CN106701186B - A kind of high temperature coal-tar processing method - Google Patents
A kind of high temperature coal-tar processing method Download PDFInfo
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- CN106701186B CN106701186B CN201510769120.2A CN201510769120A CN106701186B CN 106701186 B CN106701186 B CN 106701186B CN 201510769120 A CN201510769120 A CN 201510769120A CN 106701186 B CN106701186 B CN 106701186B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The present invention provides a kind of high temperature coal-tar processing method, and methods described includes following content：High temperature coal-tar enters demetalization processor after being mixed with solvent naphtha, the effluent obtained after being reacted with filler enters water scrubber, contacted with fresh water, obtained mixture enters dehydrating tower, high temperature coal-tar and water after isolated removing metal, obtained high temperature coal-tar enters fluidized bed reactor and carries out hydrogenation reaction, reaction effluent is fractionated to obtain light component and heavy constituent by flash-evaporation dehydration, the light component enters fixed bed reactors and carries out hydrogenation reaction, and reaction product obtains gas, naphtha and diesel oil after separation；Isolated heavy constituent all returns to fluidized bed reactor circular treatment, or part returns to fluidized bed reactor, and device is thrown away outside remainder.The inventive method in the metal in removing high temperature coal-tar under the conditions of mitigation, can slow down metal inactivation and the rising of bed pressure drop of catalyst in hydrogenation reactor.
Description
Technical field
The invention belongs to field of coal tar deep processing, and in particular to high temperature coal-tar low temperature, low cost, fast eliminating metal
And carry out the process of hydrotreating.
Background technology
Coal tar is the black or dark brown viscous liquid with pungent odour generated during coal destructive distillation, referred to as burnt
Oil, coal tar can be divided into low high three kind coal tar, wherein coalite tar 500 DEG C -600 DEG C different according to heating final temperature,
700 DEG C -900 DEG C of medium temperature coal tar, 900 DEG C -1100 DEG C of high temperature coal-tar, its processing temperature is different, the composition of corresponding coal tar
There is very big difference with property, especially high temperature coal-tar property is the most inferior, and middle coalite tar and high temperature coal-tar are two kinds
Completely different tar, composition do not have to, and water content is different, and also difference is very big for tenor, and high temperature coal-tar is a kind of black oil
The material of shape, there is special odor, and compared with middle coalite tar, high temperature coal-tar density is big, carbon residue is high, condensed-nuclei aromatics content
Height, especially high with the heavy constituent such as colloid, asphalitine content, tenor is high.Contain 10% ~ 30% moisture content in high temperature coal-tar,
And the state of Water-In-Oil is presented.Coalite tar processing method is not appropriate for handling high temperature coal-tar in, it is necessary to finds
New process route and process conditions.
As economic development and light-weight fuel oil demand constantly increase, coal tar hydrogenating is produced into light-weight fuel oil increasingly
The favor of tar producer is obtained, middle coalite tar hydrogenation production light Fuel oil tech is relatively ripe, in the industry cycle promotes
It is more.But middle coalite tar and high temperature coal-tar are two kinds of completely different tar, and nature difference is very big, high temperature coal-tar mesh
The industrialized device of front-end hydrogenation is relatively fewer, it is reported that industrialized device has Qitaihe treasured ACE Semi coal chemical industry limited at present
100,000 tons of industrialized units of company, it uses high temperature coal-tar back-end crop technology, by the colloid in coal tar, asphalitine and machinery
Impurity removal, light component is subjected to hydrotreating, in addition, not yet document report has industrialized plant running.Cause height
Warm coal tar fails extensive industrialized reason and its property composition much relations, and wherein one of reason is high temperature coal-tar restructuring
Divide content high, especially the condensed-nuclei aromatics such as colloid, asphalitine content is high, and the tenor such as wherein corresponding Fe, Ca, Na is special
Height, in using traditional fixed bed hydrogenation processing procedure, these metals can be deposited on catalyst surface or bed after being removed
In layer space, catalyst inactivation or bed pressure drop is caused to raise, especially Hydrodemetalation catalyst superficial metal deposition amount is big,
Catalyst inactivation speed and pressure drop rise speed especially cause device shortening service cycle soon.
