CN109722303A - A kind of method of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component - Google Patents
A kind of method of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component Download PDFInfo
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Abstract
The invention discloses a kind of methods of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component.This method comprises the following steps: a) high-sulfur heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；B) composite modifier is added in the visbreaking residue that step a) obtains, continuous sedimentation then is carried out to mixture, top obtains overflow material, and lower part obtains underflow materials；C) the resulting overflow material of step b), which enters, carries out hydrodesulfurization in fixed bed residual hydrogenation equipment, obtain the blend component of low-sulfur oil fuel peculiar to vessel.Blend component of this method especially suitable for volume production low-sulfur bunker fuel oil, have the advantages that technology maturation, equipment operation expense are low etc., it can be improved the yield of visbreaking light-end products simultaneously, added value of product is improved, 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 a kind of methods of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component.
Background technique
With the continuous development of industry, problem of environmental pollution is increasingly valued by people, and environmental regulation is also increasingly tight
Lattice.New MARPOL pact regulation: on January 1st, 2015 and after, when ship at sea navigate by water by general area, marine fuel
Oily sulfur content is not to be exceeded 3.5%, while should also conform to each harbour specific requirement standard；And when emission control region is navigated by water, ship
On the sulphur content of fuel oil that uses be not to be exceeded 0.1%.The year two thousand twenty January 1 and after, when ship at sea general area navigate by water when,
Bunker fuel oil sulfur content is not to be exceeded 0.5%；When emission control region is navigated by water, should not be surpassed on ship using the sulfur content of fuel oil
Cross 0.1%.
The strength of stringenter sulfur content standard and discharge areas, which is managed, brings huge challenge to supplier, in the market
The supply of low-sulfur bunker fuel oil is limited, and existing production capacity is difficult to meet world market demand.It sees with practical conditions, existing low-sulfur
Large-scale production may be implemented in fraction type fuel oil resource, but because the oil product and ship equipment cannot be completely mating, when long
Between used in ship, on low-speed diesel engine, huge test will be brought to the fuel oil converting system and equipment of ship, while
Bigger security risk can be brought.In addition low-sulfur fraction type price of fuel oil is higher, under the conditions of originally sluggish shipping market,
The financial burden of shipowner will be further increased.And crude resources gradually tends to heaviness, in poor quality in world wide, it is contemplated that
Heavy crude reserves, which account for the whole world, after the year two thousand twenty can adopt 50% of crude oil reserve or so, how to efficiently use inferior heavy oil processing
Satisfactory low-sulfur bunker fuel oil becomes refinery and supplier's urgent problem to be solved.
CN 102746890A discloses a kind of preparation method of bunker fuel oil, the side being then fractionated by visbreaking
Formula obtains visbreaking blend component.This method can reduce the production cost of bunker fuel oil.But produce the visbreaking of fuel oil
Generally according to lower conversion operation (being typically only 6% ~ 7%), the light-end products that can make added value high in this way are reduced for cracking,
It is unfavorable for maximization of economic benefit, and the residual oil sulfur content of visbreaking production remains unchanged very high (generally 2% or so), it can not
Meet the index request of new bunker fuel oil.
CN 103695631A discloses a kind of method by producing diesel by utilizing coal tar and production marine fuel blend component.It should
Method makes raw material pass sequentially through slurry bed hydroprocessing and fixed bed hydrogenation to obtain product.It is very low that this method can produce sulfur content
Blend component peculiar to vessel.But the current technology of slurry bed system is also immature, and restriction of the bed technology by raw material oil nature,
Not being capable of processing the higher inferior raw material of metal, carbon residue content (can only process tenor lower than 150 μ g/g, carbon residue and be lower than 15%
Heavy oil).
CN 106753556A disclose it is a kind of using inferior heavy oil process lube base oil and liquid fuel plus
Work method obtains liquid fuel by solvent deasphalting and hydrotreating.Liquid component yield can be improved in this method, improves and produces
Quality.But solvent de-asphalting process is complicated, energy consumption is high, realizes difficulty, and deasphalted oil viscosity is big, needs to mix lightweight
Oil product reduces viscosity, to reduce the efficiency of fixed bed hydrogenation device.
