CN105567273A - Coal tar hydrogenation pretreatment method and coal tar hydrogenation treatment method - Google Patents
Coal tar hydrogenation pretreatment method and coal tar hydrogenation treatment method Download PDFInfo
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Abstract
The invention discloses a coal tar hydrogenation pretreatment method and a method for coal tar hydrogenation treatment by using the coal tar hydrogenation pretreatment method. The coal tar hydrogenation pretreatment method comprises the following steps: introducing materials containing coal tar and hydrogen to a hydrogenation protective reaction system to carry out hydrogenation pretreatment, so as to obtain a hydrogenation protective effluent; the hydrogenation pretreatment is implemented under the conditions of respectively introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil to the hydrogenation protective reaction system. The method disclosed by the invention can improve the utilization efficiency of a hydrogenation protective catalyst, and prolong the running cycle of a coal tar hydrogenation device, and further can obtain product oil of which the metal content is remarkably reduced. Furthermore, a diesel product obtained by the hydrogenation treatment method disclosed by the invention has high cetane number, low density and low sulfur and nitrogen content, thereby being a high-quality diesel oil blending component suitable for vehicles.
Description
Technical field
The present invention relates to a kind of weighted BMO spaces method of coal tar and a kind of hydroprocessing process of coal tar.
Background technology
Along with the fast development of Modern Coal-based Chemical (leading with gasification) coal preparing natural gas, ammonia from coal, olefin hydrocarbon making by coal, coal-ethylene glycol, coal aromatic hydrocarbons and coal liquifaction etc., the especially middle coalite tar output of coal tar presents the trend increased fast.
In recent years, in view of energy-saving and emission-reduction and environmental requirement, coal tar hydrogenating gordian technique break through, and the impact of the factor such as coal tar hydrogenating demonstration unit considerable benefit, domesticly start the coal tar hydrogenating investment tide.Up-to-date statistics display, China's coal tar production capacity about 2,350 ten thousand tons in 2013; Along with the release of newly-increased production capacity, within 2014, China's coal tar production capacity is by breakthrough 2,500 ten thousand tons.So far, domestic coal tar hydrogenating unit is gone into operation, exceeded 20 in the device quantity built and plan to build, and scale has exceeded 6,000,000 tons/year.The expansion of coal tar hydrogenating unit scale, not only solve the problem that the energy consumption of coking industry is high with discharge, also significantly improve the profitability of the sector, the market competitiveness and the level of resources utilization, facilitate coking industry green, sustainable health development.
At present, mainly the following aspects is divided into the processing and utilization approach of coal tar abroad: one is extract monomer product for master, such as German Lv Gete company can isolate 400 kinds of products from coal tar, the wherein industrialization of kind more than 200, mainly produces the Chemicals such as phenol, refined naphthalene, anthraquinone; Two is based on pitch deep processing, and with Mitsubishi Co., Ltd., Rilly company of the U.S. and Australian Koppars company for representative, main purpose produces needle coke, high class pavement pitch etc.; Three is directly burn as oil fuel; Four is take coal tar as stock oil, adopts the operational path of hydrofining or hydro-upgrading to produce diesel oil.
Because in coal tar raw material, metal content is higher, especially the content of Fe, Ca, Na is high, in coal tar hydrogenating process, these metals can be deposited on catalyst surface, and enter the less of granules of catalyst inside, therefore in hydrogenation unit operation process, beds pressure drop is risen very soon and is caused device shorter for running period.
Summary of the invention
The object of the invention is the defect overcoming prior art; a kind of utilising efficiency, the weighted BMO spaces method that extends coal tar hydrogenating unit running period that improve hydrogenation protecting catalyst are provided; the method of the present invention can obtain the significantly reduced product oil of metal content; and; the cetane value of the diesel product obtained by hydroprocessing process of the present invention is high, density is low, sulphur nitrogen content is low, is to be suitable for automobile-used fine-quality diesel oil blending component.
To achieve these goals, on the one hand, the invention provides a kind of weighted BMO spaces method of coal tar, the method comprises: the material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carries out weighted BMO spaces, obtain hydrogenation protecting effluent, described hydrogenation protecting reactive system comprises at least two hydrogenation protecting reactors and is sequentially connected in series the pipeline of described hydrogenation protecting reactor, and carrying out in described weighted BMO spaces process, first from the pipeline before and after first hydrogenation protecting reactor, in described hydrogenation protecting reactive system, high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is introduced respectively, until the pressure drop in described first hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after second hydrogenation protecting reactor, until the pressure drop in described second hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after next hydrogenation protecting reactor, the like, wherein, when introducing high temperature hydrogenation tail oil from the pipeline before last hydrogenation protecting reactor in described hydrogenation protecting reactive system, from the pipeline after last hydrogenation protecting reactor described, in described hydrogenation protecting reactive system, do not introduce low temperature hydrogenation tail oil.
On the other hand, the invention provides a kind of hydroprocessing process of coal tar, wherein, the method comprises:
(1) material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carry out weighted BMO spaces, obtain hydrogenation protecting effluent;
(2) carry out hydrotreatment by described hydrogenation protecting effluent introducing hydrogenation main reactor, obtain hydrogenation main reactor effluent;
(3) described hydrogenation main reactor effluent is carried out gas-liquid separation and fractionation successively, obtain hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil;
(4) described hydrogenation tail oil is divided at least two portions, wherein a part heats up and obtains described high temperature hydrogenation tail oil, and another part cooling obtains described low temperature hydrogenation tail oil;
Wherein, described weighted BMO spaces carries out according to aforesaid method of the present invention.