Patent CN1676583A describes a kind of high temperature coal tar hydrocracking technique, and wherein high temperature coal tar introduces
Heating furnace is mixed with hydrogen, and hydrofining reactor, then the hydrogen isolated through exchanging heat into high-pressure separator are entered after mixing
Hydrofining reactor is returned to through circulating hydrogen compressor, generation oil enters low pressure separator, entered after low point of fuel oil of sub-department
Deoxidation tower, enter fractionating column after further taking off fuel gas, gasoline, diesel oil and lubricating oil are obtained after fractionation, tail oil enters to be hydrocracked
Reactor.A large amount of metals of content etc. are easily caused what catalyst inactivation and bed pressure drop rose in high temperature coal tar in this patent
Component, directly handled in the case where not anticipated to raw material using traditional hydrofining reactor, can cause to urge
Agent deactivation rate is accelerated and bed pressure drop rises, and then causes device shortening service cycle.
Patent CN200610105277.6 describes a kind of power plant's purification method of coal tar, needs to prepare in the method and mixes
Oil is closed, demulsifier is added, then heats, one-level electricity is respectively enterd and takes off, step, the steps such as two level electricity is de- and three-level electricity is de- are relatively multiple
It is miscellaneous, and cost is higher.
The content of the invention
It is big for tenor in current high temperature coal-tar, carry out hydrogenation reaction when hydrogenation reactor in catalyst for demetalation
The shortcomings that metal deposition capability is big, deactivation rate is fast, the present invention provide a kind of high temperature coal-tar processing method, Binding experiment research hair
The existence form of metal and actual tests result in existing coal tar, the gold in high temperature coal-tar is removed under relaxing process conditions
Category, coal tar raw material is purified, slow down metal inactivation and the rising of bed pressure drop of catalyst in hydrogenation reactor, be high temperature coal tar
Oil provides a kind of feasible hydrotreating method.
Found by studying, the existence form of metal and the existence form of metal in traditional residual oil have very in high temperature coal-tar
Big difference, metal is mainly the metals such as Ni, V in residual oil, and is existed more in the form of porphyrin metal complex, due to these metals
Be embedded in heavy constituent colloid and the asphalitine in residual oil, it is necessary in the presence of catalyst and hydrogen high temperature removal；And high temperature
Metal in coal tar mainly exists with metal oxide forms such as Fe, Ca, Na, and Ni, V tenor are seldom, this and its shape
Relevant into process, coal steam needs Water spray to cool down during High T-emperature Carbonization, and the salt such as Ca, Mg in water can enter in coal tar, together
When the dry distillation of coal during have substantial amounts of coal ash, furnace wall breakage thing and some mineral matters（Calcite, albite）Deng doping wherein,
These materials can carry substantial amounts of alkaline metal oxide（CaO, Na2O、MgO、Fe2O3）Into in high temperature coal-tar, at the same it is high
In warm coal tar storage and transportation, enter coal tar because the reasons such as corrosive pipeline also result in the part metals such as Fe ion
Oil, as the above analysis, the metal in high temperature coal-tar have be greatly with existing for mineral form, so if
It is clearly contretemps to be applied to again using traditional demetallated mode of residual oil on coal tar metal removal.But due to high temperature
Coal tar contains 10% ~ 30% moisture, and the state that Water-In-Oil is presented more, a certain degree of emulsification be present, is sent out during experiment
Now it is difficult to be demulsified to coal tar and remove metal therein using traditional in general demulsifier.
