0.5 ~ 3).
The additional amount of the step b) composite modifier accounts for the 0.01% ~ 0.2% of step a) heavy oil feedstock weight, excellent
Select 0.05% ~ 0.1%.
Heavy oil feedstock described in step a) includes reduced crude, decompression residuum, deasphalted oil, oil sands bitumen, thick original
One or more of oil, coal tar and coal liquefaction heavy oil.
In heavy oil feedstock described in step a), tenor is greater than 150 μ g/g, colloid and pitch with the poidometer of Ni and V
The total content of matter is greater than 50wt%.
Visbreaking described in step a) use either shallow thermal cracking process, process condition are as follows: reaction temperature be 350 ~
450 DEG C, reaction pressure is 0.1 ~ 1.5 MPa, and the weight conversion rate of visbreaking is 1% ~ 40%；Preferred operating condition are as follows:
Reaction temperature is 400 ~ 450 DEG C, 0.5 ~ 1.5 MPa of reaction pressure, the weight conversion rate 10% ~ 20% of visbreaking.Wherein,
Light component (fraction that boiling point is lower than heavy oil feedstock) weight that conversion ratio is obtained by visbreaking accounts for the percentage of heavy oil feedstock weight
Number.
Composite modifier composition in step b): polyacrylamide (CPAM), aluminium polychloride (PAC), bis- uncle of 2,6-
Bis- salicylidene propane diamine of butyl -4- methylphenol (BHT) and N, N'-, weight ratio is preferably (15 ~ 35): (35 ~
65): (55 ~ 85): (1 ~ 2).
Continuous sedimentation in step b) uses Gravity Separation principle, and continuous sedimentation device uses high-efficiency thickener or cone
Deep concentrator, by the conditional operation of separation of solid and liquid, the material that wherein overflow material, that is, continuous sedimentation device overflow outlet is discharged, bottom
Flow material, that is, continuous sedimentation device underflow outlet discharge material.The operation temperature of continuous sedimentation device is 0 ~ 100 DEG C, preferably
70~ 80℃.Continuous sedimentation device operating pressure is the pressure for keeping being added that composite modifier is liquid phase at the operational.
Continuous sedimentation device obtains overflow material and underflow materials in step b), and overflow material volume yield is with the company
60% ~ 90% on the basis of continuous sedimentation device feed volume, preferably 65% ~ 90%.Metal impurities are substantially reduced in overflow material,
It can be used as the charging of fixed bed hydrogenation device after filter device.The biggish heavy constituent of underflow materials studies on asphaltene isodensity
Most of metal impurities are enriched in heavy oil, can be used as the charging of delayed coking unit.
Compared with prior art, the pretreated method of heavy oil of the present invention has the advantages that
(1) in the method for the present invention step a), heavy oil feedstock enters viscosity breaking plant and carries out visbreaking, and control reaction is deep
Degree, slagging prevention make the asphalitine in visbreaking residue reach a higher content；
(2) in the method for the present invention step b), continuous sedimentation is carried out to visbreaking residue using composite modifier, utilizes step a)
The visbreaking residue stability of generation is poor, gel phase disequilibration determines this feature, and composite modifier is added, passes through polyacrylamide
Amine (CPAM), aluminium polychloride (PAC), 2,6- di-tert-butyl-4-methy phenol (BHT) and bis- salicylidene of N, N'- the third two
Cooperation synergistic effect between amine, further destroys the balance of continuous phase and dispersed phase, prevents most of asphalitine from system
In steadily peptization and aggregation separation occurs, from it is original it is single homogeneously become two-phase, cause asphaltene precipitation to come out, mention significantly
High separating rate and separative efficiency, effectively remove the asphalitine component rich in impurity such as metal, sulphur, nitrogen, oxygen in inferior heavy oil,
Meanwhile the synergistic effect of composite modifier can also inhibit the activity of the active metallic ion in oil product, prevent in infall process
Middle colloid is oxidized to asphalitine too much, to improve overflow material yield, and also helps the gold contained in overflow material
Belong to impurity (such as nickel, vanadium, copper) to be easier to remove during subsequent residual hydrocracking, and reduces steady to catalyst activity
Qualitatively influence.
Detailed description of the invention
Fig. 1 is the flow diagram of heavy oil of the present invention pretreatment and hydrogenation combination technique；
In figure: 1- heavy oil feedstock, 2- viscosity breaking plant, 3- composite modifier, 4- continuous sedimentation device, the makeup of 5- delay coke
It sets, 6- fixed bed hydrogenation device.