The significantly reduced product oil of metal content can be obtained by the hydroprocessing process of the weighted BMO spaces method and coal tar that adopt above-mentioned coal tar of the present invention, and, the cetane value of the diesel product obtained by hydroprocessing process of the present invention is high, density is low, sulphur nitrogen content is low, is to be suitable for automobile-used fine-quality diesel oil blending component.Aforesaid method of the present invention can improve the cycle of operation of the utilising efficiency prolongation coal tar hydrogenating treatment unit of hydrogenation protecting catalyst.When carrying out the hydrotreatment of coal tar by adopting method of the present invention; the result of embodiments of the invention 1 shows: the level (namely lower than 0.1 μ g/g) that method of the present invention makes the metal content in the coal tar after the process of hydrogenation protecting reactive system all be reduced to can't detect; the cetane value of the diesel oil distillate obtained is made to reach more than 42; density is lower than 0.86; sulphur nitrogen content is extremely low; it is extraordinary derv fuel oil blend component; and method of the present invention makes the device continuous cycle of operation long.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with embodiment one below.In the accompanying drawings:
Fig. 1 is the process flow diagram that the embodiment of the present invention 1 adopts.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
On the one hand, the invention provides a kind of weighted BMO spaces method of coal tar, the method comprises: the material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carries out weighted BMO spaces, obtain hydrogenation protecting effluent, described hydrogenation protecting reactive system comprises at least two hydrogenation protecting reactors and is sequentially connected in series the pipeline of described hydrogenation protecting reactor, and carrying out in described weighted BMO spaces process, first from the pipeline before and after first hydrogenation protecting reactor, in described hydrogenation protecting reactive system, high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is introduced respectively, until the pressure drop in described first hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after second hydrogenation protecting reactor, until the pressure drop in described second hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after next hydrogenation protecting reactor, the like, wherein, when introducing high temperature hydrogenation tail oil from the pipeline before last hydrogenation protecting reactor in described hydrogenation protecting reactive system, from the pipeline after last hydrogenation protecting reactor described, in described hydrogenation protecting reactive system, do not introduce low temperature hydrogenation tail oil.
In the weighted BMO spaces method of coal tar of the present invention, it should be noted that, when introducing described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after the some hydrogenation protecting reactors in described hydrogenation protecting reactive system in described hydrogenation protecting reactive system, in described hydrogenation protecting reactive system, described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is not introduced respectively from the pipeline before and after remaining hydrogenation protecting reactor, also be, in described hydrogenation protecting reactive system, each moment all only introduces described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after a hydrogenation protecting reactor in described hydrogenation protecting reactive system.
In method of the present invention; from the pipeline before and after hydrogenation protecting reactor, introduce high temperature hydrogenation tail oil respectively in described hydrogenation protecting reactive system and low temperature hydrogenation tail oil refers to, those skilled in the art can introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively by adopting the conventional means (such as by use pipeline etc.) used in this area from the pipeline before and after described hydrogenation protecting reactor in described hydrogenation protecting reactive system.In the present invention, described " before " and " afterwards " refer to that described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil are not directly inject in described hydrogenation protecting reactor, described high temperature hydrogenation tail oil can be introduced from the pipeline before the entrance of described hydrogenation protecting reactor, then form mixture with the stream contacts in hydrogenation protecting reactive system, this mixture enters in described hydrogenation protecting reactor; And described low temperature hydrogenation tail oil can be introduced from the pipeline after the outlet of described hydrogenation protecting reactor; then form mixture with the stream contacts in hydrogenation protecting reactive system, this mixture enters into the next hydrogenation protecting reactor of the downstream direction of directly connecting with described hydrogenation protecting reactor.In method of the present invention; there is no particular limitation described pipeline before and after hydrogenation protecting reactor to be injected to described hydrogenation protecting reactive system to the distance of the entrance and exit of decanting point on the pipeline of described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil and described hydrogenation protecting reactor respectively, and those skilled in the art can carry out selection adjustment according to practical situation after understanding of technical scheme of the present invention.
In method of the present invention, the pressure drop normal value of each hydrogenation protecting reactor in described hydrogenation protecting reactive system can be 0.3-0.5MPa usually.In the present invention; it should be noted that; the pressure drop normal value of each hydrogenation protecting reactor described can be aimed at full scale plant for 0.3-0.5MPa usually; and usually; in lab setup, pressure drop normal value is generally not higher than 0.015MPa, such as, in subsequent embodiment of the present invention; be exemplarily illustrate in laboratory conditions, the maximum value thus defining the pressure drop normal value of each hydrogenation protecting reactor is 0.015MPa.
The preferred embodiment of one according to the present invention, in described hydrogenation protecting reactive system, described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is introduced respectively from the pipeline before and after the some hydrogenation protecting reactors described hydrogenation protecting reactive system, when find the pressure drop in this hydrogenation protecting reactor higher than normal value and higher than normal value less than 150% time, stop in described hydrogenation protecting reactive system, introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after described hydrogenation protecting reactor, change from the next hydrogenation protecting reactor of its downstream direction be directly connected in series (along logistics direction) before and after pipeline in described next hydrogenation protecting reactor, introduce described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively, all the other the like.