Based on above-mentioned discovery, the present invention provides a kind of high temperature coal-tar processing method, and methods described includes following content：
（1）High temperature coal-tar enters demetalization processor after merging preheated to 150~250 DEG C with oil miscible solvent, with taking off
The filler of filling is fully contacted and reacted in metal processor；
（2）Step（1）Obtained reaction effluent enters water scrubber, fully contacts with fresh water, is solved in reaction effluent
The metal inorganic substance come is separated out to be dissolved into water；
（3）Step（2）Obtained mixture enters dehydrating tower, carries out water-oil separating, obtains removing the high-temperature coal after metal
Tar and water；
（4）Step（3）Obtained high temperature coal-tar enters fluidized bed reactor after being mixed with hydrogen and carries out hydrogenation reaction, instead
Effluent is answered after flash-evaporation dehydration, is fractionated into obtaining light component and heavy constituent；
（5）Step（4）Isolated light component enters fixed bed reactors after being mixed with hydrogen, in the presence of a catalyst
Hydrogenation reaction is carried out, reaction product obtains gas, naphtha and diesel oil after separation；
（6）Step（4）Isolated heavy constituent all returns to fluidized bed reactor circular treatment, or part returns to boiling
A reactor is risen, device is thrown away outside remainder.
In the inventive method, the high temperature coal-tar is that heating final temperature obtains more than 900 DEG C through destructive distillation or coking
High temperature coal-tar, the boiling range of the high temperature coal-tar is 120 DEG C ~ 650 DEG C.
In the inventive method, the boiling range of the solvent naphtha is 65~450 DEG C, preferably 120~400 DEG C, more preferably 150
~320 DEG C, in the composition of the solvent naphtha, alkane and naphthene content are 70~90%, can be specifically hydrofinishing bavins
It is one or several kinds of mixed in oil, hydrofinishing naphtha, hydrofinishing washing oil, hydrofinishing light oil, hydrofinishing carbolic oil
Compound.
In the inventive method, step（1）Described in the mass ratio of solvent naphtha and high temperature coal-tar be 1:20~1:3, preferably
For 1:10~1:5.
In the inventive method, the step（1）In can also add auxiliary agent, the auxiliary agent is alcohols material, can be one
First alcohol or polyalcohol, preferably monohydric alcohol, can be specifically the one or more in methanol, ethanol, isopropanol, sec-butyl alcohol.
In the inventive method, the promoter addition is the 1/10000~1/100 of raw material weight of oil；It is preferred that 1/1000~
1/150。
In the inventive method, in the demetalization reactor filler of filling can be ceramic ring, quartz sand, activated carbon,
One or several kinds in diatomite, silica, aluminum oxide, zeolite, preferably ceramic ring, diatomite, activated carbon and silica；
The aperture of the filler is 200nm~50 μm, preferably 300nm~10 μm.
In the inventive method, 2~5 layers of filling of filler point in the demetalization reactor, preferably divide 3~4 layers of filling,
And along the aperture of Flow of Goods and Materials direction filler from large to small, while bed voidage is also from large to small, adjacent two layers filling
The pore size difference of thing is the nm of 50 nm~1000, to those skilled in the art, when dividing the multilayer to load filler,
The ratio of multilayer filler is that those skilled in the art can determine by existing knowledge.
In the inventive method, the demetalization reactor can be two and be arranged in parallel, when wherein a reactor reaches
During processing limit, switch another demetalization reactor.
In the inventive method, the filler of filling is different from traditional Hydrodemetalation catalyst in demetalization reactor, this
Filler has very strong appearance dirt and interception capacity in text, but does not have catalytic activity substantially；Therefore tradition can be avoided de-
Metallic catalyst is when high-temperature hydrogenation caused by aromatic hydrocarbons polycondensation the problems such as catalyst coking.
In the inventive method, step（4）Middle light component and heavy constituent cutting temperature be 320 DEG C~400 DEG C, preferably 340
DEG C~360 DEG C, the cutting temperature of weight component can be suitably adjusted according to feedstock property and ebullating bed reactor area temperature rise situation.
In the inventive method, step（4）Described in the reaction condition of fluidized bed reactor be：Reaction temperature 300 DEG C~400
DEG C, preferably 340 DEG C~380 DEG C, preferably 8~18MPa of reaction pressure, 10~16MPa, 0.2~8.0h of volume space velocity-1, it is excellent
Elect 0.4~4.0h as-1, hydrogen to oil volume ratio 100:1~1500:1, preferably 600:1~1200:1.
