CN206279164U - The system that a kind of coal tar maximizes production light Fuel and needle coke - Google Patents
The system that a kind of coal tar maximizes production light Fuel and needle coke Download PDFInfo
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- CN206279164U CN206279164U CN201621128524.XU CN201621128524U CN206279164U CN 206279164 U CN206279164 U CN 206279164U CN 201621128524 U CN201621128524 U CN 201621128524U CN 206279164 U CN206279164 U CN 206279164U
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Abstract
The utility model is related to the system that a kind of coal tar maximizes production light Fuel and needle coke.System of the present utility model includes blending tank, floating bed hydrogenation reactor, the first separator, the first filter, hydrofining reactor, the second separator, atmospheric distillation tower, delayed coking reaction device, washing tank, the second filter.The utility model can utilize dust high, high metal, high-sulfur, nitrogen high, the fast pyrogenation coal tar of resin and asphalt content high, to produce light Fuel and needle coke, improve the quality of needle coke, light fraction yield is significantly improved, while improving the economy of the technique.
Description
Technical field
The utility model is related to coal chemical technology, more particularly to a kind of coal tar to maximize production light Fuel and needle coke
System.
Background technology
Coal sub-prime, using being considered as to realize the effective way that Coal Clean is efficiently utilized, is also China " 13 " coal
The direction that chemical industry is given priority to.The sub-prime of coal is using exactly by being pyrolyzed to enter the coal gas in coal, coal tar and semicoke etc.
Row is separated.Wherein, coal tar can produce gasoline, diesel oil by hydrogenation, semicoke by pyrolysis be changed into low volatile, low-sulfur it is clear
Clean fuel or raw material.
Coal tar oil and gas to extract scale production quantities, coal sub-prime is utilized to be needed to realize scale, maximization.Coal heat
" tap " that solution technology is utilized as coal sub-prime, wherein, single set pyrolysis of coal unit scale is more and more large-scale, and pyrolysis rate
Also rapid to improve, residence time of the coal in pyrolysis oven is only several seconds, and pyrolysis oil gas overflows that speed is fast, and output coal tar
Mostly middle coalite tar, its property has bigger difference with the coal tar of conventional coking output.
The coal tar that fine coal carries out middle low-temperature rapid thermal solution generation is generally oily under water, and substantial amounts of coal dust and coal are contained in tar
Ash, gum asphaltic content is high, and viscosity is larger, and water content is higher, and heat endurance is poor.Especially in the low crude oil price epoch,
The deep processing of high-efficiency and economic is carried out to fast pyrogenation coal tar, for the economy important in inhibiting that coal sub-prime is utilized.Cause
This, the research to coal tar processing method is of increased attention.
Prior art one discloses a kind of coal tar hydrogenation process for maximally utilizing coal tar oil residue, and the technique is to steam
Evaporate obtain heavy distillat (>320 DEG C or>350 DEG C) hydrogenation reaction, hydrogenation products liquid phase warp are carried out using slurry bed system hydrogenation reactor
Hot high score is separated and obtains heavy residual stocks and light oil, and gas phase separately wins to obtain light oil through heat is low, this two parts light oil and distillation light oil (≤320
DEG C or≤350 DEG C) mixing, as the extractant of above-mentioned heavy residual stocks, obtains liquid phase after filtering, liquid phase obtains lightweight through distillation again
Oily, middle matter oil and mink cell focus, light oil and middle matter oil produce gasoline and aviation kerosine, mink cell focus conduct as hydrofinishing raw material
Delayed coking raw material produces needle coke, and coking liquid phase feeds as slurry bed system hydrogenation reaction.But, extraction of the light oil to heavy residual stocks
Limited efficacy, through the hetero atoms such as substantial amounts of sulphur, nitrogen, and trace meter, its direct work can be contained in the mink cell focus that distillation is obtained
To produce the raw material of needle coke, the quality of needle coke can be had a strong impact on.
Utility model content
The utility model aims to provide the system that a kind of coal tar maximizes production light Fuel and needle coke.This practicality is new
Type maximizing is using containing oil residue so that the coal tar of coal fast pyrogenation process generation is comprehensively utilized, and improves economy
Benefit.
