CN109705909A - By the method for coal tar production bunker fuel oil - Google Patents
By the method for coal tar production bunker fuel oil Download PDFInfo
- Publication number
- CN109705909A CN109705909A CN201711007125.7A CN201711007125A CN109705909A CN 109705909 A CN109705909 A CN 109705909A CN 201711007125 A CN201711007125 A CN 201711007125A CN 109705909 A CN109705909 A CN 109705909A
- Authority
- CN
- China
- Prior art keywords
- oil
- weight
- coal tar
- fuel oil
- content
- 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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
It the present invention relates to coal tar hydrogenating field, discloses by the method for coal tar production bunker fuel oil, comprising: carry out hydrotreating for being dehydrated to be introduced into slurry bed system hydrogenator with the full fraction of coal tar raw material after mechanical purifying；The slurry bed system hydrogenator effluent obtained after the hydrotreating is successively separated, normal pressure fractionation and vacuum fractionation, obtains often pushing up oil, normal line oil, first vacuum side stream and subtract base oil；Using normal line oil and part subtract base oil formation mixture as light fuel oil product peculiar to vessel, and using first vacuum side stream and it is remaining subtract base oil formation mixture as heavy fuel oil product peculiar to vessel；The light Fuel oil product that the above method provided by the present invention obtains can be directly as low-sulfur high-lubricity lightweight admiralty fuel oil without using antiwear additive or lubricity improver；The heavy oil that the above method provided by the present invention obtains simultaneously can fire blend component directly as No. 120 or No. 180 ships of low-sulfur.
Description
Technical field
The present invention relates to coal tar hydrogenating fields, and in particular to a method of bunker fuel oil is produced by coal tar.
Background technique
As social economy continues, high speed development, demand of the China to oil product also increasingly increases.However, petroleum category
In non-renewable energy resources, it is faced with increasingly exhausted crisis.In contrast, Chinese coal reserves account is relatively abundanter, therefore, by coal
Preparing liquid fuel has become a basic orientation of coal processing and utilization.
On the other hand, with the rapid growth of international, domestic steel industry, the trend of high growth, coal is presented in coking industry
The yield of tar is increasing, and the cleaning processing and effective use of coal tar also become more and more important.
Currently, the Conventional processing methods of coal tar are the various fractions cut in diversity by pretreatment distillation, then right
The methods of various fractions acid-alkali washing, distillation, polymerization, crystallization carry out processing and extract net product；Also some coal tar passes through
It is directly burnt after crossing acid-alkali refining as low-quality fuel oil, or is used as emulsion fuel burns after directly emulsifying.
The impurity such as institute's sulfur-bearing, nitrogen become sulphur in combustion in coal tar and nitrogen oxide is discharged into the atmosphere and caused
Atmosphere pollution, and large amount of sewage can be generated during acid-alkali refining, it would seriously pollute the environment.Therefore, it is either protected from environment
The angle of shield still in terms of comprehensive utilization, is intended to find an effective chemical process approach, obtains coal tar
Upgrading, to expand its own utility value.How tar resource is rationally utilized, and the economic benefit for improving enterprise becomes more next
It is more important.
CN1903994A discloses a kind of method of producing fuel oil by coal tar hydrogenation modifying, specifically removing moisture and ash
After the full fraction coal tar divided mixes in proportion with flux oil, add by the either shallow equipped with hydrogenation protecting agent, catalyst for pre-hydrogenation
Hydrogen unit and deep hydrogenation unit equipped with main hydrogenating catalyst, product are separated, are fractionated to obtain low sulphur fuel oil.This method by
It needs to be added flux oil dilution in coal tar raw material, reduces the treating capacity of device and easily cause the analysis of coal tar studies on asphaltene
Precipitating is generated out, and this method also can be in actual application by the limitation of flux oil.
CN103695031A discloses a kind of side by coal tar raw material production diesel oil and production bunker fuel oil blend component
Method.Specially full fraction of coal tar raw material enters paste state bed reactor progress pre-hydrotreating reaction after mixing with hydrogen, and pre-add hydrogen produces
Object separates light component and heavy constituent, part of heavy constituent is as bunker fuel oil, remaining recombination after gas-liquid separation and fractionation
Divide and light component further progress adds hydrogen upgrading to produce cleaning diesel oil.However the method hydrogen gas consumption that the prior art provides
Height, also, even the slurry bed system product in the prior art is fractionated to obtain diesel component, the profit of the diesel component
Slip is also bad.
Summary of the invention
The purpose of the invention is to overcome the problems, such as drawbacks described above of the existing technology, provide that process flow is simple, throws
It provides low method and the significantly reduced bunker fuel oil of grinding defect diameter is produced by coal tar.
