CN206279166U - The system that a kind of coal tar maximizes production light Fuel - Google Patents
The system that a kind of coal tar maximizes production light Fuel Download PDFInfo
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- CN206279166U CN206279166U CN201621341301.1U CN201621341301U CN206279166U CN 206279166 U CN206279166 U CN 206279166U CN 201621341301 U CN201621341301 U CN 201621341301U CN 206279166 U CN206279166 U CN 206279166U
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Abstract
The utility model is related to the system that coal tar maximizes production light Fuel.System of the present utility model includes feed material preparation units, light fraction processing unit, heavy end processing unit：Feed material preparation units include mixing arrangement, floating bed hydrocracking device, separator (4), fractionating device (6) successively；Light fraction processing unit includes fixed bed hydrogenation refining plant, fixed bed hydrogenation cracking unit successively；Heavy end processing unit includes riser reactor, fractionating device (8) successively；Wherein, fractionating device (6) is connected with fixed bed hydrogenation refining plant, riser reactor respectively；Fractionating device (8) is connected with fixed bed hydrogenation refining plant, mixing arrangement respectively.The utility model can improve light Fuel yield, reach the purpose for maximizing production light-weight fuel oil.
Description
Technical field
The utility model is related to coal chemical technology, more particularly to the system that a kind of coal tar maximizes production light Fuel.
Background technology
As economic develops rapidly, China increasingly increases the demand of fuel oil.Due to most of fuel oil still need to from
Obtained in petroleum resources, the crude oil demand amount and external dependence degree of China are also increasing year by year.By 2014, crude oil in China
External dependence degree has reached 59.6%.Therefore, in face of the problem and the energy general layout of the few oil of China's richness coal of petroleum resources shortage,
Clean fuel is obtained from coal resource to have important practical significance.
Coal tar is the accessory substance of the dry distillation of coal, according to pyrolysis temperature, coal tar can be divided into high temperature coal-tar, middle temperature coal tar
Oily and middle coalite tar etc..Compared with high temperature coal-tar, middle coalite tar arene content is relatively low, saturated hydrocarbon content phase
To higher, closer to the composition of oil.Therefore, middle coalite tar is more suitable for producing cleaning combustion by hydrotreating techniques
Material oil product.
Due in middle coalite tar containing the solid impurity such as substantial amounts of coal dust, pyrolytic carbon, and colloid, asphalt content compared with
It is high.Therefore, coal tar is processed using traditional fixed bed hydrogenation technique, there is a problem of that easy green coke, the cycle of operation are shorter.Native land
Inside develop the technique that coal tar light component hydrogenation or delayed coking and fixed bed hydrogenation are combined, but coal tar utilization rate not
It is high.Also, though the impurity such as N, S, the O in coal tar can be removed using hydrofining technology, its lighting degree is relatively low, gained
Light-weight fuel oil product yield it is relatively low, economy is not high.Therefore, using suspension bed/slurry bed system/slurry bed system and fixed bed knot
Conjunction, hydrofinishing and the group technology for being hydrocracked combination, coal tar utilization rate is improved by maximizing, and produces light-weight fuel oil,
Improve the economy of coal tar processing.
Prior art discloses a kind of method of coal tar suspension bed catalytic hydrogenation.The method steams coal tar by normal pressure
Evaporate and be separated into carbolic oil cut, diesel oil distillate and heavy oil fraction.Dephenolize oil is obtained after carbolic oil distillate dephenolizing, heavy oil fraction is suspended
Bed hydroprocessing cracking, after carrying out separation of solid and liquid to isocrackate, distillation obtains product liquid, using bottom of towe tail oil as recycle oil
Mix with heavy oil fraction, upgrading unit is entered after the diesel oil distillate mixing in lighter products and dephenolize oil, raw material.But, tower
Bottom tail oil is recycled directly back to suspended-bed reactor, is not processed further, and reaction depth is relatively low, and utilization rate is low, and the method flow
It is more complicated.