Summary of the invention
In view of the deficiencies of the prior art, the object of the present invention is to provide a kind of high-sulfur heavy oil to produce low-sulfur bunker fuel oil tune
With the method for component, there is blend component of this method especially suitable for volume production low-sulfur bunker fuel oil technology maturation, equipment to grasp
Make the advantages such as expense is low, while can be improved the yield of visbreaking light-end products, improves added value of product, and be conducive to weaken
Influence in subsequent fixed bed hydroprocessing treatment process to catalyst activity stability.
In order to achieve the above object, the side of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component provided by the invention
Method comprises the following processes:
A) high-sulfur heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；
B) composite modifier is added in the visbreaking residue that step a) obtains, continuous sedimentation then is carried out to mixture, top obtains
To overflow material, lower part obtains underflow materials；
C) the resulting overflow material of step b), which enters, carries out hydrodesulfurization in fixed bed residual hydrogenation equipment, obtain low-sulfur bunker oil
The blend component of fuel.
In high-sulfur heavy oil feedstock described in step a), sulfur content is greater than 3.5wt%, and tenor is big with the poidometer of Ni and V
It is greater than 50wt% in the total content of 150 μ g/g, resin and asphalt.The high-sulfur heavy oil cannot be directly as conventional fixed bed slag
The raw material of oily hydrogenation plant.
Visbreaking described in step a) use either shallow thermal cracking process, process condition are as follows: reaction temperature be 350 ~
450 DEG C, preferably 400 ~ 450 DEG C；Reaction pressure is 0.1 ~ 1.5 MPa, preferably 1.0 ~ 1.5 MPa；Residence time is 60
~ 180min, preferably 120 ~ 150min；The weight conversion rate of visbreaking is 1% ~ 40%, preferably 10% ~ 20%.Wherein, it converts
Light component (fraction that boiling point is lower than heavy oil feedstock) weight that rate is obtained by visbreaking accounts for the percentage of heavy oil feedstock weight.
Composite modifier composition in step b) is as follows: polyacrylamide, aluminium polychloride, N, N'- di-sec-butyl is to benzene
Diamines, p-tert-Butylcatechol and N, bis- salicylidene propane diamine of N'-, weight ratio are (10 ~ 40): (30 ~ 70):
(10 ~ 100): (10 ~ 80): (0.5 ~ 3), preferably (15 ~ 35): (35 ~ 65): (55 ~ 85): (15 ~ 35): (1 ~ 2).It is described compound
The additional amount of modifying agent accounts for the 0.01% ~ 0.2% of step a) high-sulfur heavy oil feedstock weight, and preferably 0.05% ~ 0.1%.
Continuous sedimentation device in step b) using high-efficiency thickener or bores deep concentrator, grasps by the condition of separation of solid and liquid
Make；Its operation temperature is 0 ~ 100 DEG C, preferably 70 ~ 80 DEG C；Its operating pressure is to keep addition composite modified at the operational
Agent is the pressure of liquid phase；Wherein overflow material, that is, continuous sedimentation device overflow outlet discharge material, underflow materials are i.e. continuous heavy
The material of falling unit underflow outlet discharge；Overflow material volume yield on the basis of the continuous sedimentation device feed volume 60% ~
90%, preferably 70% ~ 80%.
The resulting underflow materials of step b) can be used as the raw material of the devices such as solvent deasphalting or delayed coking.
Fixed bed residual hydrogenation equipment described in step c) includes 1 ~ 5 hydrotreating reactor being arranged in series, preferably
The hydrotreating reactor being arranged in series including 3 ~ 4；The operating condition of fixed bed residual hydrogenation equipment are as follows: reaction temperature is
370 DEG C ~ 430 DEG C, preferably 380 DEG C ~ 410 DEG C；Reaction pressure is 10MPa ~ 25MPa, preferably 14MPa ~ 18MPa；Hydrogen
Oil volume ratio is 300 ~ 1500, preferably 400 ~ 800；Volume space velocity is 0.15h when raw material oil liquid-1~ 0.80h-1, preferably
For 0.2h-1~0.60h-1。
Conventional catalyst for hydrotreatment of residual oil can be loaded in fixed bed residual hydrogenation equipment described in step c), such as
One or more of hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst, preferably by liquid phase stream direction according to
Secondary filling hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst.The catalyst for hydrotreatment of residual oil contains
Active metal component and carrier, wherein the active metal contains at least one in group VIB metal and group VIII metal
Kind, the carrier contains at least one of aluminium oxide, amorphous silica-alumina and silica.The group VIB metal is selected from W
And/or Mo, the group VIII metal are selected from Co and/or Ni.On the basis of the weight of catalyst, group VIB metal is with oxide
The content of meter is 5% ~ 40%, and content of the group VIII metal in terms of oxide is 1% ~ 15%.Such as had by Sinopec's share
The FZC series catalyst for hydrotreatment of residual oil of limit company catalyst branch production.