It is increasingly tighter with environmental regulation, it is also increasingly tighter to the sulfur content limitation of admiralty fuel oil, by adding hydrogen side
When method produces low-sulphur fuel, the lubricity of hydrogenated products will appear problem.Derv fuel mainly passes through addition lubricity at present
Modifier solves problems.Unlike vehicle fuel, there is no limit to oil distillation for marine fuel, therefore the present invention
Inventor obtain normal line oil, first vacuum side stream by controlling the hydrotreating depth of full fraction of coal tar raw material and subtract bottom
Oil, and the above-mentioned product oil that rational allocation obtains can obtain greasy property under the premise of not using lubricity improver
Improved light Fuel, while will not influence other performance indicators of product, enterprise's production cost can be greatly lowered.According to
This, the present inventor completes technical solution of the present invention.
To achieve the goals above, the present invention provides a kind of method by coal tar production bunker fuel oil, this method packet
It includes:
(1) it in the presence of heterogeneous slurry bed hydrogenation catalyst, will be dehydrated and the full fraction of coal tar after mechanical purifying
Raw material, which is introduced into slurry bed system hydrogenator, carries out hydrotreating；
(2) the slurry bed system hydrogenator effluent obtained after the hydrotreating is successively separated, normal pressure fractionation
And vacuum fractionation, it obtains often pushing up oil, normal line oil, first vacuum side stream and subtracts base oil；
(3) subtract the mixture of base oil formation using normal line oil and partially as light fuel oil product peculiar to vessel, and will subtract one
Line oil and the remaining mixture for subtracting base oil formation are as heavy fuel oil product peculiar to vessel；
Wherein, the depth of the hydrotreating of rate-determining steps (1) make in the normal line obtained in step (2) oil it is bicyclic with
Upper arene content is not higher than 15 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 85 weight %；And to subtract four in base oil
The above aromatic hydrocarbons total content of ring is not higher than 5 weight %, and thrcylic aromatic hydrocarbon and four cycloaromatics total contents are not less than 20 weight %.
The light Fuel oil product that the above method provided by the present invention obtains is without using antiwear additive or improved lubricity
Agent can be lower than 300 μm of low-sulfur high-lubricity lightweight marine fuel directly as sulfur content lower than 200 μ g/g, grinding defect diameter
Oil；The heavy oil that the above method provided by the present invention obtains simultaneously can be directly as No. 120 or No. 180 ship combustions of low-sulfur
Blend component.
It is low that method of the invention also has the advantages that hydrogen consumes.
Detailed description of the invention
Fig. 1 is that a kind of method flow by coal tar production bunker fuel oil of preferred embodiment of the invention is illustrated
Figure.
Description of symbols
1, slurry bed system hydrogenator 2, separation and filtration system
3, atmospheric tower 4, vacuum tower
5, full fraction of coal tar raw material 6, hydrogen
7, solid slag 8, separation gas
9, often top oil 10, a normal line are oily
11, first vacuum side stream 12, subtract base oil
13, heavy fuel oil product 14 peculiar to vessel, light fuel oil product peculiar to vessel
15, vacuum system
Specific embodiment
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or
Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively
It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more
New numberical range, these numberical ranges should be considered as specific open herein.
As previously mentioned, the present invention provides a kind of methods by coal tar production bunker fuel oil, this method comprises:
(1) it in the presence of heterogeneous slurry bed hydrogenation catalyst, will be dehydrated and the full fraction of coal tar after mechanical purifying
Raw material, which is introduced into slurry bed system hydrogenator, carries out hydrotreating；
(2) the slurry bed system hydrogenator effluent obtained after the hydrotreating is successively separated, normal pressure fractionation
And vacuum fractionation, it obtains often pushing up oil, normal line oil, first vacuum side stream and subtracts base oil；
(3) subtract the mixture of base oil formation using normal line oil and partially as light fuel oil product peculiar to vessel, and will subtract one
Line oil and the remaining mixture for subtracting base oil formation are as heavy fuel oil product peculiar to vessel；
Wherein, the depth of the hydrotreating of rate-determining steps (1) make in the normal line obtained in step (2) oil it is bicyclic with
Upper arene content is not higher than 15 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 85 weight %；And to subtract four in base oil
The above aromatic hydrocarbons total content of ring is not higher than 5 weight %, and thrcylic aromatic hydrocarbon and four cycloaromatics total contents are not less than 20 weight %.
Normal pressure of the invention refers to: a standard atmospheric pressure, as 101KPa.
Method provided by the invention is just able to produce sulfur content lower than 200 μ without using antiwear additive or lubricity improver
G/g, grinding defect diameter are lower than 300 μm of low-sulfur high-lubricity admiralty fuel oil, which is particularly suitable for coastal waters, in inland river
The ship of rev-happy engine.
In the present invention, full fraction of coal tar raw material settled through preliminary pretreatment first, be centrifugated to remove
There is no particular limitation for the concrete operation method of water, mechanical admixture etc., as long as can reach preliminary removing full fraction of coal tar raw material
In water, mechanical admixture purpose.