Prior art two discloses a kind of method for processing full fraction of coal tar to produce fuel oil.The method is by coal tar
Heavy distillat is well mixed with catalyst and vulcanizing agent, and hydrocracking reaction, product point are carried out into paste state bed reactor after vulcanization
Naphtha, diesel oil and hydrogenation tail oil are obtained after evaporating, partial hydrogenation tail oil returns to paste state bed reactor as recycle oil, remaining hydrogenation
Enter fixed bed reactors after tail oil removing solid particle with coal tar light fraction, product fractionation obtains naphtha, diesel oil and adds
Hydrogen tail oil.But, full fraction of coal tar lighting effect is poor, and coal tar utilization rate is relatively low, and technological process is complicated.
Prior art three discloses a kind of method of producing diesel by utilizing coal tar.Full fraction of coal tar is separated into richness by the method
Asphalitine phase and poor asphalitine phase, rich asphalitine mix anti-into fixed bed after slurry bed system hydrogenation reaction with poor asphalitine
Device is answered, diesel product is obtained after hydrogenation products cutting, a portion hydrogenated diesel oil mixes as recycle oil with coal tar raw material.
But, diesel cycle amount is larger, and diesel product quantum of output is less, product lighting low degree.
Utility model content
The purpose of this utility model is essentially consisted in and solves the problems, such as that coal tar utilization rate is relatively low, there is provided a kind of floating bed hydrogenation
Cracking, fixed bed hydrogenation it is refined be hydrocracked system combine and process, effectively convert full fraction of coal tar, maximization output stone
The light fraction such as cerebrol and diesel oil, improves the utilization rate of coal tar.
The utility model proposes the system that a kind of coal tar maximizes production light Fuel, the system includes that raw material is pre-
Processing unit, light fraction processing unit, heavy end processing unit；
The feed material preparation units successively include mixing arrangement, floating bed hydrocracking device, separator (4), point
Distillation unit (6), the mixing arrangement has coal tar oil-in, catalyst inlet, vulcanizing agent entrance, fractionating device (6) tool
There is light fraction -1 to export, heavy end -1 is exported；
The light fraction processing unit includes fixed bed hydrogenation refining plant, fixed bed hydrogenation cracking unit, institute successively
Stating fixed bed hydrogenation refining plant has the entrance of light fraction -1, the entrance of light fraction -2, the entrance of light fraction -1 and institute
State the outlet connection of light fraction -1 of fractionating device (6)；
The heavy end processing unit includes riser reactor, fractionating device (8), the riser reactor successively
With the entrance of heavy end -1, the entrance of heavy end -1 is connected with the outlet of heavy end -1 of the fractionating device (6)；
The fractionating device (8) is exported with light fraction -2, heavy end -2 is exported, the light fraction -2 outlet with
The entrance of light fraction -2 connection of the fixed bed hydrogenation refining plant.
Further, the mixing arrangement also have the entrance of heavy end -2, the entrance of heavy end -2 with described point
The outlet connection of heavy end -2 of distillation unit (8).
The utility model can realize recycling for heavy end -2, and floating bed hydrocracking is entered after mixing with coal tar
Device, is conducive to the further reaction of heavy end -2, while being diluted, the charging for reducing floating bed hydrocracking device is glued
Degree, improves the mass transfer of reactant, reduces the generation of coke.Using system of the present utility model, the yield of light Fuel can be improved,
Reach the purpose for maximizing production light-weight fuel oil.
Brief description of the drawings
Fig. 1 is the system schematic of coal tar maximization production light Fuel in the utility model.
Fig. 2 is the process flow diagram of coal tar maximization production light Fuel in the utility model.
Reference in accompanying drawing is as follows：
1st, raw material preprocessing device；2nd, mixing arrangement；3rd, floating bed hydrocracking device；4th, separator；5th, system is reclaimed
System；6th, fractionating device；7th, riser reactor；8th, fractionating device；9th, fixed bed hydrogenation refining plant；10th, fixed bed hydrogenation splits
Makeup is put.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the present utility model is described in more details, with
Just scheme of the present utility model and the advantage of its various aspects be better understood when.However, specific implementations described below
Mode and embodiment are only descriptive purposes, rather than to limitation of the present utility model.