Compared with prior art, the method for the present invention has the advantages that
(1) high-sulfur heavy oil feedstock enters viscosity breaking plant progress visbreaking, and control reaction is under a higher conversion ratio
It carries out, light oil yield can be made to increase in this way, increased economic efficiency, and the asphalitine in visbreaking residue is made to reach one
Higher content；
(2) in the method for the present invention step b), continuous sedimentation is carried out to visbreaking residue using composite modifier, is generated using step a)
Visbreaking residue stability is poor, gel phase disequilibration determines this feature, composite modifier is added, by polyacrylamide,
Aluminium polychloride, N, N'- di-sec-butyl-p-phenyl enediamine, p-tert-Butylcatechol and N, bis- salicylidene propane diamine of N'- it
Between cooperation synergistic effect, further destroy the balance of continuous phase and dispersed phase, prevent most of asphalitine from steady in system
Surely peptization and aggregation separation occurs, from it is original it is single homogeneously become two-phase, cause asphaltene precipitation to come out, substantially increase
Separating rate and separative efficiency effectively remove the asphalitine component rich in impurity such as metal, sulphur, nitrogen, oxygen in inferior heavy oil.Together
When, the synergistic effect of composite modifier can also prevent the substance for being subsequently formed the high pour point of excessive macromolecular from generating, and control it
Pour point is in a zone of reasonableness；In addition it can inhibit the activity of the active metallic ion in oil product, prevent in infall process
Colloid is oxidized to asphalitine too much, to improve overflow material yield, and also helps the metal contained in overflow material
Impurity (such as nickel, vanadium, copper) is easier to remove during subsequent residual hydrocracking, and reduces and stablize to catalyst activity
The influence of property.
(3) deep desulfuration is carried out to overflow material by fixed bed residual hydrogenation equipment, it is low sulfur content can be produced in batches
In the good high-quality bunker fuel oil blend component of 0.5%, modest viscosity, stability.
(4) entire process technology is mature, and operating cost is low, good economy performance.
Detailed description of the invention
Fig. 1 is process flow diagram of the invention；
In figure: 1- high-sulfur heavy oil feedstock, 2- viscosity breaking plant, 3- composite modifier, 4- continuous sedimentation device, 5- underflow object
Material, 6- overflow material, 7- fixed bed residual hydrogenation equipment, 8- bunker fuel oil blend component.
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 process flow of the invention are as follows: high-sulfur heavy oil feedstock 1 is subtracted into viscosity breaking plant 2
Viscous cracking, obtains visbreaking residue.Visbreaking residue is mixed into continuous sedimentation device 4 with composite modifier 3 and is separated, and is separated into
Underflow materials 5 and overflow material 6.Underflow materials 5 can enter delayed coking or solvent deasphalting unit.Overflow material 6 enters solid
Fixed bed residual hydrogenation equipment 7 carries out hydrodesulfurization, obtains bunker fuel oil blend component 8.
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 that high-sulfur heavy oil produces low-sulfur bunker fuel oil blend component.Vacuum residuum feed into
Enter viscosity breaking plant and carries out visbreaking.After appropriate visbreaking, visbreaking residue is obtained.It is added into visbreaking residue multiple
Close modifying agent, the composite modifier of addition is the N'- di-sec-butyl-p-phenyl enediamine, to uncle by polyacrylamide, aluminium polychloride, N
Butyl-catechol and N, bis- salicylidene propane diamine of N'- mixing composition, weight ratio 20:40:60:30:1 are compound
The additional amount of modifying agent is the 0.05% of vacuum residuum feed weight.The mixture enters continuous sedimentation device and carries out continuous sedimentation,
Operating condition is as follows: 80 DEG C of temperature, operating pressure is the pressure for keeping being added that composite modifier is liquid phase at the operational.?
Continuous sedimentation device overflow exports to obtain overflow material, and overflow material volume yield is 70%, in continuous sedimentation device underflow outlet
Obtain underflow materials.