In method of the present invention, full fraction of coal tar raw material after tentatively being removed water, mechanical admixture and it is non-
Phase slurry bed hydrogenation catalyst enters together with hydrogen after mixing carries out hydrotreating in slurry bed system hydrogenator.
In method of the present invention, full fraction of coal tar raw material carries out adding at hydrogen in slurry bed system hydrogenator
Reason reaches the purpose of removing metal, mechanical admixture, sulphur, nitrogen, and the hydrogenation depth suitable by control, is added with reducing slurry bed system
The generation of the by-products such as dry gas, liquefied gas and coke during hydrogen.
In step (2) of the invention, the slurry bed system hydrogenator effluent obtained after the hydrotreating is carried out
Isolated purpose is to remove solid slag therein and gas (being named as separation gas below).The separation can for example contain gas-liquid
It is carried out in the system of separation and solid-liquor separation.
In step (2) of the invention, the slurry bed system hydrogenator effluent obtained after the hydrotreating is carried out
Fractionation includes successively carrying out normal pressure fractionation and vacuum fractionation.Often top oil and normal line oil are obtained by normal pressure fractionation, by normal pressure point
The distillate for evaporating tower bottom, which is introduced in such as vacuum tower, carries out vacuum fractionation to obtain first vacuum side stream and subtract base oil.
Under preferable case, the depth of the hydrotreating of rate-determining steps (1) makes in the normal line obtained in step (2) oil
The bicyclic above arene content is not higher than 10 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 90 weight %；And to subtract bottom
The above aromatic hydrocarbons total content in Fourth Ring is not higher than 3 weight % in oil, and thrcylic aromatic hydrocarbon and four cycloaromatics total contents are not less than 25 weight %.It adopts
It can make hydrogen under the premise of obtaining the marine fuel oil product of more preferable performance with the hydrotreating depth under the preferable case
It consumes lower.
Method provided by the invention realizes the removing of miscellaneous metal, machine, sulphur, nitrogen etc. by using slurry bed system hydrogenator,
And the hydrotreating reaction depth suitable by control, make the bicyclic above arene content in normal line oil not higher than 15 weights
%, preferably no greater than 10 weight % are measured, aromatic hydrocarbons and cycloalkane total content are not less than 85 weight %, preferably not less than 90 weight %；
Make to subtract the above aromatic hydrocarbons total content in Fourth Ring in base oil not higher than 5 weight %, preferably no greater than 3 weight %, thrcylic aromatic hydrocarbon and four cyclophanes
Hydrocarbon total content is not less than 20 weight %, preferably not less than 25 weight %.
By control hydrogenation depth in above range of the invention, particularly preferably in the range of when, can be improved mixed
The intersolubility and stability of oil are closed, and can ensure that the lubricity of product is sufficiently high and stability is good enough simultaneously.
Preferably, the content for subtracting base oil that control is formed in the mixture of the light fuel oil product peculiar to vessel makes the ship
It is 2.5~5.0 weight % with thrcylic aromatic hydrocarbon in light fuel oil product and four cycloaromatics total contents.It is highly preferred that control forms institute
It states the content for subtracting base oil in the mixture of light fuel oil product peculiar to vessel and makes thrcylic aromatic hydrocarbon in the light fuel oil product peculiar to vessel
It is 3.0~4.5 weight % with four cycloaromatics total contents.
The heterogeneous slurry bed hydrogenation catalyst of the invention can be high dispersive type catalyst.According to a kind of preferred
Specific embodiment contains at least one of coal dust, coke blacking and active carbon in the heterogeneous slurry bed hydrogenation catalyst
For substance as decentralized medium, and containing the active component as dispersed phase, the active component is selected from group VIB base metal
At least one of with group VIII base metal.It is highly preferred that the active component be iron, cobalt, nickel, molybdenum and tungsten at least
It is a kind of.The supported catalyst for example, the heterogeneous slurry bed hydrogenation catalyst is negative.
Under preferable case, on the basis of the total weight of the heterogeneous slurry bed hydrogenation catalyst, based on the element described
The content of active component is 2~20 weight %.It is highly preferred that using the total weight of the heterogeneous slurry bed hydrogenation catalyst as base
Standard, the content of the active component based on the element are 5~18 weight %.
Preferably, described on the basis of the total weight of the full fraction of coal tar raw material after dehydration and mechanical purifying
The additional amount of heterogeneous slurry bed hydrogenation catalyst is 1.0~3.0 weight %, the more preferable heterogeneous slurry bed system hydrogenation catalyst
The additional amount of agent is 1.0~2.0 weight %.