The preferred embodiment of another kind according to the present invention, in described hydrogenation protecting reactive system, described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is introduced respectively from the pipeline before and after the some hydrogenation protecting reactors described hydrogenation protecting reactive system, when finding that the pressure drop in this hydrogenation protecting reactor is higher than normal value, and higher than normal value less than 120% time, stop in described hydrogenation protecting reactive system, introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after described hydrogenation protecting reactor, change from the next hydrogenation protecting reactor in its downstream be directly connected in series (along logistics direction) before and after pipeline in described next hydrogenation protecting reactive system, introduce described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively, all the other the like.
In the present invention; described higher than less than 150% of normal value refer to those skilled in the art can pressure drop in hydrogen guard reactor higher than normal value; and lower than normal value 150% pressure drop within the scope of any time stop from the pipeline before and after this hydrogen guard reactor, in described hydrogenation protecting reactor, introduce described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively, those skilled in the art can select in above-mentioned scope according to practical situation.The described implication representative higher than normal value less than 120% is similar, and the present invention does not repeat them here.
According to method of the present invention, described hydrogenation protecting reactive system can comprise 3-8 hydrogenation protecting reactor.
In method of the present invention, the temperature of described high temperature hydrogenation tail oil can be 200-400 DEG C; Be preferably 280-380 DEG C.
In method of the present invention, the temperature of described low temperature hydrogenation tail oil can be 30-150 DEG C; Be preferably 50-120 DEG C.
According to method of the present invention; the consumption introducing described high temperature hydrogenation tail oil from the pipeline before described hydrogenation protecting reactor in described hydrogenation protecting reactive system can for making the temperature entering the material before described hydrogenation protecting reactor after the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system higher than 270 DEG C; preferably higher than 275 DEG C, be more preferably 280-400 DEG C.
According to method of the present invention; the consumption introducing described low temperature hydrogenation tail oil from the pipeline after described hydrogenation protecting reactor in described hydrogenation protecting reactive system can for making the temperature entering the material before next hydrogenation protecting reactor after the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system lower than 250 DEG C; preferably lower than 200 DEG C, be more preferably 190-100 DEG C.
In method of the present invention; when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system, the reaction conditions in each hydrogenation protecting reactor described can be identical or different.
In method of the present invention, when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system, the reaction conditions in each hydrogenation protecting reactor described can comprise independently of one another: temperature of reaction is 200-400 DEG C; Be preferably 220-300 DEG C.
In method of the present invention, when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system, the reaction conditions in each hydrogenation protecting reactor described can comprise independently of one another: pressure is 8-20MPa; Be preferably 12-18MPa.
In method of the present invention; when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system, the reaction conditions in each hydrogenation protecting reactor described can comprise independently of one another: during liquid, volume space velocity is 0.1-2h
-1; Be preferably 0.2-1.2h
-1.
In method of the present invention, when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system, the reaction conditions in each hydrogenation protecting reactor described can comprise independently of one another: hydrogen to oil volume ratio is 500-2000:1; Be preferably 1000-1800:1.
In method of the present invention; when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before or after some hydrogenation protecting reactors in described hydrogenation protecting reactive system, the operational condition in all the other hydrogenation protecting reactors can comprise: temperature is 100-200 DEG C.
According to method of the present invention, in described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil, aromaticity content is not less than 25 % by weight separately; Preferably be not less than 40 % by weight separately.
Method according to the present invention; to the kind of the volume of each hydrogenation protecting reactor in described hydrogenation protecting reactive system and wherein loaded hydrogenation protecting catalyst, there is no particular limitation; the volume of each hydrogenation protecting reactor described can be the same or different, and those skilled in the art can select according to practical situation.Exemplarily giving described hydrogenation protecting catalyst in embodiments of the invention can for be developed by Research Institute of Petro-Chemical Engineering, the RGC-1 type hydrogenation protecting catalyst produced by China Petrochemical Industry's catalyzer Chang Ling branch office.In an embodiment of the present invention, in each hydrogenation protecting reactor, exemplarily load the hydrogenation protecting catalyst of same volume, and the volume of each hydrogenation protecting reactor is identical.
According to method of the present invention, preferred described coal tar is 120-200 DEG C entering the temperature before described hydrogenation protecting reactive system.
On the other hand, present invention also offers a kind of hydroprocessing process of coal tar, wherein, the method comprises:
(1) material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carry out weighted BMO spaces, obtain hydrogenation protecting effluent;
(2) carry out hydrotreatment by described hydrogenation protecting effluent introducing hydrogenation main reactor, obtain hydrogenation main reactor effluent;
(3) described hydrogenation main reactor effluent is carried out gas-liquid separation and fractionation successively, obtain hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil;
(4) described hydrogenation tail oil is divided at least two portions, wherein a part heats up and obtains described high temperature hydrogenation tail oil, and another part cooling obtains described low temperature hydrogenation tail oil;
Wherein, any one pretreatment process that the method for described weighted BMO spaces can adopt the present invention above-mentioned carries out.