It tests the vacuum residuum feed property used and is listed in table 1.As shown in Table 1 the residual oil raw material viscosity, carbon residue, metal and
Sulfur content is very high, is with the unmanageable inferior raw material of conventional residual hydrogenation equipment.Visbreaking experimental condition and test knot
Fruit is shown in Table 2, and visbreaking residue (> 350 DEG C of fractions) property is shown in Table 3, and overflow material property is shown in Table 4.
A residual hydrogenation is fixed to the overflow material of embodiment 1, reactor is 4 tandem reactors, reactor according to
Secondary filling hydrogenation protecting agent (FZC-100B and FZC-12B), Hydrodemetalation catalyst (FZC-204A and FZC-28A) plus hydrogen
The test result of desulphurization catalyst (FZC-33 and FZC-34), reaction condition and operating 500 hours is shown in Table 5.
Embodiment 2
With embodiment 1, polyacrylamide, aluminium polychloride, the N being only added, N'- di-sec-butyl-p-phenyl enediamine, to tert-butyl
Catechol and N, bis- salicylidene propane diamine of N'- mixing composition, weight ratio 30:60:60:30:1.Wherein, gained
Overflow material volume yield is 68%, and overflow material property is shown in Table 4.Reaction condition and the test result of operating 500 hours are shown in Table 5.
Embodiment 3
With embodiment 1, polyacrylamide, aluminium polychloride, the N being only added, N'- di-sec-butyl-p-phenyl enediamine, to tert-butyl
Catechol and N, bis- salicylidene propane diamine of N'- mixing composition, weight ratio 20:40:80:30:2.Wherein, gained
Overflow material volume yield is 72%, and overflow material property is shown in Table 4.Reaction condition and the test result of operating 500 hours are shown in Table 5.
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 68%, and overflow material property is shown in Table 4.Reaction condition and the test result of operating 500 hours are shown in Table 5.
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%, and overflow material property is shown in Table 4.Reaction condition and the test result of operating 500 hours are shown in Table 5.
By table 3 and 4 result of table it is found that high carbon residue, high sulfur content, high metal content poor quality that fixed bed hydrogenation can not be handled
Heavy oil, after the method for the present invention is appropriate visbreaking and carries out continuous sedimentation using composite modifier, resulting overflow material peace
It is qualitative good, it can be used as the raw material of fixed bed hydrogenation technique, widened fixed bed hydrogenation raw materials technology range.Table 5 and table 6 can be with
Find out, the bunker fuel oil blend component stability produced by the method for the invention is good, sulfur content is low, meets wanting for environmental regulation
It asks, and its pour point is also controlled in a zone of reasonableness.
Comparative example 1
With embodiment 1, the composite modifier being only added only has polyacrylamide, aluminium polychloride and to tert-butyl o benzene two
Phenol, weight ratio 2:4:3.Wherein, overflow material volume yield is 68%.
The overflow material of comparative example 1 is fixed a residual hydrogenation, reaction condition and operates 500 hours test results and sees
Table 5.
Comparative example 2
With embodiment 1, the composite modifier of addition only has polyacrylamide, aluminium polychloride, N, N'- di-sec-butyl-p-phenyl enediamine
And bis- salicylidene propane diamine of N, N'- mixing composition, weight ratio 20:40:60:1.Wherein, overflow material volume is received
Rate is 61%.
A residual hydrogenation is fixed in the overflow material of comparative example 2, and reaction condition is the same as embodiment 1, the examination of operating 500 hours
It tests and the results are shown in Table 6.In addition, the operation cycle of 2 device of comparative example is 8400 hours.
Comparative example 3
Using the method for existing conventional production fuel oil blend component, blend component, raw material are directly produced using visbreaking
Property is shown in Table 1, and visbreaking conditions are shown in Table 2, and visbreaking residue property is shown in Table 6.
When comparison reaction result can be seen that visbreaking and directly produce fuel oil ingredient, visbreaking residue in order to prevent
Stability is poor, and general condition can compare mitigation, causes light oil yield not high, under the preferable situation of feedstock property,
Sulfur content is still very high, is unable to satisfy increasingly strict environmental regulation requirement, and needing to be added a large amount of light-end products could reconcile out
The fuel oil of meet demand.And the method for the present invention can be visbreaking and carry out under the operating condition of a higher yields, lead to
Subsequent processing is crossed, improves the stability of overflow component, and so that sulfur content is declined to a great extent by fixed bed residual hydrogenation equipment,
Meet increasingly strict environmental regulation.