In the inventive method, step（5）Described in the operating conditions of fixed bed reactors be：Reaction temperature 240~380
DEG C, preferably 280~340 DEG C, preferably 3~18MPa of reaction pressure, 8~16MPa, 0.1~4.0h of volume space velocity-1, it is preferably
0.4~2.0h-1, hydrogen to oil volume ratio 100:1~1500:1, preferably 500:1~1300:1
In the inventive method, fixed bed reactors filling Hydrobon catalyst, generally with silicon-containing alumina or aluminum oxide
For carrier, using group VIB and/or group VIII metal as active metal component, the preferred molybdenum of group VIB and/or tungsten, the VIIIth race is excellent
Select cobalt or/and nickel.In described Hydrobon catalyst, group VIII metal content is calculated as 2wt% ~ 12wt%, the VIth B with oxide
Race's tenor is calculated as 5wt% ~ 25wt% with oxide.The Hydrobon catalyst can be prepared by prior art, can also
Select business Hydrobon catalyst.The business Hydrobon catalyst such as FDS-4A of Fushun Petrochemical Research Institute's development,
481-3, FH-40 etc..
In the inventive method, the catalyst in described fluidized bed reactor is the hydrogenation for the water resistant of coal tar development
Refined microspheric catalyst, using group VIB and group VIII metal as active metal component, wherein the preferred molybdenum of group VIB and/or
Tungsten, the preferred cobalt of group VIII metal or/and nickel, metal active constituent is cobalt, the one or more in nickel, molybdenum, tungsten, catalyst for refining
In can contain auxiliary agent, such as the one or more in K, P, Mg, Zr and Ca, group VIII metal content with oxide be calculated as 3wt% ~
10wt%, group VIB tenor are calculated as 6wt% ~ 30wt% with oxide.
In the inventive method, the gas-liquid separator and fractionating column are that current commercial plant is conventional and be people in the art
Separation equipment known to member.
Compared with prior art, the inventive method has the following advantages that：
1st, in the inventive method, it is found that the metal in high temperature coal-tar exists with inorganic salt form, using the inventive method
Metal impurities therein can be removed under the relative operating condition relaxed, avoid conventional method using hydrogenation high temperature removal into
The problem of this is high.
2nd, the inventive method operates the metal in removing coal tar at a lower temperature, can avoid alkadienes in coal tar
The problem of easy polycondensation causes catalyst inactivation at high temperature Deng unsaturated hydrocarbons.
3rd, in the inventive method, the demetalization processor inner stuffing is without carried metal, and aperture is big, retention and appearance dirt
Ability is strong, and cost is less than the catalyst for demetalation of the carried metal in conventional method, at the same can effectively catching remove
Metallic salt.
4th, in the inventive method, by using solvent naphtha as precipitating reagent, system can be destroyed by adding solvent naphtha
Colloidal stability, the viscous force between original component is on the one hand reduced, on the other hand by the weight such as asphalitine in glue core center
Component parses, and the components precipitate such as toluene insolubles and mechanical admixture for most being suspended at last in system gets off, simultaneous
Most precipitated metals get off.
5th, in the inventive method, after adding auxiliary agent alcohols material, because alcohols material contains hydroxyl, and in coal tar
Oxygenatedchemicals aldehydes matter property it is similar, can reach and dissolve each other, dissociateed in such coal tar come metal inorganic salt parent
It is water-based strong, have part metals and be dissolved into first in alcohols, and in dehydrating tower, alcohols is miscible with water, and alcohol-water mixture is not
Dissolved each other with coal tar raw material, such alcohols carries salt and entered in water, realizes and metal inorganic salt is extracted from coal tar.
6th, using fluidized bed reactor and corresponding catalyst treatment coal tar, effectively can disperse during coal tar hydrogenating
The heat of release, avoids focus from occurring, and helps to realize that reactor temperature is homogeneous, beneficial to reaction；Boiling-bed catalyst simultaneously
The problem of bed pressure drop caused by high aromatic hydrocarbons material reaction green coke can be avoided under back-mixing state rises.
Embodiment
Technical scheme is further illustrated below by specific embodiment, but is not limited to the embodiment.