The utility model proposes the system that a kind of coal tar maximizes production light Fuel and needle coke, the system bag
Include blending tank, floating bed hydrogenation reactor, the first separator, the first filter, hydrofining reactor, the second separator, often
Pressure destilling tower, delayed coking reaction device, washing tank, the second filter；
There is the blending tank coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material to export；
There is the floating bed hydrogenation reactor mixed material entrance, hydrogen inlet, crackate to export, the mixed material
Entrance is connected with the mixed material outlet of the blending tank；
There is first separator crackate entrance, cracked gas product outlet, hydrocracked liquid product to export, and this splits
Change product inlet to be connected with the crackate outlet of the floating bed hydrogenation reactor；
First filter has hydrocracked liquid product entrance, liquid-phase outlet, the hydrocracked liquid product entrance with it is described
The hydrocracked liquid product outlet connection of the first separator；
The hydrofining reactor have liquid phase entrance, hydrogen inlet, refined products export, the liquid phase entrance with it is described
The liquid-phase outlet connection of the first filter；
Second separator has refined products entrance, processed gas product exit, purification product exit, the essence
Product inlet processed is connected with the refined products outlet of the hydrofining reactor；
There is the atmospheric distillation tower purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy to evaporate
Sub-export, the purification product inlet is connected with the purification product exit of second separator；
The delayed coking reaction utensil has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid discharge
Mouthful, the heavy end entrance is connected with the heavy end outlet of the air-distillation device；
The washing tank have coking liquid inlet, oil-containing residue entrance, mixed material export, the coking liquid inlet with
The coking liquid outlet connection of the delayed coking reaction device；
Second filter has mixed material entrance, and the mixed material entrance goes out with the mixed material of the washing tank
Mouth connection.
Further, first filter also has oil-containing solid discharge.
Further, second filter also has oil phase outlet and solid discharge, oil phase outlet and the hydrogenation
The liquid phase entrance connection of finishing reactor.
The utility model can utilize dust high, high metal, high-sulfur, nitrogen high, the fast speed heat of resin and asphalt content high
Coal tar is solved to produce light Fuel and needle coke.
Used as the heavy end of production needle-shape coke raw material, the utility model can effectively remove the glue in the heavy end
Matter, asphalitine, metal and sulphur, and the content of four PAHs and five PAHs in needle coke is improved, and then it is effectively improved needle-like
Burnt quality.
The utility model can realize maximally utilizing containing oil residue.Coking liquid, can used as the extractant containing oil residue
Reclaimed containing the oil phase in oil residue with abundant, the oil phase can feed as hydrofining reaction, so as to significantly improve light fraction
Yield, while improving the economy of the technique.
Brief description of the drawings
Fig. 1 is that the system architecture of coal tar maximization production light Fuel and needle coke in the utility model embodiment is illustrated
Figure.
Fig. 2 is that the system flow of coal tar maximization production light Fuel and needle coke in the utility model embodiment is illustrated
Figure.
Reference in accompanying drawing is as follows：
1st, blending tank；2nd, floating bed hydrogenation reactor；3rd, the first separator；4th, the first filter；5th, hydrofining reaction
Device；6th, the second separator；7th, atmospheric distillation tower；8th, delayed coking reaction device；9th, washing tank；10th, the second filter.
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, it is the system of coal tar maximization production light Fuel and needle coke in the utility model embodiment
Structural representation.The system includes that the blending tank 1 being sequentially connected, floating bed hydrogenation reactor 2, the first separator 3, first are filtered
Device 4, hydrofining reactor 5, the second separator 6, atmospheric distillation tower 7, delayed coking reaction device 8, washing tank 9, second are filtered
Device 10.The specific annexation between each device is described in detail below.
Blending tank 1 has coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material outlet.
Floating bed hydrogenation reactor 2 has mixed material entrance, hydrogen inlet, crackate outlet.Wherein, mixed material
Entrance is connected with the mixed material outlet of blending tank 1.
First separator 3 has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet.Wherein, split
Change product inlet to be connected with the crackate outlet of floating bed hydrogenation reactor 2.
First filter 4 has hydrocracked liquid product entrance, liquid-phase outlet, oil-containing solid discharge.Wherein, cracked liquid is produced
Thing entrance is connected with the hydrocracked liquid product outlet of the first separator 3.
Hydrofining reactor 5 has liquid phase entrance, hydrogen inlet, refined products outlet.Wherein, liquid phase entrance and first
The liquid-phase outlet connection of filter 4.
Second separator 6 has refined products entrance, processed gas product exit, purification product exit.Wherein, essence
Product inlet processed is connected with the refined products outlet of hydrofining reactor 5.
Atmospheric distillation tower 7 has purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy end
Outlet.Wherein, purification product inlet is connected with the purification product exit of the second separator 6.
Delayed coking reaction device 8 has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid outlet.
Wherein, heavy end entrance is connected with the heavy end outlet of air-distillation device 7.