1 Vacuum Residue Properties of table
| Project | Embodiment 1 | Comparative example 3 |
| Density (20 DEG C), g/cm3 | 1.0052 | 0.9813 |
| Viscosity (100 DEG C), mm2/s | 578.4 | 413.8 |
| Sulfur content, wt% | 3.89 | 2.25 |
| Carbon residue, wt% | 17.28 | 12.56 |
| Tenor Ni+V, wppm | 178 | 106 |
| Four components, wt% | ||
| Saturation point | 15 | 22 |
| Fragrance point | 26 | 34 |
| Colloid | 53 | 41 |
| Asphalitine | 6 | 3 |
2 visbreaking experimental condition of table and test result
| Project | Embodiment 1 | Comparative example 3 |
| Experimental condition | ||
| Temperature, DEG C | 400 | 380 |
| Pressure, MPa | 1 | 1 |
| Residence time, min | 120 | 60 |
| Products collection efficiency (mass fraction), % | ||
| Cracked gas | 3.3 | 1.4 |
| <200℃ | 7.8 | 3.5 |
| 200~350℃ | 11.1 | 4.1 |
| >350℃ | 77.8 | 91.0 |
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 |
| Sulfur content, wt% | 4.12 |
| Tenor Ni+V, wppm | 222.6 |
| Four components, wt% | |
| Saturation point | 28 |
| Fragrance point | 27 |
| 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 | 0.9758 | 0.9883 |
| Viscosity (100 DEG C), mm2/s | 68.7 | 65.9 | 69.2 | 73.8 | 63.4 | 88.9 | 78.2 |
| Sulfur content, wt% | 2.14 | 2.03 | 2.27 | 2.46 | 1.98 | 2.59 | 2.31 |
| Carbon residue, wt% | 11.42 | 11.03 | 11.65 | 12.21 | 10.98 | 14.69 | 13.34 |
| W metal+V, wppm | 83.6 | 86.7 | 89.9 | 92.2 | 80.1 | 98.1 | 96.9 |
| Four components, wt% | |||||||
| Saturation point | 44.6 | 44.0 | 42.8 | 43.0 | 44.8 | 39.3 | 40.1 |
| Fragrance point | 39.7 | 40.4 | 40.5 | 39.5 | 38.6 | 36.2 | 39.0 |
| Colloid | 13.2 | 12.6 | 14.3 | 13.7 | 14.8 | 17.9 | 16.5 |
| Asphalitine | 2.5 | 3.0 | 2.4 | 3.8 | 1.8 | 6.6 | 4.4 |
5 fixed bed residual hydrogenation experimental condition of table and reaction result
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | Comparative example 1 |
| Experimental condition | ||||||
| Temperature, DEG C | 380 | 380 | 380 | 380 | 380 | 380 |
| Pressure, MPa | 15 | 15 | 15 | 15 | 15 | 15 |
| Hydrogen to oil volume ratio | 650 | 650 | 650 | 650 | 650 | 650 |
| Volume space velocity when liquid, h-1 | 0.23 | 0.23 | 0.23 | 0.23 | 0.23 | 0.23 |
| Experimental result | ||||||
| Density (20 DEG C), g/cm3 | 0.9312 | 0.9350 | 0.9343 | 0.9481 | 0.9275 | 0.9343 |
| Viscosity (100 DEG C), mm2/s | 25.37 | 26.16 | 24.56 | 27.63 | 24.37 | 29.54 |
| Sulfur content, wt% | 0.39 | 0.36 | 0.35 | 0.46 | 0.31 | 0.68 |
| Carbon residue, wt% | 5.14 | 5.87 | 5.50 | 5.26 | 4.80 | 5.50 |
| Pour point, DEG C | 19 | 22 | 17 | 26 | 14 | 22 |
| Operation cycle, h | 9400 | 9200 | 9600 | 9000 | 9900 | 8800 |
Table 6
Infuse *: " standard " in table 6 refers to residue type fuel oil standard (GB17411).