According to method of the present invention, the boiling range of described hydrogenation tail oil can be 350-500 DEG C.
In the present invention, it should be noted that, the various method described in the weighted BMO spaces method of coal tar as aforesaid in the present invention and condition and parameter etc. all may be used for of the present invention as described in coal tar hydroprocessing process corresponding steps in, the present invention repeats no more this.
In the present invention, to the operation of described intensification and cooling, there is no particular limitation, and those skilled in the art can utilize the conventional various intensification that uses and cool-down method to carry out, and such as in the present invention, water cooler and electric heater can be adopted to carry out.
There is no particular limitation to described coal tar oil properties etc. for described method of the present invention, and those skilled in the art can adopt various full fraction of coal tar raw material as the coal tar raw material in method of the present invention.
According to method of the present invention, to the condition of described hydrogenation main reactor and gas-liquid separation and fractionation, there is no particular limitation, the various conditions that those skilled in the art can use according to routine are selected, such as described temperature of reaction can be 300-450 DEG C, pressure can be 8-20MPa, and during liquid, volume space velocity can be 0.1-2h
-1, hydrogen to oil volume ratio can be 500-2000:1.
Method according to the present invention, the main Hydrobon catalyst of appropriate volume can be loaded in described hydrogenation main reactor, there is no particular limitation to the kind of described main Hydrobon catalyst for method of the present invention, the various main Hydrobon catalyst that those skilled in the art can use according to routine is selected, such as, exemplarily adopt in embodiments of the invention and developed by Research Institute of Petro-Chemical Engineering, the main Hydrobon catalyst of RTC-2 type produced by China Petrochemical Industry's catalyzer Chang Ling branch office.
Method tool of the present invention has the following advantages:
1, by controlling the reaction depth of different runtime, different hydrogenation protecting reactor, the running period of coal tar hydrogenating unit is effectively improved;
2, by injecting hydrogenation tail oil in hydrogenation protecting system, the coking tendency of reaction high-temperature systems is reduced, prolong operating period.
Below will be described the present invention by embodiment.In following examples, in case of no particular description, the various raw materials used are commercially available product.
The character of the coal tar raw material used in following examples and comparative example is as shown in table 1.
Table 1
| Project | Numerical value |
| Density (20 DEG C)/(g/cm 3) | 1.0603 |
| Sulphur content/(μ g/g) | 2400 |
| Nitrogen content/(μ g/g) | 5000 |
| H content/% | 8.22 |
| Carbon residue/% | 6.61 |
| Ash oontent/% | 0.031 |
| Content of impurities/% | 0.31 |
| Metal content/(ug/g) | |
| Fe | 109 |
| Ni | 1.6 |
| V | 1.0 |
| Na | 15.2 |
| Ca | 333 |
| Al | 17.8 |
| Metal content adds up to/(ug/g) | 477.6 |
Embodiment 1
The present embodiment carries out in coal tar hydrogenating treatment unit, hydrogenation protecting system in the present embodiment comprises 3 hydrogenation protecting reactors of connecting successively, all load RGC-1 as hydrogenation protecting catalyst in these 3 hydrogenation protecting reactors, loadings is 20mL; The main Hydrobon catalyst RTC-2 of 100mL is loaded in described hydrogenation main reactor; The temperature of described high temperature hydrogenation tail oil is 350 DEG C, and the temperature of described low temperature hydrogenation tail oil is 60 DEG C.
The present embodiment adopts processing method as shown in Figure 1 to carry out, and is in particular:
Recycle hydrogen in device mixes with the coal tar raw material from pipeline 2 through pipeline 3 after mixing with the new hydrogen from pipeline 1, enter first hydrogenation protecting reactor 6 through pipeline 5 after mixing with the high temperature hydrogenation tail oil from pipeline 28 after interchanger 4 heat exchange to contact with hydrogenation protecting catalyst, reactor effluent flows out from described first hydrogenation protecting reactor 6 through pipeline 7, and mix with the low temperature hydrogenation tail oil from pipeline 25, then successively through reactor 8, pipeline 9, reactor 10 and pipeline 11 enter reaction heating furnace 12, hydrogenation main reactor 14 is entered through pipeline 13 after reaction heating furnace 12 heats, hydrogenation main reactor effluent enters Separate System of Water-jet 16 through pipeline 15, isolated gas is except portion is except pipeline 17 is discharged, all the other return hydrogenation protecting reactive system as recycle hydrogen.Enter separation column 19 by the isolated liquid stream of Separate System of Water-jet through pipeline 18 and isolate naphtha fraction, diesel oil distillate and tail oil fraction, wherein naphtha fraction and diesel oil distillate go out device as product, tail oil fraction is except partly going out except device, rest part is divided into two strands, and wherein one uses as described low temperature hydrogenation tail oil successively after pipeline 20 and pipeline 21 are lowered the temperature by interchanger 23; Another stock uses as high temperature hydrogenation tail oil successively after pipeline 20 and pipeline 22 are heated up by interchanger 27.When the pressure drop of first guard reactor 6 is higher than normal value, stop introducing high temperature hydrogenation tail oil by pipeline 28 and stopping introducing low temperature hydrogenation tail oil by pipeline 25, change and before second guard reactor 8, introduce described high temperature hydrogenation tail oil by pipeline 29, described low temperature hydrogenation tail oil changes to be introduced after second guard reactor 8 by pipeline 26, when the pressure drop of second guard reactor 8 is higher than normal value, stop the introducing of the high temperature hydrogenation tail oil of pipeline 29 and the low temperature hydrogenation tail oil of pipeline 26, high temperature hydrogenation tail oil changes to be introduced before the 3rd guard reactor 10 by pipeline 24.