As shown in figure 1, being the system schematic of coal tar maximization production light Fuel in the utility model.This practicality is new
The system of type embodiment includes feed material preparation units, light fraction processing unit, heavy end processing unit.
Feed material preparation units include raw material preprocessing device 1, mixing arrangement 2, floating bed hydrocracking device 3, point
From device 4, recovery system 5, fractionating device 6.
Raw material preprocessing device 1 is used to carry out dehydrothermal pretreatment to coal tar raw material, with feed(raw material)inlet, pretreatment
Coal tar oil export.
Mixing arrangement 2 is mixed with slurry oil for coal tar and catalyst etc., enters with coal tar oil-in, catalyst
Mouth, the outlet of vulcanizing agent entrance, the entrance of heavy end -2, slurry oil.Wherein, the pre- place of coal tar oil-in and raw material preprocessing device 1
The oil export connection of reason coal tar.
Floating bed hydrocracking device 3 is used for the hydrocracking reaction of slurry oil, with slurry oil entrance, hydrogen inlet, gas phase
Outlet, liquid-phase outlet.Wherein, slurry oil entrance is connected with the slurry oil outlet of mixing arrangement 2.
Separator 4 is used for the separation of liquid phase, with liquid phase entrance, generation oil export, solid impurity outlet.Wherein, liquid
Phase entrance is connected with the liquid-phase outlet of floating bed hydrocracking device 3.Separator 4 includes dehydration device and filter.
Recovery system 5 is used to reclaim solid impurity, and with solid impurity entrance, the solid impurity with separator 4 is exported
Connection.
Fractionating device 6 be used for generate oil fractionation separate, with generation oil-in, light fraction -1 outlet, heavy end -
1 outlet.Also, generation oil-in is connected with the generation oil export of separator 4.
(2) light fraction processing unit includes fixed bed hydrogenation refining plant 9, fixed bed hydrogenation cracking unit 10 successively.
Fixed bed hydrogenation refining plant 9 is used for the hydrofining reaction of light fraction, with the entrance of light fraction -1, gently
The entrance of matter cut -2, hydrotreated product outlet.Wherein, the entrance of light fraction -1 is exported with the light fraction -1 of fractionating device 6
Connection.
Fixed bed hydrogenation cracking unit 10 further carries out hydrocracking reaction for hydrotreated product, with hydrogenation essence
Product inlet processed, naphtha outlet, diesel oil outlet.Also, hydrotreated product entrance adds with fixed bed hydrogenation refining plant 9
The outlet connection of hydrogen refined products.
(3) heavy end processing unit includes riser reactor 7, fractionating device 8 successively.
Riser reactor 7 carries out catalytic cracking reaction for heavy end, goes out with the entrance of heavy end -1, liquid phase
Mouthful.Also, the entrance of heavy end -1 is connected with the outlet of heavy end -1 of fractionating device 6.
There is fractionating device 8 liquid phase entrance, the outlet of light fraction -2, heavy end -2 to export.Wherein, liquid phase entrance with carry
The entrance of light fraction -2 of the liquid-phase outlet connection of riser reactors 7, the outlet of light fraction -2 and fixed bed hydrogenation refining plant 9
Connection, the outlet of heavy end -2 is connected with the entrance of heavy end -2 of mixing arrangement 2.
As shown in Fig. 2 being the process flow diagram of coal tar maximization production light Fuel in the utility model.Utilize
System of the present utility model, it is possible to achieve coal tar maximizes the purpose of production light Fuel, comprises the following steps：
Step A：Coal tar, catalyst, vulcanizing agent are mixed in mixing arrangement 2, slurry oil is obtained.Then, by oil
Hydrocracking reaction is carried out in slurry feeding floating bed hydrocracking device 3, product obtains gas phase and liquid after gas-liquid separation
Phase.In gained liquid phase feeding separator 4, moisture is removed through dehydration device, and through filter filtering and removing solid, given birth to
Into oil and solid impurity.