Claims (10)
1. a kind of method of high-sulfur heavy oil production low-sulfur bunker fuel oil blend component, comprises the following processes:
A) high-sulfur heavy oil feedstock enters viscosity breaking plant progress visbreaking, obtains visbreaking residue；
B) composite modifier is added in the visbreaking residue that step a) obtains, continuous sedimentation then is carried out to mixture, top obtains
To overflow material, lower part obtains underflow materials；
C) the resulting overflow material of step b), which enters, carries out hydrodesulfurization in fixed bed residual hydrogenation equipment, obtain low-sulfur bunker oil
The blend component of fuel；
Wherein, the composite modifier composition in step b) is as follows: polyacrylamide, aluminium polychloride, N, N'- di-sec-butyl is to benzene
Diamines, p-tert-Butylcatechol and N, bis- salicylidene propane diamine of N'-, weight ratio are (10 ~ 40): (30 ~ 70):
(10 ~ 100): (10 ~ 80): (0.5 ~ 3).
2. according to the method for claim 1, which is characterized in that the additional amount of composite modifier described in step b) accounts for step
A) the 0.01% ~ 0.2% of high-sulfur heavy oil feedstock weight, preferably 0.05% ~ 0.1%.
3. according to the method for claim 1, which is characterized in that in high-sulfur heavy oil feedstock described in step a), sulfur content is big
In 3.5wt%, tenor is greater than 150 μ g/g with the poidometer of Ni and V, and the total content of resin and asphalt is greater than 50wt%.
4. according to the method for claim 1, which is characterized in that visbreaking described in step a) is split using either shallow visbreaking
Change process, process condition are as follows: reaction temperature is 350 ~ 450 DEG C, and reaction pressure is 0.1 ~ 1.5 MPa, and the residence time is
60~180min；The weight conversion rate of visbreaking is 1% ~ 40%.
5. according to method described in claim 1 or 4, which is characterized in that visbreaking described in step a) uses either shallow visbreaking
Cracking process, process condition are as follows: reaction temperature is 400 ~ 450 DEG C, 1.0 ~ 1.5 MPa of reaction pressure, and the residence time is
120~150min；The weight conversion rate 10% ~ 20% of visbreaking.
6. according to the method for claim 1, which is characterized in that polyacrylamide in composite modifier described in step b), poly-
Close aluminium chloride, N, N'- di-sec-butyl-p-phenyl enediamine, p-tert-Butylcatechol and N, the weight of bis- salicylidene propane diamine of N'-
Amount ratio is (15 ~ 35): (35 ~ 65): (55 ~ 85): (15 ~ 35): (1 ~ 2).
7. according to the method for claim 1, which is characterized in that the continuous sedimentation device in step b) uses high-efficiency thickener
Or deep concentrator is bored, and by the conditional operation of separation of solid and liquid, the object that wherein overflow material, that is, continuous sedimentation device overflow outlet is discharged
Material, underflow materials, that is, continuous sedimentation device underflow outlet discharge material.
8. according to method described in claim 1 or 7, which is characterized in that the operation temperature of the step b) continuous sedimentation device
It is 0 ~ 100 DEG C, preferably 70 ~ 80 DEG C, the continuous sedimentation device operating pressure in step b) is to keep being added at the operational
Composite modifier is the pressure of liquid phase.
9. according to the method for claim 1, which is characterized in that overflow material described in step b) is after filtering as solid
The charging of fixed bed hydrogenation plant；Charging of the underflow materials as solvent deasphalting or delayed coking unit.
10. according to the method for claim 1, which is characterized in that the behaviour of fixed bed residual hydrogenation equipment described in step c)
Make condition are as follows: reaction temperature be 370 DEG C ~ 430 DEG C, reaction pressure be 10MPa ~ 25MPa, hydrogen to oil volume ratio be 300 ~
1500, volume space velocity is 0.15h when raw material oil liquid-1~ 0.80h-1；Wherein, fixed bed residual hydrogenation equipment described in step c)
Operating condition it is preferred are as follows: reaction temperature is 380 DEG C ~ 410 DEG C, and reaction pressure is 15MPa ~ 20MPa, and hydrogen to oil volume ratio is
400 ~ 800, volume space velocity is 0.2h when raw material oil liquid-1~0.60h-1。
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| CN115181584A (en) * | 2021-04-01 | 2022-10-14 | 中国石油天然气股份有限公司 | Production process and system of residual type low-sulfur marine fuel oil |
| CN115181584B (en) * | 2021-04-01 | 2023-12-22 | 中国石油天然气股份有限公司 | Production process and system of residue type low-sulfur marine fuel oil |
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