When introducing described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil from the pipeline before and after first hydrogenation protecting reactor respectively in described hydrogenation protecting reactive system, described hydrogenation protecting reactive system is in the first stage; When introducing described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil from the pipeline before and after second hydrogenation protecting reactor respectively in described hydrogenation protecting reactive system, described hydrogenation protecting reactive system is in subordinate phase, the like.In each stage, the condition of each hydrogenation protecting reactor is as follows:
First stage: the temperature of first hydrogenation protecting reactor is 280 DEG C, the temperature of second hydrogenation protecting reactor is 180 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 180 DEG C, and the temperature of hydrogenation main reactor is 390 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 15MPa, and during liquid, volume space velocity is 1h
-1, hydrogen to oil volume ratio is 1000:1; The temperature of the material entered before described first hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before first hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 280 DEG C; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after first hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 180 DEG C.
Subordinate phase: the temperature of first hydrogenation protecting reactor is 180 DEG C, the temperature of second hydrogenation protecting reactor is 285 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 180 DEG C, and the temperature of hydrogenation main reactor is 390 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 15MPa, and during liquid, volume space velocity is 1h
-1, hydrogen to oil volume ratio is 1000:1; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before second hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 285 DEG C; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after second hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 180 DEG C.
Phase III: the temperature of first hydrogenation protecting reactor is 180 DEG C, the temperature of second hydrogenation protecting reactor is 180 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 290 DEG C, and the temperature of hydrogenation main reactor is 390 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 15MPa, and during liquid, volume space velocity is 1h
-1, hydrogen to oil volume ratio is 1000:1; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before the 3rd hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 290 DEG C, does not introduce low temperature hydrogenation tail oil wherein.
Initial operating stage is opened at the device of the present embodiment; the pressure drop of each hydrogenation protecting reactor is 0.01MPa; when device running 62h; pressure drop in first hydrogenation protecting reactor is increased to 0.014MPa; the pressure drop of all the other hydrogenation protecting reactors is still 0.01MPa, now operational condition is switched to subordinate phase.When being when the device is in operation 121h; the pressure drop of the second hydrogenation protecting reactor is increased to 0.014MPa; pressure drop in first hydrogenation protecting reactor is increased to 0.015MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is still 0.01MPa, now operational condition is switched to the phase III.When being when the device is in operation 179h; the pressure drop of the 3rd hydrogenation protecting reactor is increased to 0.014MPa; the pressure drop of the first hydrogenation protecting reactor is increased to 0.016MPa, and the pressure drop of the second hydrogenation protecting reactor rises to 0.015MPa, and now the stagnation pressure of hydrogenation protecting reactive system reduces to 0.045MPa.
In the different steps of device running, the aromaticity content in detection hydrogenation tail oil is all higher than 50 % by weight.
In the different steps of device running, the metal content from the outlet sampling analysis oil product of the 3rd hydrogenation protecting reactor, to observe the demetalization performance of hydrogenation protecting reactive system, the results are shown in Table 3.Stopped work by device and drawn off by each catalyzer, analyzing the content of Fe, Na and Ca on each catalyzer, calculated total deposition of the metal on catalyzer by metal content analysis result, data are in table 2.The bavin oil properties of table 4 for obtaining through separation column fractionation.
Table 2
Table 3
| Metal content/(μ g/g) | |
| Fe | <0.1 |
| Ni | <0.1 |
| V | <0.1 |
| Na | <0.1 |
| Ca | <0.1 |
| Al | <0.1 |
Table 4
| Density (20 DEG C)/(g/cm 3) | 0.8529 |
| Sulphur content/(μ g/g) | 5.9 |
| Nitrogen content/(μ g/g) | 2.1 |
| Viscosity (20 DEG C)/(mm 2/s) | 3.611 |
| Condensation point/DEG C | -22 |
| Flash-point/DEG C | 65 |
| Oxidation stability (total insoluble substance)/(mg/100mL) | 0.7 |
| Cetane value | 42.5 |
| Boiling range (ASTM D-86)/DEG C | |
| Initial boiling point/5 volume % | 168/194 |
| 10 volume %/20 volume % | 201/210 |
| 30 volume %/50 volume % | 219/233 |
| 70 volume %/80 volume % | 257/275 |
| 90 volume %/95 volume % | 308/338 |
| Final boiling point | 364 |
From the results shown in Table 3, the level (namely lower than 0.1 μ g/g) adopting method of the present invention that metal content in coal tar after the process of hydrogenation protecting reactive system is all reduced to can't detect.
From the results shown in Table 4, the cetane value of the diesel oil distillate adopting method of the present invention to make to obtain can reach more than 42, and density is lower than 0.86, and sulphur nitrogen content is extremely low, is extraordinary derv fuel oil blend component.