Specific embodiment
For the technical solution that the present invention is further explained, it is described in detail below in conjunction with Fig. 1.
As shown in Figure 1, a kind of technical process of the invention are as follows: heavy oil feedstock 1 enters the progress visbreaking of viscosity breaking plant 2 and splits
Change, obtains visbreaking residue.Visbreaking residue is mixed into continuous sedimentation device 4 with composite modifier 3 and is separated, and is separated into overflow
Material and underflow materials.Overflow material meets the feed needs of fixed bed hydrogenation processing after filtering, can be used as fixed bed and adds
The charging of hydrogen production device 6.Underflow materials can enter delayed coking unit 5 and carry out pyrogenetic reaction.
Below with reference to embodiment to further illustrate the technical scheme of the present invention and technical effect, but it is not limited to following reality
Apply example.Refer to that timing to pressure drop reaches the design value shut-down time used since feedstock operation cycle of the invention.
Embodiment 1
The present embodiment is a kind of embodiment of vacuum residuum feed preprocess method.Vacuum residuum feed enters visbreaking dress
Set carry out visbreaking.After appropriate visbreaking, visbreaking residue is obtained.Composite modifier is added into visbreaking residue, adds
The composite modifier entered is by polyacrylamide (CPAM), aluminium polychloride (PAC), 2,6 di tert butyl 4 methyl phenol
(BHT) and bis- salicylidene propane diamine of N, N'- mixing composition, weight ratio 20:40:60:1, composite modifier add
Enter 0.05% that amount is vacuum residuum feed weight.The mixture enters continuous sedimentation device and carries out continuous sedimentation, and operating condition is such as
Under: 80 DEG C of temperature, operating pressure is the pressure for keeping being added that composite modifier is liquid phase at the operational.It is filled in continuous sedimentation
It sets overflow to export to obtain overflow material, overflow material volume yield is 70%, obtains underflow object in continuous sedimentation device underflow outlet
Material.
It tests the vacuum residuum feed property used and is listed in table 1.The residual oil raw material viscosity, carbon residue, metal contain as shown in Table 1
Amount is very high, is with the unmanageable inferior raw material of conventional residual hydrogenation equipment.Visbreaking experimental condition and test result are shown in
Table 2, visbreaking residue (> 350 DEG C of fractions) property are shown in Table 3, and overflow material property is shown in Table 4.
The overflow material of embodiment 1 is fixed the test result of a residual hydrogenation, reaction condition and operating 500 hours
It is shown in Table 5.
Embodiment 2
With embodiment 1, the polyacrylamide (CPAM), aluminium polychloride (PAC), 2, the 6- di-t-butyl -4- methyl that are only added
Phenol (BHT) and the weight ratio of bis- salicylidene propane diamine of N, N'- mixing are 30:60:60:1.Wherein, gained overflow substance
Material product yield is 68%, and overflow material property is shown in Table 4.
Embodiment 3
With embodiment 1, the polyacrylamide (CPAM), aluminium polychloride (PAC), 2, the 6- di-t-butyl -4- methyl that are only added
Phenol (BHT) and the weight ratio of bis- salicylidene propane diamine of N, N'- mixing are 20:40:80:2.Wherein, gained overflow substance
Material product yield is 72%.
Embodiment 4
With embodiment 1, only the additional amount of composite modifier is the 0.02% of vacuum residuum feed weight.Wherein, gained overflow substance
Material product yield is 63%.
Embodiment 5
With embodiment 1, only the additional amount of composite modifier is the 0.1% of vacuum residuum feed weight.Wherein, gained overflow substance
Material product yield is 78%.
Comparative example 1
With embodiment 1, the composite modifier being only added only has polyacrylamide (CPAM) and aluminium polychloride (PAC), weight
Ratio is 1:2.Wherein, overflow material volume yield is 59%.
The overflow material of comparative example 1 is fixed the test result of a residual hydrogenation, reaction condition and operating 500 hours
It is shown in Table 5.
Comparative example 2
A residual hydrogenation is fixed as raw material using the miscella of conventional residual oil mixed refining wax oil, feedstock property is shown in Table 4, instead
It answers condition and the results are shown in Table 5.
By table 3 and 4 result of table it is found that fixed bed hydrogenation can not handle high carbon residue, high metal content inferior heavy oil, pass through
After the method for the present invention is appropriate visbreaking and carries out continuous sedimentation using composite modifier, resulting overflow material can be used as fixation
The raw material of bed hydroprocessing technique has widened fixed bed hydrogenation raw materials technology range.