High temperature coal-tar raw material and solvent oil nature are listed in table 1, demetalization processing respectively used by the embodiment of the present invention
Device process conditions are shown in Table 2.Ceramic ring, diatomite, activated carbon and two are loaded in direction respectively from top to bottom in the demetalization processor
Four kinds of fillers of silica, the apertures of four kinds of fillers are followed successively by 5 ~ 10 μm, 1 ~ 3 μm, 500nm ~ 900nm, 300 ~
500nm, the admission space ratio of four kinds of fillers is 30:25:25:20, flux oil is the naphtha that hydrotreating obtains
And diesel fuel mixtures.
The catalyst of filling is the hydrofinishing microspheric for the water resistant of coal tar development in the fluidized bed reactor
Catalyst, using group VIB as active metal component, wherein it is preferred that molybdenum and/or tungsten, auxiliary agent can be contained in catalyst for refining, such as
K, the one or more in P, Mg, Zr and Ca, group VIB tenor are calculated as 6wt% ~ 30wt% with oxide.Urged in reactor
Agent reserve is 60%；
Fixed bed reactors load Hydrobon catalyst, using aluminum oxide as carrier, using group VIB as active metal group
Divide, preferably molybdenum and/or tungsten.In described Hydrobon catalyst, group VIB tenor with oxide be calculated as 5wt% ~
25wt%.The Hydrobon catalyst is the FH-40 catalyst that Fushun Petrochemical Research Institute develops.
The coal tar of table 1 and dilution oil nature
Embodiment 1
Test raw material is high temperature coal-tar described in table 1, adds solvent naphtha in demetalization processing procedure and auxiliary agent, auxiliary agent are
Ethanol, concrete technology condition are shown in Table 2, and reaction result is shown in Table 3, table 4 and table 5.
Embodiment 2
Test raw material is high temperature coal-tar described in table 1, adds solvent naphtha in demetalization processing procedure and auxiliary agent, auxiliary agent are
Ethanol, concrete technology condition are shown in Table 2, and reaction result is shown in Table 3, table 4 and table 5.
Embodiment 3
Test raw material is middle coalite tar described in table 1, and solvent naphtha, concrete technology bar are added in demetalization processing procedure
Part is shown in Table 2, and reaction result is shown in Table 3, table 4 and table 5.
Embodiment 4
Test raw material is high temperature coal-tar described in table 1, adds solvent naphtha in demetalization processing procedure, but be added without and help
Agent, concrete technology condition are shown in Table 2, and reaction result is shown in Table 3, table 4 and table 5.
Comparative example 1
Comparative example 1 uses high temperature coal-tar as raw material, but solvent naphtha and auxiliary agent are added without in processing procedure, still using biography
The method of system is handled, for ease of comparing, using ebullated bed-fixed bed group technology and traditional catalyst for demetalation to institute
State raw material and carry out HDM processing, reaction condition is that temperature is 280, hydrogen dividing potential drop 15MPa, hydrogen to oil volume ratio 900, body
Product air speed is 0.5h-1, ebullated bed and fixed bed point hydrogenation conditions are shown in Table 2, and result of the test is shown in Table 3.
The demetalization processor of table 2 and ebullated bed-fixed bed hydrogenation reactor reaction condition
Metal removal effect contrasts under the conditions of the different disposal of table 3
The different material of table 4 is hydrogenated to the contrast of naphtha property
The different material of table 5 is hydrogenated to the contrast of diesel oil property
Claims (17)
1. a kind of high temperature coal-tar processing method, methods described includes following content：
（1）High temperature coal-tar enters demetalization processor after merging preheated to 150~250 DEG C with oil miscible solvent, with demetalization
The filler of filling is fully contacted and reacted in processor；
（2）Step（1）Obtained reaction effluent enters water scrubber, fully contacts with fresh water, is dissociateed in reaction effluent
The metal inorganic substance come is dissolved into water；
（3）Step（2）Obtained mixture enters dehydrating tower, carries out water-oil separating, obtains removing the high temperature coal-tar after metal
And water；
（4）Step（3）Obtained high temperature coal-tar enters fluidized bed reactor after being mixed with hydrogen and carries out hydrogenation reaction, reaction stream
Go out thing after flash-evaporation dehydration, be fractionated into obtaining light component and heavy constituent；
（5）Step（4）Isolated light component enters fixed bed reactors after being mixed with hydrogen, carries out in the presence of a catalyst
Hydrogenation reaction, reaction product obtain gas, naphtha and diesel oil after separation；
（6）Step（4）Isolated heavy constituent all returns to fluidized bed reactor circular treatment, or part returns to ebullated bed
Reactor, remainder throw away device outside.