Comparative example 1
This comparative example adopts the method similar to embodiment 1 to carry out, and difference is:
In device operation process, before and after described hydrogenation protecting reactor, do not introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively.
Each hydrogenation protecting reactor adopts operational condition identical as follows when device operates, and is in particular:
The temperature of first hydrogenation protecting reactor is 280 DEG C, and the temperature of second hydrogenation protecting reactor is 280 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 280 DEG C, and the temperature of hydrogenation main reactor is 390 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 15MPa, and during liquid, volume space velocity is 1h
-1, hydrogen to oil volume ratio is 1000:1.
Initial operating stage is opened at the device of this comparative example, the pressure drop of each hydrogenation protecting reactor is 0.01MPa, when device runtime is 60h, pressure drop in first hydrogenation protecting reactor is increased to 0.014MPa, pressure drop in second hydrogenation protecting reactor is 0.01MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is 0.01MPa; When being when the device is in operation 92h, the pressure drop of the first hydrogenation protecting reactor is increased to 0.022MPa, and the pressure drop in the second hydrogenation protecting reactor is increased to 0.011MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is 0.01MPa; When being when the device is in operation 112h; the pressure drop of the first hydrogenation protecting reactor is increased to 0.033MPa; pressure drop in second hydrogenation protecting reactor is increased to 0.012MPa; pressure drop in 3rd hydrogenation protecting reactor is increased to 0.011MPa, and now hydrogenation protecting reactive system stagnation pressure reduces to 0.056MPa.
In the different steps of device running, the aromaticity content in detection hydrogenation tail oil is all higher than 40 % by weight.
Stopped work by device and drawn off by each catalyzer, analyzing the content of Fe, Na and Ca on each catalyzer, calculated total deposition of the metal on catalyzer by metal content analysis result, data are in table 5.
Table 5
The data of comparative example 1 and comparative example 1 and table 2 and table 5 can be found out; the runtime of comparative example 1 is shorter than embodiment 1; because the most of metal in comparative example has all been deposited on the hydrogenation protecting catalyst in the first hydrogenation protecting reactor; when the pressure drop rise of the first hydrogenation protecting reactor is after higher degree; catalyzer in second hydrogenation protecting reactor and the 3rd hydrogenation protecting reactor does not also play a role, and causes the waste of catalyzer thus.And adopt the method for embodiment 1 better can play the overall performance of the hydrogenation protecting catalyst in each hydrogenation protecting reactor; effective prolong operating period; and; as can be seen from above result also; adopt method demetalization ability of the present invention strong, make the metal content in product extremely low.
Embodiment 2
The present embodiment adopts the method similar to embodiment 1 to carry out, and difference is:
Each hydrogenation protecting reactor adopts following operational condition when device operates, and is in particular:
First stage: the temperature of first hydrogenation protecting reactor is 300 DEG C, the temperature of second hydrogenation protecting reactor is 160 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 160 DEG C, and the temperature of hydrogenation main reactor is 400 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 18MPa, and during liquid, volume space velocity is 1.2h
-1, hydrogen to oil volume ratio is 1200:1; The temperature of the material entered before described first hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before first hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 300 DEG C; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after first hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 160 DEG C.
Subordinate phase: the temperature of first hydrogenation protecting reactor is 160 DEG C, the temperature of second hydrogenation protecting reactor is 300 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 160 DEG C, and the temperature of hydrogenation main reactor is 400 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 16MPa, and during liquid, volume space velocity is 1.1h
-1, hydrogen to oil volume ratio is 1200:1; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before second hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 300 DEG C; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after second hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 160 DEG C.
Phase III: the temperature of first hydrogenation protecting reactor is 160 DEG C, the temperature of second hydrogenation protecting reactor is 160 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 305 DEG C, and the temperature of hydrogenation main reactor is 410 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 17MPa, and during liquid, volume space velocity is 1.1h
-1, hydrogen to oil volume ratio is 1300:1; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before the 3rd hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 305 DEG C, does not introduce low temperature hydrogenation tail oil wherein.
Initial operating stage is opened at the device of the present embodiment; the pressure drop of each hydrogenation protecting reactor is 0.01MPa; when device running 65h; pressure drop in first hydrogenation protecting reactor is increased to 0.014MPa; the pressure drop of all the other hydrogenation protecting reactors is still 0.01MPa, now operational condition is switched to subordinate phase.When being when the device is in operation 120h; the pressure drop of the second hydrogenation protecting reactor is increased to 0.013MPa; pressure drop in first hydrogenation protecting reactor is increased to 0.015MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is still 0.01MPa, now operational condition is switched to the phase III.When being when the device is in operation 182h; the pressure drop of the 3rd hydrogenation protecting reactor is increased to 0.015MPa; the pressure drop of the first hydrogenation protecting reactor is increased to 0.016MPa, and the pressure drop of the second hydrogenation protecting reactor rises to 0.014MPa, and now the stagnation pressure of hydrogenation protecting reactive system reduces to 0.045MPa.
In the different steps of device running, the aromaticity content in detection hydrogenation tail oil is all higher than 50 % by weight.
Stopped work by device and drawn off by each catalyzer, analyzing the content of Fe, Na and Ca on each catalyzer, calculated total deposition of the metal on catalyzer by metal content analysis result, data are in table 6.