According to a kind of preferred embodiment, the condition of the hydrotreating in step (1) includes: reaction temperature
It is 360~440 DEG C, hydrogen partial pressure is 5.0~10.0MPa, and volume space velocity is 0.1~1.5h-1, hydrogen to oil volume ratio be 200~
1000Nm3/m3。
According to another preferred specific embodiment, the condition of the hydrotreating in step (1) includes: reaction
Temperature is 380~420 DEG C, and hydrogen partial pressure is 5.0~8.0MPa, and volume space velocity is 0.5~1.2h-1, hydrogen to oil volume ratio be 300~
800。
Under preferable case, the cut point of the normal top oil and the normal line oil is 150~170 DEG C, the normal line oil
Cut point with the first vacuum side stream is 340~360 DEG C, and the first vacuum side stream and the cut point for subtracting base oil are 390~400
℃.For example, the cut point of the normal top oil and the normal line oil is 165 DEG C, the normal line oil and the first vacuum side stream
Cut point is 350 DEG C, and the first vacuum side stream and the cut point for subtracting base oil are 390 DEG C.
Under preferable case, it is dehydrated with the water content in the full fraction of coal tar raw material after mechanical purifying less than 0.05 weight
% is measured, content of impurities is less than 0.20 weight %.It is highly preferred that being dehydrated and the full fraction of coal tar raw material after mechanical purifying
In water content less than 0.03 weight %, content of impurities is less than 0.10 weight %.
The coal tar of the invention refers to pyrolysis of coal or coal generating gas or the coal tar that other processes generate.Therefore, the coal
Tar can be the coalite tar of coal generating gas generation, be also possible to pyrolysis of coal process (including semicoke, medium temperature coking, height
Warm process of coking) generate coalite tar or medium temperature coal tar or high temperature coal-tar full feedstock.Under preferable case, institute
Stating full fraction of coal tar raw material is at least one of coalite tar, medium temperature coal tar and high temperature coal-tar.
Present invention combination Fig. 1 provides a kind of preferred embodiment and produces bunker fuel oil, this method by coal tar
Include:
By through be dehydrated and mechanical purifying after full fraction of coal tar raw material 5 and hydrogen 6 mix after be introduced to slurry bed hydroprocessing
It contacts in reactor 1 with the heterogeneous slurry bed hydrogenation catalyst wherein contained to carry out hydrotreating；By the hydrotreating
The slurry bed system hydrogenator effluent obtained afterwards, which is introduced in separation and filtration system 2, to be separated, and obtains separation gas 8 respectively
With solid slag 7, the liquid phase after separation is introduced to progress normal pressure fractionation in atmospheric tower 3, obtains often top oil 9 and normal line oil 10 respectively,
And the material of 3 tower bottom of atmospheric tower is introduced in vacuum tower 4 and carries out vacuum fractionation, obtain first vacuum side stream 11 respectively and subtracts base oil
12, and the gas at 4 top of vacuum tower is introduced in subsequent vacuum system 15 and is further processed；By normal line oil 10
Partially subtract the mixture of the formation of base oil 12 as light fuel oil product 14 peculiar to vessel, and by first vacuum side stream 11 and remaining subtracts bottom
The mixture that oil 12 is formed is as heavy fuel oil product 13 peculiar to vessel；Wherein, the depth for controlling hydrotreating makes obtain normal one
The bicyclic above arene content in line oil is not higher than 15 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 85 weight %；And
It is not less than 20 not higher than 5 weight %, thrcylic aromatic hydrocarbon and four cycloaromatics total contents so that subtracting the above aromatic hydrocarbons total content in Fourth Ring in base oil
Weight %.
Preceding method provided by the invention also has the advantages that following specific:
1, the present invention makes full use of coal tar different fractions section hydro carbons feature, realizes that the property of different fractions section is complementary,
In the case where without using lubricity improver, low-sulfur high-lubricity marine fuel is produced by simple method；
2, method provided by the invention has the characteristics that adaptability to raw material is strong, device operation cycle is long.
The present invention will be described in detail by way of examples below.Following instance in case of no particular description,
Flow chart according to figure 1 carries out.
The property for the full fraction of coal tar raw material that following instance uses is shown in Table 1.
The heterogeneous slurry bed hydrogenation catalyst of high dispersive, the heterogeneous slurry of the high dispersive are used in slurry bed system hydrogenator
Bed catalyst be the carbon-based loaded catalyst of high-dispersion iron, consisting of: active carbon be used as carrier, active component be Fe with
Mo.Also, the weight ratio of Fe and Mo in the carbon-based loaded catalyst of high-dispersion iron based on the element are 1:0.2, with institute
The total weight of the carbon-based loaded catalyst of high-dispersion iron is stated, the content of the active component based on the element is 15 weights
Measure %.