Above-mentioned coal tar was pre-processed in raw material preprocessing device 1 first before mixing arrangement 2 is sent into.This is pre-
Processing procedure is heated, until coal tar without carrying out removing mechanical admixture treatment to coal tar raw material after need to being only dehydrated to it
Oil is in flow regime, is easy to it to mix with catalyst.Pretreated coal tar oil viscosity is relatively low, is conducive to follow-up removing machinery
Impurity, first coal tar is pre-processed remove again mechanical admixture method can increase light Fuel yield while, reduce
Requirement to coal tar dustiness.The utility model can convert the resin and asphalt of easy green coke in coal tar heavy component, have
Reacted beneficial to heavy component, and reduced carbon deposit therein, extended the cycle of operation.
In solid impurity feeding recovery system 5, removal process is：There is thermal cracking in pyrolytic reaction device in solid impurity
Reaction, the oil phase that reaction is obtained is processed after mixing with coal tar raw material, and the solid for obtaining is circulated after burning as catalyst
Use.
The use of catalyst is iron system micro-spherical catalyst or other cheap and urging with relatively low hydrogenation activity in the step
Agent, particle diameter is 100~300 μm.The reaction temperature of hydrocracking reaction is 400~440 DEG C, and hydrogen partial pressure is 10~16MPa,
Hydrogen to oil volume ratio is 600~1400, and reaction velocity is 0.5~1.5h-1。
By hydrocracking reaction, the easy green coke material in coal tar is stripped of substantially, can completely convert heavy therein
Component (>500 DEG C), the requirement of fixed bed hydrogenation treatment charging is met, the preliminary lighting of coal tar is realized, and tentatively take off
Sulphur removal, nitrogen, oxygen, metal impurities, while reducing the viscosity of coal tar, are conducive to removing the mechanical admixture in coal tar.
Step B：It is fractionated in the generation oil feeding fractionating device 6 that above-mentioned steps are obtained, more than cut point T1
To heavy end -1, below cut point T1 obtains light fraction -1.
Above-mentioned cut point T1 is 350~370 DEG C.
Step C：Above-mentioned light fraction -1 is sequentially sent to fixed bed hydrogenation refining plant 9, fixed bed hydrogenation cracking unit
In 10, hydrofining reaction and hydrocracking reaction are carried out respectively, finally give octane number naphtha cut higher and cleaning
Diesel oil distillate.
(1) in the step, the Hydrobon catalyst that hydrofining reaction is used is loaded catalyst, major catalyst
It is clover strip, the ㎜ of diameter 2, carried metal is nickel molybdenum system, and used as auxiliary agent, carrier is γ-Al to phosphorus2O3.Hydrofinishing is catalyzed
The composition of agent is：1wt%~5wt% nickel oxide, 8wt%~15wt% molybdenum oxides, 0.5wt%~3wt% phosphorous oxides, 77wt%
~90.5wt% γ-Al2O3(wt% is mass percent).Protective agent is loaded on major catalyst top, protective agent is inert material
The Raschig ring being made, for depositing metal and mechanical admixture for being remained in oil product etc..
The reaction temperature of hydrofining reaction is 330~350 DEG C, and hydrogen partial pressure is 6~10MPa, and hydrogen to oil volume ratio is 800
~1400, reaction velocity is 0.8~1.2h-1.By hydrofining reaction, be significantly stripped of in light fraction -1 it is nitrogenous,
Oxygen, sulphur compound, to meet the feed needs of hydrocracking reaction, and fractional saturation polycyclic aromatic hydrocarbon, are conducive to polycyclic aromatic hydrocarbon to enter
There is hydrocracking reaction in one step, beneficial to its conversion.