2. in accordance with the method for claim 1, it is characterised in that：The boiling range of the high temperature coal-tar is 120 DEG C ~ 650 DEG C.
3. in accordance with the method for claim 1, it is characterised in that：The boiling range of the solvent naphtha is 65~450 DEG C.
4. according to the method described in claim 1 or 2, it is characterised in that：The solvent naphtha is hydrofining diesel oil, hydrofinishing
One or several kinds in naphtha, hydrofinishing washing oil, hydrofinishing carbolic oil.
5. in accordance with the method for claim 1, it is characterised in that：Step（1）Described in the matter of solvent naphtha and high temperature coal-tar
Amount is than being 1:20~1:3.
6. in accordance with the method for claim 1, it is characterised in that：Step（1）Middle addition auxiliary agent, the auxiliary agent are alcohols thing
Matter.
7. in accordance with the method for claim 6, it is characterised in that：The alcohols material is monohydric alcohol or polyalcohol, is specifically
One or more in methanol, ethanol, isopropanol, sec-butyl alcohol.
8. in accordance with the method for claim 6, it is characterised in that：The promoter addition is the 1/10000 of raw material weight of oil
~1/100.
9. in accordance with the method for claim 1, it is characterised in that：The filler of filling is porcelain in the demetalization reactor
One or several kinds in ring, quartz sand, activated carbon, diatomite, silica, aluminum oxide, zeolite.
10. in accordance with the method for claim 1, it is characterised in that：The aperture of the filler is 200nm~50 μm.
11. in accordance with the method for claim 1, it is characterised in that：2~5 layers of filler point in the demetalization reactor
Filling, and along the aperture of Flow of Goods and Materials direction filler from large to small, while bed voidage is also from large to small.
12. in accordance with the method for claim 11, it is characterised in that：The pore size difference of adjacent two layers filler is 50
The nm of nm~1000.
13. in accordance with the method for claim 1, it is characterised in that：Step（4）Middle light component and heavy constituent cutting temperature is
320 DEG C~400 DEG C.
14. in accordance with the method for claim 1, it is characterised in that：Step（4）Described in fluidized bed reactor reaction condition
For：300 DEG C~400 DEG C of reaction temperature, 8~18MPa of reaction pressure, 0.2~8.0h of volume space velocity-1, hydrogen to oil volume ratio 100:1~
1500:1。
15. according to the method described in claim 1 or 14, it is characterised in that：Step（4）Described in fluidized bed reactor reaction
Condition is：340 DEG C~380 DEG C of reaction temperature, 10~16MPa of reaction pressure, 0.4~4.0h of volume space velocity-1, hydrogen to oil volume ratio
600:1~1200:1.
16. in accordance with the method for claim 1, it is characterised in that：Step（5）Described in fixed bed reactors operating condition
For：240~380 DEG C, 3~18MPa of reaction pressure, 0.1~4.0h of volume space velocity of reaction temperature-1, hydrogen to oil volume ratio 100:1~
1500:1。
17. according to the method described in claim 1 or 16, it is characterised in that：Step（5）Described in fixed bed reactors operation
Condition is：280~340 DEG C, 8~16MPa of reaction pressure, 0.4~2.0h of volume space velocity of reaction temperature-1, hydrogen to oil volume ratio 500:1
~1300:1.
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| CN111849552B (en) * | 2019-04-30 | 2021-12-17 | 中国石油化工股份有限公司 | Coal tar full-fraction hydrogenation upgrading method and system |
| CN113122323B (en) * | 2021-04-21 | 2022-05-20 | 中国石油化工股份有限公司 | Coal-based solvent oil and production method and application thereof |
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| 煤焦油加氢制燃料油的试验研究;田小藏;《工业安全与环保》;20070731(第07期);第56-57页 * |
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