Table 1: the property of full fraction of coal tar raw material
| Full fraction of coal tar raw material | |
| Density (20 DEG C)/(g/cm3) | 0.9998 |
| Carbon residue/% | 4.97 |
| Nitrogen content/(μ g/g) | 6100 |
| Sulfur content/(μ g/g) | 2200 |
| C content/weight % | 83.34 |
| H content/weight % | 9.61 |
| Asphalt content/weight % | 13.5 |
| Boiling range ASTM D-1160/ DEG C | |
| IBP | 172 |
| 50% | 370 |
| 95% | 505 |
| Tenor/(μ g/g) | |
| Fe | 46.9 |
| Ni | < 0.1 |
| V | < 0.1 |
| Na | 13.3 |
| Ca | 130.7 |
| Al | 8.1 |
Embodiment 1
It is heterogeneous with aforementioned high dispersive after tentatively being removed water and mechanical admixture using full fraction of coal tar in table 1 as raw material
Slurry bed hydrogenation catalyst after mixing, enters together with hydrogen and carries out hydrotreating in slurry bed system hydrogenator.With coal
On the basis of the total weight of tar stock, dosage of the heterogeneous slurry bed hydrogenation catalyst in terms of the active metallic element wherein contained
For 1.0 weight %.Be hydrogenated to logistics separated and fractionating system separate < 165 DEG C normal top is oily, 165~350 DEG C of normal lines
Oil, 350~390 DEG C of first vacuum side streams, > 390 DEG C subtract base oil.
The operation condition of embodiment 1 is shown in Table 2.Reactive hydrogen consumption and normal line oil and subtract base oil hydro carbons composition be shown in Table 3, to
That 3 weight % (on the basis of normal line oil) are added in normal line oil subtracts base oil, obtains the production of high-lubricity lightweight bunker fuel oil
Product, mix first vacuum side stream and residue subtracts base oil, obtain sweet heavy marine fuel oil product.Obtained lightweight bunker fuel oil
Product and heavy bunker fuel oil product property are shown in Table 4.
As shown in Table 4, using method of the invention, hydrogen consumption is only 1.50 weight %, and hydrogen consumption is lower；Obtained clean ship
It can be used as No. 4 light fuel oils of low-sulfur high-lubricity with fuel oil products；The heavy marine fuel oil product of production can be used as excellent
No. 120 bunker fuel oil blend components of low-sulfur of matter.
Table 2: the operating condition of embodiment 1
| Hydrogen partial pressure/MPa | 6.0 |
| Reaction temperature/DEG C | 400 |
| Hydrogen-oil ratio/(Nm3/m3) | 600 |
| Volume space velocity/h-1 | 1.0 |
Table 3: the hydrogen consumption and product hydrocarbon composition of embodiment 1
Table 4: 1 product property of embodiment
Embodiment 2
It is heterogeneous with aforementioned high dispersive after tentatively being removed water and mechanical admixture using full fraction of coal tar in table 1 as raw material
Slurry bed hydrogenation catalyst after mixing, enters together with hydrogen and carries out hydrotreating in slurry bed system hydrogenator.With coal
On the basis of the total weight of tar stock, dosage of the heterogeneous slurry bed hydrogenation catalyst in terms of the active metallic element wherein contained
For 1.5 weight %.Be hydrogenated to logistics separated and fractionating system separate < 170 DEG C normal top is oily, 170~355 DEG C of normal lines
Oil, 355~395 DEG C of first vacuum side streams, > 395 DEG C subtract base oil.
The operation condition of embodiment 2 is shown in Table 5.Reactive hydrogen consumption and normal line oil and subtract base oil hydro carbons composition be shown in Table 6, to
That 6 weight % (on the basis of normal line oil) are added in normal line oil subtracts base oil, obtains the production of high-lubricity lightweight bunker fuel oil
Product, mix first vacuum side stream and residue subtracts base oil, obtain sweet heavy marine fuel oil product.Obtained lightweight bunker fuel oil
Product and heavy bunker fuel oil product property are shown in Table 7.
As shown in Table 7, using method of the invention, hydrogen consumption is only 1.21 weight %, and hydrogen consumption is lower；Obtained clean ship
It can be used as No. 4 light fuel oils of low-sulfur high-lubricity with fuel oil products；The heavy marine fuel oil product of production can be used as excellent
No. 120 bunker fuel oil blend components of low-sulfur of matter.
Table 5: the operating condition of embodiment 2
| Hydrogen partial pressure/MPa | 8.0 |
| Reaction temperature/DEG C | 390 |
| Hydrogen-oil ratio/(Nm3/m3) | 400 |
| Volume space velocity/h-1 | 0.55 |
Table 6: the hydrogen consumption and product hydrocarbon composition of embodiment 2
Table 7: 2 product property of embodiment
Embodiment 3
It is heterogeneous with aforementioned high dispersive after tentatively being removed water and mechanical admixture using full fraction of coal tar in table 1 as raw material
Slurry bed hydrogenation catalyst after mixing, enters together with hydrogen and carries out hydrotreating in slurry bed system hydrogenator.With coal
On the basis of the total weight of tar stock, dosage of the heterogeneous slurry bed hydrogenation catalyst in terms of the active metallic element wherein contained
For 0.9 weight %.Be hydrogenated to logistics separated and fractionating system separate < 155 DEG C normal top is oily, 155~345 DEG C of normal lines
Oil, 345~390 DEG C of first vacuum side streams, > 390 DEG C subtract base oil.