(2) hydrocracking catalyst that hydrocracking reaction is used is difunctional loaded catalyst, and catalyst is three leaves
Swath shape, diameter 1.5mm, carried metal is nickel molybdenum system, and used as auxiliary agent, carrier is γ-Al to phosphorus2O3With the mixing of Y type molecular sieve
The percentage that thing, wherein Y type molecular sieve account for carrier is 25wt%~45wt%.The composition of hydrocracking catalyst is：1wt%~
5wt% nickel oxide, 8wt%~15wt% molybdenum oxides, 0.5wt%~5wt% phosphorous oxides, 75wt%~90.5wt% carriers.
The reaction temperature of hydrocracking reaction is 370~410 DEG C, and hydrogen partial pressure is 6~10MPa, and hydrogen to oil volume ratio is 800
~1400, reaction velocity is 0.8~1.5h-1.By hydrocracking reaction, the significantly lighting of coal tar, naphtha are realized
Yield with diesel oil is higher.Meanwhile, the disconnected side chain of the aromatic hydrocarbons open loop of fractional saturation in hydrotreated product maximizes production short-side chain
Aromatic hydrocarbons, is conducive to improving the octane number of naphtha and the Cetane number of diesel oil, and coal tar utilization rate is substantially improved, clean fuel oil
Yield lifting, the remarkable in economical benefits of processing technology.
Step D：Catalytic cracking reaction is carried out in the feeding riser reactor 7 of heavy end -1 that step B is obtained, is reacted
Product obtains liquid phase through three phase separation.By in liquid phase feeding fractionating device 8, cut point T2 heavy end -2 derived above are divided
Evaporate below temperature T2 and obtain light fraction -2.Heavy end is separated to be obtained including cut oil distillate and heavy oil fraction.
By above-mentioned light fraction -2 via the entrance of light fraction -2 feeding fixed bed hydrogenation refining plant 9 in, evaporated with lightweight
Dividing -1 mixing carries out hydrofining reaction.And by heavy end -2 via the entrance of heavy end -2 feeding mixing arrangement 2 in, with coal
Tar is mixed, hence into carrying out hydrocracking reaction in floating bed hydrocracking device 3.
Above-mentioned cut point T2 is 350~370 DEG C.
Embodiment
Embodiment 1 is raw material from a kind of typical coal tar, and its property is analyzed, and the results are shown in Table 1.
The coal tar raw material property analysis result of table 1
Coal tar, heavy end -2, catalyst are mixed, is stirred under the conditions of 80 DEG C.Used catalyst be 100~
300 μm of ferrum-based catalysts, catalyst content is 2wt%.Slurry oil is into being hydrogenated with floating bed hydrocracking device after mixing
Cracking reaction.Hydrocracking reaction hydrogen partial pressure is 16MPa, and reaction temperature is 440 DEG C, and hydrogen to oil volume ratio is 1200, and reaction is empty
Speed is 1.5h-1.Wherein more than 25 μm of solid impurity is removed by filter after product gas-liquid separation, is generated
Oil.
Generation oil is fractionated into device fractionation<370 DEG C of light fraction -1 and>370 DEG C of heavy end -1.Lightweight is evaporated
Divide -1 and the mixing of light fraction -2, send into fixed bed hydrogenation refining plant.Hydrobon catalyst composition for nickel oxide 2wt%,
Molybdenum oxide 15wt%, phosphorous oxide 1.5wt%, balance of γ-Al2O3.Hydrofining reaction hydrogen partial pressure is 10MPa, reaction temperature
It it is 350 DEG C, hydrogen to oil volume ratio is 1400, reaction velocity is 1.2h-1.Hydrotreated product enters in fixed bed hydrogenation cracking unit
Carry out hydrocracking reaction, hydrocracking catalyst composition is nickel oxide 3wt%, molybdenum oxide 15wt%, phosphorous oxide 3wt%, remaining
It is carrier to measure, and Y type molecular sieve content is 25wt% in carrier.Hydrocracking reaction hydrogen partial pressure is 10MPa, reaction temperature 370
DEG C, hydrogen to oil volume ratio is 800, and reaction velocity is 1.5h-1.Isocrackate is by after gas-liquid separation, fractionation, obtaining naphtha
Cut and diesel oil distillate.