By embodiment 1 and comparative example 1 as can be seen that the addition of composite modifier, it is therefore prevented that colloid oxygen in infall process
Asphalitine is turned to, the yield of overflow component is improved, and in subsequent Fixed Bed Residue, due to glue in residual oil
The reduction of matter asphalitine reduces catalyst bed coking, extends operation cycle.
By embodiment 1 with comparative example 2 as can be seen that compared with conventional raw material, visbreaking and composite modifier are to subtracting
The viscosity of product of viscosine continuous sedimentation group technology processing declines to a great extent, and gum asphalt also has and drops to a certain degree
Low, the composite modifier of addition can also inhibit murder by poisoning of some metal impurities to catalyst, to reduce catalyst bed knot
Coke extends operation cycle, and product quality is also improved.
1 Vacuum Residue Properties of table
| Project | Data |
| Density (20 DEG C), g/cm3 | 1.0052 |
| Viscosity (100 DEG C), mm2/s | 578.4 |
| Carbon residue, wt% | 17.28 |
| Tenor Ni+V, wppm | 178 |
| Four components, wt% | |
| Saturation point | 21 |
| Fragrance point | 30 |
| Colloid | 44 |
| Asphalitine | 5 |
2 visbreaking experimental condition of table and test result
| Project | Data |
| Experimental condition | |
| Temperature, DEG C | 400 |
| Pressure, MPa | 1 |
| Residence time, min | 120 |
| Products collection efficiency (mass fraction), % | |
| Cracked gas | 3.3 |
| <200℃ | 7.8 |
| 200~350℃ | 11.1 |
| >350℃ | 77.8 |
The property of 3 embodiment of table, 1 gained visbreaking residue
| Project | Data |
| Density (20 DEG C), g/cm3 | 0.9868 |
| Viscosity (100 DEG C), mm2/s | 70.7 |
| Carbon residue, wt% | 20.14 |
| Tenor Ni+V, wppm | 222.6 |
| Four components, wt% | |
| Saturation point | 29 |
| Fragrance point | 26 |
| Colloid | 33 |
| Asphalitine | 12 |
4 overflow material property of table
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | Comparative example 1 | Comparative example 2 |
| Density (20 DEG C), g/cm3 | 0.9624 | 0.9586 | 0.9636 | 0.9756 | 0.9542 | 0.9658 | 0.9846 |
| Viscosity (100 DEG C), mm2/s | 68.7 | 66.9 | 69.2 | 69.8 | 66.4 | 68.9 | 112.0 |
| Carbon residue, wt% | 11.42 | 11.03 | 11.65 | 12.21 | 10.98 | 12.6 | 12.62 |
| W metal+V, wppm | 89.6 | 88.7 | 89.9 | 90.2 | 86.1 | 91.5 | 82.0 |
| Four components, wt% | |||||||
| Saturation point | 44.3 | 44.0 | 43.9 | 43.3 | 44.4 | 44.3 | 37.8 |
| Fragrance point | 39.7 | 40.3 | 38.6 | 39.5 | 38.9 | 40.2 | 40.7 |
| Colloid | 13.2 | 12.6 | 14.1 | 13.7 | 14.6 | 11.9 | 17.1 |
| Asphalitine | 2.8 | 3.1 | 3.4 | 3.5 | 2.1 | 3.6 | 4.4 |
5 fixed bed residual hydrogenation experimental condition of table and reaction result
| Project | Embodiment 1 | Comparative example 1 | Comparative example 2 |
| Experimental condition | |||
| Temperature, DEG C | 380 | 380 | 380 |
| Pressure, MPa | 15 | 15 | 15 |
| Hydrogen to oil volume ratio | 650 | 650 | 650 |
| Volume space velocity when liquid, h-1 | 0.23 | 0.23 | 0.23 |
| Experimental result | |||
| Density (20 DEG C), g/cm3 | 0.9312 | 0.9343 | 0.9350 |
| Carbon residue, wt% | 5.14 | 5.50 | 5.87 |
| W metal+V, wppm | 14.0 | 15 | 15 |
| Operation cycle, h | 9200 | 8600 | 8100 |
Claims (12)
1. a kind of pretreated method of heavy oil, which is characterized in that comprise the following processes:
A) heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；
B) composite modifier is added in the visbreaking residue that step a) is obtained, continuous sedimentation then is carried out to mixture, on
Portion obtains overflow material, and lower part obtains underflow materials；
Wherein, composite modifier composition it is as follows: polyacrylamide, aluminium polychloride, 2,6- di-tert-butyl-4-methy phenol and
Bis- salicylidene propane diamine of N, N'-, weight ratio are (10 ~ 40): (30 ~ 70): (10 ~ 100): (0.5 ~ 3).