The operation condition of embodiment 3 is shown in Table 8.Reactive hydrogen consumption and normal line oil and subtract base oil hydro carbons composition be shown in Table 9, to
That 8 weight % (on the basis of normal line oil) are added in normal line oil subtracts base oil, obtains the production of high-lubricity lightweight bunker fuel oil
Product, mix first vacuum side stream and residue subtracts base oil, obtain sweet heavy marine fuel oil product.Obtained lightweight bunker fuel oil
Product and heavy bunker fuel oil product property are shown in Table 10.
As shown in Table 10, using method of the invention, hydrogen consumption is only 1.86 weight %, and hydrogen consumption is lower；Obtained lightweight
Marine fuel oil product can be used as No. 4 light fuel oils of low-sulfur high-lubricity；The heavy marine fuel oil product of production can be used as
No. 180 bunker fuel oil blend components of good low-sulfur.
Table 8: the operating condition of embodiment 3
| Hydrogen partial pressure/MPa | 5.0 |
| Reaction temperature/DEG C | 420 |
| Hydrogen-oil ratio/(Nm3/m3) | 800 |
| Volume space velocity/h-1 | 1.2 |
Table 9: the hydrogen consumption and product hydrocarbon composition of embodiment 3
Table 10: 3 product property of embodiment
Comparative example 1
This comparative example is carried out using raw material same as Example 1.
The operating condition of the catalyst of this comparative example, catalyst amount and reactive moieties is the same as embodiment 2.It is only technique stream
Different in Cheng Shangyu embodiment 2, specifically: this comparative example will be hydrogenated to logistics and separate < 170 DEG C through separation and fractionating system
Often top oil, 170~355 DEG C of normal line oil, > 355 DEG C of heavy oil.
Meanwhile this comparative example gives the main character of the normal line oil and heavy oil of this comparative example acquisition by table 11.
Table 11: the product property of comparative example 1
| Normal line oil | Heavy oil | |
| Density (20 DEG C)/(g/cm3) | 0.8822 | 0.9253 |
| Kinematic viscosity (40 DEG C)/(mm2/s) | 3.886 | / |
| Kinematic viscosity (50 DEG C)/(mm2/s) | / | 17.35 |
| Carbon residue/weight % | < 0.1 | 0.65 |
| Ash content/weight % | < 0.002 | 0.01 |
| Sulfur content/(μ g/g) | 143 | 433 |
| Grinding defect diameter/μm | 486 | |
| Boiling range ASTM D-1160/ DEG C | ||
| IBP | 170 | 362 |
| 50% | 272 | 408 |
| 95% | 358 | 489 |
As can be seen from Table 11, the grinding defect diameter for the normal line oil that this comparative example obtains is 486 μm, much higher than the present invention
Embodiment in light fuel oil product peculiar to vessel grinding defect diameter, show the present invention to the polishing scratch for improving light fuel oil product peculiar to vessel
Diameter significant effect.
The preferred embodiment of the present invention has been described above in detail, and still, the present invention is not limited thereto.In skill of the invention
In art conception range, can with various simple variants of the technical solution of the present invention are made, including each technical characteristic with it is any its
Its suitable method is combined, and it should also be regarded as the disclosure of the present invention for these simple variants and combination, is belonged to
Protection scope of the present invention.
Claims (10)
1. a kind of method by coal tar production bunker fuel oil, this method comprises:
(1) it in the presence of heterogeneous slurry bed hydrogenation catalyst, will be dehydrated and the full fraction of coal tar raw material after mechanical purifying
It is introduced into slurry bed system hydrogenator and carries out hydrotreating；
(2) the slurry bed system hydrogenator effluent obtained after the hydrotreating is successively separated, normal pressure is fractionated and subtracts
Pressure fractionating obtains often pushing up oil, normal line oil, first vacuum side stream and subtracts base oil；
(3) normal line oil and part are subtracted into the mixture of base oil formation as light fuel oil product peculiar to vessel, and by first vacuum side stream
With the remaining mixture for subtracting base oil formation as heavy fuel oil product peculiar to vessel；
Wherein, the depth of the hydrotreating of rate-determining steps (1) makes the bicyclic above virtue in the normal line obtained in step (2) oil
Hydrocarbon content is not higher than 15 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 85 weight %；And to subtract in base oil Fourth Ring with
Upper aromatic hydrocarbons total content is not higher than 5 weight %, and thrcylic aromatic hydrocarbon and four cycloaromatics total contents are not less than 20 weight %.
2. according to the method described in claim 1, wherein, the depth of the hydrotreating of rate-determining steps (1) to obtain in step (2)
The bicyclic above arene content in normal line oil obtained is not higher than 10 weight %, and aromatic hydrocarbons and cycloalkane total content are not less than 90 weights
Measure %；And to subtract the above aromatic hydrocarbons total content in Fourth Ring in base oil not higher than 3 weight %, thrcylic aromatic hydrocarbon and four cycloaromatics total contents
Not less than 25 weight %.