Table 6
Embodiment 3
The present embodiment adopts the method similar to embodiment 1 to carry out, and difference is:
Each hydrogenation protecting reactor adopts following operational condition when device operates, and is in particular:
First stage: the temperature of first hydrogenation protecting reactor is 250 DEG C, the temperature of second hydrogenation protecting reactor is 140 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 140 DEG C, and the temperature of hydrogenation main reactor is 380 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 12MPa, and during liquid, volume space velocity is 0.9h
-1, hydrogen to oil volume ratio is 800:1; The temperature of the material entered before described first hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before first hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 280 DEG C; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after first hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 140 DEG C.
Subordinate phase: the temperature of first hydrogenation protecting reactor is 140 DEG C, the temperature of second hydrogenation protecting reactor is 250 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 140 DEG C, and the temperature of hydrogenation main reactor is 380 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 12MPa, and during liquid, volume space velocity is 0.9h
-1, hydrogen to oil volume ratio is 800:1; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before second hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 280 DEG C; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after second hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 140 DEG C.
Phase III: the temperature of first hydrogenation protecting reactor is 140 DEG C, the temperature of second hydrogenation protecting reactor is 140 DEG C; The temperature of the 3rd hydrogenation protecting reactor is 255 DEG C, and the temperature of hydrogenation main reactor is 380 DEG C; Pressure in hydrogenation protecting reactive system and hydrogenation main reactor is 12MPa, and during liquid, volume space velocity is 0.9h
-1, hydrogen to oil volume ratio is 800:1; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before the 3rd hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 280 DEG C, does not introduce low temperature hydrogenation tail oil wherein.
Initial operating stage is opened at the device of the present embodiment; the pressure drop of each hydrogenation protecting reactor is 0.01MPa; when device running 60h; pressure drop in first hydrogenation protecting reactor is increased to 0.014MPa; the pressure drop of all the other hydrogenation protecting reactors is still 0.01MPa, now operational condition is switched to subordinate phase.When being when the device is in operation 115h; the pressure drop of the second hydrogenation protecting reactor is increased to 0.013MPa; pressure drop in first hydrogenation protecting reactor is increased to 0.015MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is still 0.01MPa, now operational condition is switched to the phase III.When being when the device is in operation 175h; the pressure drop of the 3rd hydrogenation protecting reactor is increased to 0.015MPa; the pressure drop of the first hydrogenation protecting reactor is increased to 0.016MPa, and the pressure drop of the second hydrogenation protecting reactor rises to 0.014MPa, and now the stagnation pressure of hydrogenation protecting reactive system reduces to 0.045MPa.
In the different steps of device running, the aromaticity content in detection hydrogenation tail oil is all higher than 50 % by weight.
Stopped work by device and drawn off by each catalyzer, analyzing the content of Fe, Na and Ca on each catalyzer, calculated total deposition of the metal on catalyzer by metal content analysis result, data are in table 7.
Table 7
Embodiment 4
The present embodiment adopts the method similar to embodiment 1 to carry out, and difference is:
Each hydrogenation protecting reactor adopts following operational condition when device operates, and is in particular:
First stage: the temperature of the material entered before described first hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before first hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 280 DEG C; The temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after first hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 230 DEG C.
Subordinate phase: the temperature of the material entered before described second hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before second hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 285 DEG C; The temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the low temperature hydrogenation tail oil introduced from the pipeline after second hydrogenation protecting reactor makes the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 230 DEG C.
Phase III: the temperature of the material entered before described 3rd hydrogenation protecting reactor after the consumption of the high temperature hydrogenation tail oil introduced from the pipeline before the 3rd hydrogenation protecting reactor makes the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system is 290 DEG C, does not introduce low temperature hydrogenation tail oil wherein.
Initial operating stage is opened at the device of the present embodiment; the pressure drop of each hydrogenation protecting reactor is 0.01MPa; when device running 62h; pressure drop in first hydrogenation protecting reactor is increased to 0.014MPa; the pressure drop of all the other hydrogenation protecting reactors is still 0.01MPa, now operational condition is switched to subordinate phase.When being when the device is in operation 105h; the pressure drop of the second hydrogenation protecting reactor is increased to 0.015MPa; pressure drop in first hydrogenation protecting reactor is increased to 0.015MPa, and the pressure drop in the 3rd hydrogenation protecting reactor is still 0.01MPa, now operational condition is switched to the phase III.When being when the device is in operation 165h; the pressure drop of the 3rd hydrogenation protecting reactor is increased to 0.013MPa; the pressure drop of the first hydrogenation protecting reactor is increased to 0.016MPa, and the pressure drop of the second hydrogenation protecting reactor rises to 0.016MPa, and now the stagnation pressure of hydrogenation protecting reactive system reduces to 0.045MPa.Stopped work by device and drawn off by each catalyzer, analyzing the content of Fe, Na and Ca on each catalyzer, calculated total deposition of the metal on catalyzer by metal content analysis result, data are in table 8.
Table 8
Contrast the present embodiment and the result of comparative example can be found out, when adopting the method for the present embodiment to carry out the hydrotreatment of coal tar, can significantly improve the utilising efficiency of hydrogenation protecting catalyst, extend coal tar hydrogenating unit running period.