2. according to the method for claim 1, which is characterized in that the additional amount of the step b) composite modifier accounts for step
The 0.01% ~ 0.2% of rapid a) heavy oil feedstock weight, preferably 0.05% ~ 0.1%.
3. according to the method for claim 1, which is characterized in that visbreaking described in step a) uses either shallow hot tearing
Change process, process condition are as follows: reaction temperature is 350 ~ 450 DEG C, and reaction pressure is 0.1 ~ 1.5 MPa, visbreaking
Weight conversion rate is 1% ~ 40%.
4. according to the method for claim 1, which is characterized in that visbreaking described in step a) uses either shallow hot tearing
Change process, process condition are as follows: reaction temperature is 400 ~ 450 DEG C, 0.5 ~ 1.5 MPa of reaction pressure, the weight of visbreaking
Measure conversion ratio 10% ~ 20%.
5. according to the method for claim 1, which is characterized in that heavy oil feedstock described in step a) include reduced crude,
One or more of decompression residuum, deasphalted oil, oil sands bitumen, consistency crude oil, coal tar and coal liquefaction heavy oil.
6. according to method described in claim 1 or 5, which is characterized in that in heavy oil feedstock described in step a), tenor with
The poidometer of Ni and V is greater than 150 μ g/g, and the total content of resin and asphalt is greater than 50wt%.
7. according to any method of claim 1 to 6, which is characterized in that the composite modifier in step b), poly- third
The weight ratio of acrylamide, bis- salicylidene propane diamine of aluminium polychloride, 2,6- di-tert-butyl-4-methy phenol and N, N'-
For (15 ~ 35): (35 ~ 65): (55 ~ 85): (1 ~ 2).
8. according to the method for claim 1, which is characterized in that the continuous sedimentation device in step b) is using efficiently dense
Close machine bores deep concentrator, by the conditional operation of separation of solid and liquid, wherein overflow material, that is, continuous sedimentation device overflow outlet discharge
Material, the material of underflow materials, that is, continuous sedimentation device underflow outlet discharge.
9. according to method described in claim 1 or 8, which is characterized in that the operation temperature of step b) the continuous sedimentation device
Degree is 0 ~ 100 DEG C, preferably 70 ~ 80 DEG C.
10. according to the method for claim 9, which is characterized in that the continuous sedimentation device operating pressure in step b)
To keep that the pressure that composite modifier is liquid phase is added at the operational.
11. according to the method for claim 1, which is characterized in that continuous sedimentation device obtains overflow substance in step b)
Material and underflow materials, overflow material volume yield on the basis of the continuous sedimentation device feed volume 60% ~ 90%, preferably
65%~90%。
12. according to the method for claim 1, which is characterized in that overflow material described in step b) is after filtering
As the charging of fixed bed hydrogenation device, charging of the underflow materials as delayed coking unit.
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| CN201711020632.4A CN109722284B (en) | 2017-10-27 | 2017-10-27 | Heavy oil pretreatment method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113881458A (en) * | 2021-11-09 | 2022-01-04 | 山东京博石油化工有限公司 | Recycle oil catalytic cracking treatment system and treatment method |
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| CN101522868A (en) * | 2006-10-11 | 2009-09-02 | 道达尔炼油与销售部 | Marine lubricant for fuel oil having high and low sulphur contents |
| US20120246999A1 (en) * | 2011-03-28 | 2012-10-04 | Exxonmobil Research And Engineering Company | Novel fuel compositions and methods for making same |
| CN103642539A (en) * | 2013-12-25 | 2014-03-19 | 济南开发区星火科学技术研究院 | Regulating method of bunker fuel oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101522868A (en) * | 2006-10-11 | 2009-09-02 | 道达尔炼油与销售部 | Marine lubricant for fuel oil having high and low sulphur contents |
| US20120246999A1 (en) * | 2011-03-28 | 2012-10-04 | Exxonmobil Research And Engineering Company | Novel fuel compositions and methods for making same |
| CN103642539A (en) * | 2013-12-25 | 2014-03-19 | 济南开发区星火科学技术研究院 | Regulating method of bunker fuel oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113881458A (en) * | 2021-11-09 | 2022-01-04 | 山东京博石油化工有限公司 | Recycle oil catalytic cracking treatment system and treatment method |
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