3. method according to claim 1 or 2, wherein control is formed in the mixture of the light fuel oil product peculiar to vessel
The content for subtracting base oil make thrcylic aromatic hydrocarbon and four cycloaromatics total contents in the light fuel oil product peculiar to vessel be 2.5~5.0 weights
Measure %；Preferably,
The content for subtracting base oil that control is formed in the mixture of the light fuel oil product peculiar to vessel makes the light fuel oil peculiar to vessel
Thrcylic aromatic hydrocarbon and four cycloaromatics total contents are 3.0~4.5 weight % in product.
4. method described in any one of -3 according to claim 1, wherein contain in the heterogeneous slurry bed hydrogenation catalyst
There is at least one of coal dust, coke blacking and active carbon substance as decentralized medium, and contains the active group as dispersed phase
Point, the active component is selected from least one of group VIB base metal and group VIII base metal；Preferably,
The active component is at least one of iron, cobalt, nickel, molybdenum and tungsten.
5. according to the method described in claim 4, wherein, using the total weight of the heterogeneous slurry bed hydrogenation catalyst as base
Standard, the content of the active component based on the element are 2~20 weight %.
6. according to claim 1, method described in 4 or 5, wherein evaporated entirely through being dehydrated with the coal tar after mechanical purifying with described
Divide on the basis of the total weight of raw material, the additional amount of the heterogeneous slurry bed hydrogenation catalyst is 1.0~3.0 weight %, preferably
For 1.0~2.0 weight %.
7. method described in any one of -3 according to claim 1, wherein the condition of the hydrotreating in step (1)
Include: reaction temperature be 360~440 DEG C, hydrogen partial pressure be 5.0~10.0MPa, volume space velocity be 0.1~1.5h-1, hydrogen oil volume
Than being 200~1000；Preferably,
The condition of the hydrotreating in step (1) include: reaction temperature be 380~420 DEG C, hydrogen partial pressure be 5.0~
8.0MPa, volume space velocity are 0.5~1.2h-1, hydrogen to oil volume ratio is 300~800.
8. according to the method described in claim 1, wherein, the cut point of the normal top oil and the normal line oil is 150~170
DEG C, the cut point of the normal line oil and the first vacuum side stream is 340~360 DEG C, the first vacuum side stream and the base oil that subtracts
Cut point is 390~400 DEG C.
9. according to the method described in claim 1, wherein, being dehydrated and the water in the full fraction of coal tar raw material after mechanical purifying
Content is less than 0.05 weight %, and content of impurities is less than 0.20 weight %；Preferably,
It is dehydrated with the water content in the full fraction of coal tar raw material after mechanical purifying less than 0.03 weight %, content of impurities
Less than 0.10 weight %.
10. according to the method described in claim 1, wherein, the full fraction of coal tar raw material is coalite tar, medium temperature coal tar
At least one of oil and high temperature coal-tar.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711007125.7A CN109705909B (en) | 2017-10-25 | 2017-10-25 | Method for producing bunker fuel oil from coal tar |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711007125.7A CN109705909B (en) | 2017-10-25 | 2017-10-25 | Method for producing bunker fuel oil from coal tar |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109705909A true CN109705909A (en) | 2019-05-03 |
| CN109705909B CN109705909B (en) | 2020-11-13 |
Family
ID=66252370
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711007125.7A Active CN109705909B (en) | 2017-10-25 | 2017-10-25 | Method for producing bunker fuel oil from coal tar |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109705909B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112980484A (en) * | 2021-03-01 | 2021-06-18 | 内蒙古晟源科技有限公司 | Method for producing special marine heavy fuel oil by using coal tar as raw material |
| WO2022083587A1 (en) | 2020-10-19 | 2022-04-28 | 中国石油化工股份有限公司 | Method and system for producing fuel oil and use thereof, and fuel oil and use thereof |
| CN115651703A (en) * | 2022-11-11 | 2023-01-31 | 陕西延长石油（集团）有限责任公司 | Method for preparing low-sulfur marine fuel oil base oil from coal tar |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1706922A (en) * | 2004-06-07 | 2005-12-14 | 李英华 | Vehicle and ship fuel synthesized with residual oil and heavy oil and its prepn process |
| CN101113346A (en) * | 2006-07-28 | 2008-01-30 | 神木县三江煤化工有限责任公司 | Method for harmony production of bunker fuel by coal oil |
| CN101921633A (en) * | 2010-09-06 | 2010-12-22 | 锦州港船舶燃料供应有限责任公司 | Fuel oil composition |
| CN102888244A (en) * | 2012-10-22 | 2013-01-23 | 北京金海畅能源投资有限公司 | Production method of ship fuel oil |