The result of contrast the present embodiment and embodiment 1 can be found out, when the consumption of the low temperature hydrogenation tail oil injected in each stage in the present embodiment is different, the effect obtained also is different, when the temperature of the mixture formed this low temperature hydrogenation tail oil is contacted by the consumption controlling low temperature hydrogenation tail oil with the material in described hydrogenation protecting reactive system after is 230 DEG C, the utilising efficiency of the hydrogenation protecting catalyst in each district is not as good as the result of embodiment 1, the cycle of operation of device is also not as good as the result of embodiment 1, but, find out compared to the result of comparative example 1, in the present embodiment, the metal content of catalyzer is apparently higher than the metal content in comparative example, also be, metal content in product in the present embodiment is starkly lower than in comparative example, also be good quality of product.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. a weighted BMO spaces method for coal tar, the method comprises: the material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carries out weighted BMO spaces, obtain hydrogenation protecting effluent, described hydrogenation protecting reactive system comprises at least two hydrogenation protecting reactors and is sequentially connected in series the pipeline of described hydrogenation protecting reactor, and carrying out in described weighted BMO spaces process, first from the pipeline before and after first hydrogenation protecting reactor, in described hydrogenation protecting reactive system, high temperature hydrogenation tail oil and low temperature hydrogenation tail oil is introduced respectively, until the pressure drop in described first hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after second hydrogenation protecting reactor, until the pressure drop in described second hydrogenation protecting reactor is introduced higher than stopping during normal value, then change and in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after next hydrogenation protecting reactor, the like, wherein, when introducing high temperature hydrogenation tail oil from the pipeline before last hydrogenation protecting reactor in described hydrogenation protecting reactive system, from the pipeline after last hydrogenation protecting reactor described, in described hydrogenation protecting reactive system, do not introduce low temperature hydrogenation tail oil.
2. method according to claim 1, wherein, the pressure drop normal value of each hydrogenation protecting reactor in described hydrogenation protecting reactive system is 0.3-0.5MPa.
3. method according to claim 1; wherein; until the pressure drop in described hydrogenation protecting reactor higher than normal value less than 150% time; stop from the pipeline before and after described hydrogenation protecting reactor, in described hydrogenation protecting reactive system, introduce high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively, preferably higher than normal value less than 120% time stop introduce.
4. method according to claim 1, wherein, described hydrogenation protecting reactive system comprises 3-8 hydrogenation protecting reactor.
5. according to the method in claim 1-4 described in any one, wherein, the temperature of described high temperature hydrogenation tail oil is 200-400 DEG C; The temperature of described low temperature hydrogenation tail oil is 30-150 DEG C.
6. according to the method in claim 1-4 described in any one; wherein; the consumption introducing described high temperature hydrogenation tail oil from the pipeline before described hydrogenation protecting reactor in described hydrogenation protecting reactive system makes the temperature entering the material before described hydrogenation protecting reactor after the mixing of materials in this high temperature hydrogenation tail oil and described hydrogenation protecting reactive system higher than 270 DEG C; preferably higher than 275 DEG C, be more preferably 280-400 DEG C.
7. according to the method in claim 1-4 described in any one; wherein; the consumption introducing described low temperature hydrogenation tail oil from the pipeline after described hydrogenation protecting reactor in described hydrogenation protecting reactive system makes the temperature entering the material before next hydrogenation protecting reactor after the mixing of materials in this low temperature hydrogenation tail oil and described hydrogenation protecting reactive system lower than 250 DEG C; preferably lower than 200 DEG C, be more preferably 190-100 DEG C.
8. method according to claim 1; wherein; when introducing high temperature hydrogenation tail oil and low temperature hydrogenation tail oil respectively from the pipeline before and after each hydrogenation protecting reactor in described hydrogenation protecting reactive system; reaction conditions in each hydrogenation protecting reactor described is identical or different, comprises independently of one another: when temperature of reaction is 200-400 DEG C, pressure is 8-20MPa, liquid, volume space velocity is 0.1-2h
-1, hydrogen to oil volume ratio is 500-2000:1; Preferably, the reaction conditions in each hydrogenation protecting reactor described comprises independently of one another: when temperature of reaction is 220-300 DEG C, pressure is 12-18MPa, liquid, volume space velocity is 0.2-1.2h
-1, hydrogen to oil volume ratio is 1000-1800:1.
9. method according to claim 1, wherein, in described high temperature hydrogenation tail oil and low temperature hydrogenation tail oil, aromaticity content is not less than 25 % by weight separately; Preferably be not less than 40 % by weight separately.
10. a hydroprocessing process for coal tar, wherein, the method comprises:
(1) material containing coal tar and hydrogen is introduced hydrogenation protecting reactive system and carry out weighted BMO spaces, obtain hydrogenation protecting effluent;
(2) carry out hydrotreatment by described hydrogenation protecting effluent introducing hydrogenation main reactor, obtain hydrogenation main reactor effluent;
(3) described hydrogenation main reactor effluent is carried out gas-liquid separation and fractionation successively, obtain hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil;
(4) described hydrogenation tail oil is divided at least two portions, wherein a part heats up and obtains described high temperature hydrogenation tail oil, and another part cooling obtains described low temperature hydrogenation tail oil;
Wherein, described weighted BMO spaces carries out according to the method in claim 1-9 described in any one.
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