In the present embodiment 1, coal tar by after the treatment of floating bed hydrocracking device, wherein>500 DEG C of heavy component
Conversion is completed, toluene insolubles content is reduced to 2% or so.The naphtha yield that the present embodiment is obtained reaches for 46%, RON
85, diesel yield is 53%, lighting effect is significant.
Embodiment 2 uses coal tar raw material same as Example 1.Floating bed hydrocracking used catalyst content is
1.5wt%, hydrocracking reaction hydrogen partial pressure is 16MPa, 420 DEG C of temperature, hydrogen to oil volume ratio 1400, reaction velocity 0.5h-1。T1
350 DEG C are with T2.Fixed bed hydrogenation catalyst for refining composition for nickel oxide 2wt%, molybdenum oxide 15wt%, phosphorous oxide 2wt%,
Balance of γ-Al2O3.Hydrofining reaction hydrogen partial pressure is 8MPa, and reaction temperature is 350 DEG C, and hydrogen to oil volume ratio is 1000, instead
It is 1.2h to answer air speed-1.Fixed bed hydrogenation Cracking catalyst composition for nickel oxide 1wt%, molybdenum oxide 12wt%, phosphorous oxide 2wt%,
Balance of carrier, Y type molecular sieve content is 35wt% in carrier.Hydrocracking reaction hydrogen partial pressure is 8MPa, reaction temperature 410
DEG C, hydrogen to oil volume ratio is 1400, and reaction velocity is 1.0h-1。
In the present embodiment 2, coal tar by after the treatment of floating bed hydrocracking device, wherein>500 DEG C of heavy component
Conversion is completed, toluene insolubles content is reduced to 3% or so.The naphtha yield that the present embodiment is obtained reaches for 42%, RON
89, diesel yield is 58%, lighting effect is significant.
Embodiment 3 uses coal tar raw material same as Example 1.Floating bed hydrocracking used catalyst content is
2wt%, hydrocracking reaction hydrogen partial pressure 16MPa, 420 DEG C of temperature, hydrogen to oil volume ratio 800, reaction velocity 1.0h-1.T1 and T2
It is 350 DEG C.Fixed bed hydrogenation catalyst for refining composition is nickel oxide 1wt%, molybdenum oxide 12wt%, phosphorous oxide 3wt%, surplus
It is γ-Al2O3.Hydrofining reaction hydrogen partial pressure is 6.5MPa, and reaction temperature is 340 DEG C, and hydrogen to oil volume ratio is 1200, reaction
Air speed is 1.0h-1.Fixed bed hydrogenation Cracking catalyst composition is nickel oxide 2.5wt%, molybdenum oxide 12wt%, phosphorous oxide
0.5wt%, balance of carrier, Y type molecular sieve content is 45wt% in carrier.Hydrocracking reaction hydrogen partial pressure is 6.5MPa,
400 DEG C of reaction temperature, hydrogen to oil volume ratio is 800, and reaction velocity is 0.8h-1。
In the present embodiment 3, coal tar by after the treatment of floating bed hydrocracking device, wherein>500 DEG C of heavy components are
Conversion is completed, toluene insolubles content is reduced to 3% or so.The naphtha yield that the present embodiment is obtained be 43%, RON up to 91,
Diesel yield is 57%, lighting effect is significant.