| CN103695031A (en) * | 2013-12-27 | 2014-04-02 | 成都博晟能源科技有限公司 | Method for producing diesel oil and bunker fuel blend component from coal tar |
| US20150368567A1 (en) * | 2013-02-06 | 2015-12-24 | Envirollea Inc. | Thermal process to transform contaminated or uncontaminated feed materials into useful oily products, uses of the process, products thereby obtained and uses thereof, manufacturing of the corresponding plant |
| CN105778987A (en) * | 2016-02-23 | 2016-07-20 | 新疆恒晟能源科技有限公司 | Production method for biomass diesel oil and bunker fuel oil |
-
2017
- 2017-10-25 CN CN201711007125.7A patent/CN109705909B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1706922A (en) * | 2004-06-07 | 2005-12-14 | 李英华 | Vehicle and ship fuel synthesized with residual oil and heavy oil and its prepn process |
| CN101113346A (en) * | 2006-07-28 | 2008-01-30 | 神木县三江煤化工有限责任公司 | Method for harmony production of bunker fuel by coal oil |
| CN101921633A (en) * | 2010-09-06 | 2010-12-22 | 锦州港船舶燃料供应有限责任公司 | Fuel oil composition |
| CN102888244A (en) * | 2012-10-22 | 2013-01-23 | 北京金海畅能源投资有限公司 | Production method of ship fuel oil |
| US20150368567A1 (en) * | 2013-02-06 | 2015-12-24 | Envirollea Inc. | Thermal process to transform contaminated or uncontaminated feed materials into useful oily products, uses of the process, products thereby obtained and uses thereof, manufacturing of the corresponding plant |
| CN103695031A (en) * | 2013-12-27 | 2014-04-02 | 成都博晟能源科技有限公司 | Method for producing diesel oil and bunker fuel blend component from coal tar |
| CN105778987A (en) * | 2016-02-23 | 2016-07-20 | 新疆恒晟能源科技有限公司 | Production method for biomass diesel oil and bunker fuel oil |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022083587A1 (en) | 2020-10-19 | 2022-04-28 | 中国石油化工股份有限公司 | Method and system for producing fuel oil and use thereof, and fuel oil and use thereof |
| CN112980484A (en) * | 2021-03-01 | 2021-06-18 | 内蒙古晟源科技有限公司 | Method for producing special marine heavy fuel oil by using coal tar as raw material |
| CN115651703A (en) * | 2022-11-11 | 2023-01-31 | 陕西延长石油（集团）有限责任公司 | Method for preparing low-sulfur marine fuel oil base oil from coal tar |
| CN115651703B (en) * | 2022-11-11 | 2023-09-22 | 陕西延长石油（集团）有限责任公司 | Method for preparing low-sulfur marine fuel oil base oil from coal tar |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109705909B (en) | 2020-11-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101580728B (en) | Process technology for non-caking coal or weak caking coal | |
| AU2018222933B2 (en) | Combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar | |
| CN102465033B (en) | Processing method of medium-low temperature coal tar | |
| CN101429456B (en) | Delay coking hydrogenation combined process for coal oil | |
| CN105778987B (en) | A kind of production method of biodiesel and bunker fuel oil | |
| CN102453534B (en) | Method for producing gasoline and diesel oil through hydrogenation of coal tar | |
| CN107254330B (en) | Regeneration process for producing low-freezing-point lubricating oil base oil by using waste lubricating oil through total hydrogen method | |
| CN1903994A (en) | Method of producing fuel oil by coal tar hydrogenation modifying | |
| CN103205272A (en) | Method for production of purified coal tar pitch from high temperature coal tar | |
| CN109705909A (en) | By the method for coal tar production bunker fuel oil | |
| CN106906001B (en) | Method for co-processing coal with high content of inert components and heavy oil | |
| CN102863988B (en) | Coal tar combined machining method | |
| CN104498090B (en) | Perhydro moulded coal tar naphthenic base oils and the system and method for low-coagulation diesel oil | |
| CN104277879A (en) | Two-stage slurry bed hydrogenation process of medium and low temperature coal tar | |
| CN108300510B (en) | Method for producing fuel oil by hydrogenation of coal tar | |
| CN109355100B (en) | Coal tar processing and coal co-refining combined process | |
| CN110862837A (en) | System and method for grading, processing and utilizing full-fraction coal tar | |
| CN109722305B (en) | Method for producing low-carbon olefin | |
| CN110804464B (en) | Method for preparing green diesel oil by utilizing straw and waste engine oil through hydrogenation coupling pyrolysis | |
| CN109722306A (en) | The processing method of inferior heavy oil | |
| CN109355099B (en) | Method for preparing fuel oil by co-processing solid waste and coal tar | |
| CN104593061B (en) | A kind of residual hydrocracking and catalytic cracking combined processing method | |
| JP4902269B2 (en) | Caking material for coke production and its production method | |
| CN206204242U (en) | A kind of system of coal tar production light Fuel and needle coke | |
| CN106433773B (en) | The method that inferior heavy oil produces high-density propellant blend component |
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 |