Embodiment 4 uses coal tar raw material same as Example 1.Floating bed hydrocracking used catalyst content is
2wt%, hydrocracking reaction hydrogen partial pressure 10MPa, 400 DEG C of temperature, hydrogen to oil volume ratio 600, reaction velocity 1.0h-1.T1 and T2
It is 370 DEG C.Fixed bed hydrogenation catalyst for refining composition is nickel oxide 5wt%, molybdenum oxide 8wt%, phosphorous oxide 0.5wt%, remaining
It is γ-Al to measure2O3.Hydrofining reaction hydrogen partial pressure is 10MPa, and reaction temperature is 330 DEG C, and hydrogen to oil volume ratio is 800, reaction
Air speed is 0.8h-1.Fixed bed hydrogenation Cracking catalyst composition is nickel oxide 5wt%, molybdenum oxide 8wt%, phosphorous oxide 5wt%, remaining
It is carrier to measure, and Y type molecular sieve content is 45wt% in carrier.Hydrocracking reaction hydrogen partial pressure is 6MPa, reaction temperature 380
DEG C, hydrogen to oil volume ratio is 1200, and reaction velocity is 1.2h-1。
In the present embodiment 4, coal tar by after the treatment of floating bed hydrocracking device, wherein>500 DEG C of heavy components are
Conversion is completed, toluene insolubles content is reduced to 3% or so.The naphtha yield that the present embodiment is obtained be 40%, RON up to 86,
Diesel yield is 54%, lighting effect is significant.
Comparative example 1 is using coal tar raw material same as Example 1, catalyst and technological parameter, floating bed hydrocracking
After generation oil carries out being dehydrated de- mechanical admixture, it is directly entered in fixed bed reactors, the naphtha yield of gained is 37%, diesel oil
Yield is 46%,>350 DEG C of cut (heavy end) yields are 17%.
That is, the utility model can realize that coal tar maximizes production light Fuel.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate the utility model example,
And not to the restriction of implementation method.For those of ordinary skill in the field, may be used also on the basis of the above description
To make other changes in different forms.There is no need and unable to be exhaustive to all of implementation method.And thus
Among the obvious change or variation amplified out are still in protection domain of the present utility model.
Claims (2)
1. the system that a kind of coal tar maximizes production light Fuel, it is characterised in that the system includes pretreatment of raw material list
Unit, light fraction processing unit, heavy end processing unit；
The feed material preparation units include mixing arrangement, floating bed hydrocracking device, separator (4), fractionation dress successively
Put (6), the mixing arrangement has coal tar oil-in, catalyst inlet, vulcanizing agent entrance, and the fractionating device (6) is with light
The outlet of matter cut -1, heavy end -1 are exported；
The light fraction processing unit includes fixed bed hydrogenation refining plant, fixed bed hydrogenation cracking unit successively, described solid
Fixed bed hydro-refining unit has the entrance of light fraction -1, an entrance of light fraction -2, the entrance of light fraction -1 with described point
The outlet connection of light fraction -1 of distillation unit (6)；
The heavy end processing unit includes riser reactor, fractionating device (8) successively, and the riser reactor has
The entrance of heavy end -1, the entrance of heavy end -1 is connected with the outlet of heavy end -1 of the fractionating device (6)；
The fractionating device (8) is exported with light fraction -2, heavy end -2 is exported, the light fraction -2 outlet with it is described
The entrance of light fraction -2 connection of fixed bed hydrogenation refining plant.
2. system according to claim 1, it is characterised in that the mixing arrangement also has the entrance of heavy end -2, institute
The entrance of heavy end -2 is stated to be connected with the outlet of heavy end -2 of the fractionating device (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201621341301.1U CN206279166U (en) | 2016-12-07 | 2016-12-07 | The system that a kind of coal tar maximizes production light Fuel |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621341301.1U CN206279166U (en) | 2016-12-07 | 2016-12-07 | The system that a kind of coal tar maximizes production light Fuel |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106433779A (en) * | 2016-12-07 | 2017-02-22 | 北京神雾环境能源科技集团股份有限公司 | System and method for maximum production of light fuel by coal tar |
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2016
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106433779A (en) * | 2016-12-07 | 2017-02-22 | 北京神雾环境能源科技集团股份有限公司 | System and method for maximum production of light fuel by coal tar |
| CN106433779B (en) * | 2016-12-07 | 2018-09-07 | 神雾科技集团股份有限公司 | A kind of coal tar maximizes the system and method for production light Fuel |
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