Washing tank 9 has coking liquid inlet, oil-containing residue entrance, mixed material outlet.Wherein, coking liquid inlet with
The oil-containing solid discharge of the coking liquid outlet connection of delayed coking reaction device 8, oil-containing residue entrance and the first filter 4 connects
Connect.
Second filter 10 has mixed material entrance, oil phase outlet, solid discharge.Wherein, mixed material entrance with wash
The mixed material outlet connection of tank 9 is washed, oil phase outlet is connected with the liquid phase entrance of hydrofining reactor 5.
Based on said system, the utility model also proposed a kind of coal tar and maximize production light Fuel and needle coke
Method.Fig. 2 is the idiographic flow schematic diagram of the method.
As shown in Figure 2, the utility model proposes coal tar maximize production light Fuel and needle coke method, including
Following steps：
Step A, coal tar are hydrocracked：Coal tar is dehydrated, and it is miscellaneous to remove bulky grain machinery therein
Matter, purifies to coal tar, then urges itself and suspension bed hydrogenation catalyst via coal tar oil-in, floating bed hydrogenation respectively
In agent entrance feeding blending tank 1, mixed material is obtained after being well mixed.After the blended material outlet discharge of mixed material, warp
By in mixed material entrance feeding floating bed hydrogenation reactor 2.Meanwhile, hydrogen is passed through thereto via hydrogen inlet so that mixed
Compound material carries out hydrocracking reaction in floating bed hydrogenation reactor 2, and the crackate obtained after reaction is via crackate
Outlet discharge.
Wherein, suspension bed hydrogenation catalyst selects heterogeneous mineral dust, specially pyrite, red mud, bloodstone, ferronickel
One or more in ore deposit, limonite, inorganic molybdenum salt, inorganic tungsten salt.Also, the addition of the suspension bed hydrogenation catalyst accounts for mixed
The percentage of compound material is 0.1~5wt% (wt% is mass percent).
In this step, the mixed material of coal tar and suspension bed hydrogenation catalyst enters in floating bed hydrogenation reactor 2
The reaction condition of row hydrocracking reaction is：Reaction pressure is 14~26MPa, preferably 16~24MPa；Reaction temperature is 390
~500 DEG C, preferably 400~470 DEG C.
The separating and filtering of step B, crackate：The crackate discharged in above-mentioned steps A send via crackate entrance
In entering the first separator 3.In the first separator 3, crackate carries out isolated cracked gas product, cracked liquid and produces
Thing, and respectively via cracked gas product outlet, hydrocracked liquid product outlet the first separator 3 of discharge.Then, by cracked liquid
After collection of products, in sending into the first filter 4 via hydrocracked liquid product entrance, be filtrated to get liquid phase, containing oil residue, and respectively
The first filter 4 is discharged via liquid-phase outlet, oil-containing solid discharge.
Step C, production light Fuel：The liquid phase discharged in above-mentioned steps B sends into hydrofining reaction via liquid phase entrance
In device 5, meanwhile, hydrogen is passed through via hydrogen inlet, wherein in the presence of Hydrobon catalyst, carry out hydrofinishing anti-
Should.Refined products are obtained after reaction, and via refined products outlet discharge hydrofining reactor 5.After refined products discharge, warp
In by refined products entrance the second separator 6 of feeding, processed gas product, purification product are obtained after separation, and pass through respectively
Second separator 6 is discharged by processed gas product exit, purification product exit.
During above-mentioned purification product is via purification product inlet feeding atmospheric distillation tower 7, stone brain is obtained after distillation
Oil distillate, diesel oil distillate, heavy end, and respectively via naphtha cut outlet, diesel oil distillate outlet, heavy end outlet row
Go out atmospheric distillation tower 7.Wherein, the light Fuel needed for naphtha cut, diesel oil distillate are the utility model.
Wherein, the hydrogenation active component in Hydrobon catalyst is one or more in Ni, Mo, W, the utility model
Carrier selection γ-Al in embodiment2O3。
In this step, the reaction condition for carrying out hydrofining reaction is：Reaction pressure is 8~15MPa, and reaction temperature is
380~440 DEG C, volume space velocity is 0.5~2.0h during liquid in course of reaction-1, hydrogen is (600 with the percent by volume of oil phase
~1200):1.
Wherein, volume space velocity is a kind of representation of air speed during liquid.In the utility model embodiment, volume space velocity during liquid
Refer to the volume that unit volume Hydrobon catalyst processes oil phase per hour.
Step D, prepare needle coke：The heavy end discharged in above-mentioned steps C sends into delay coke via heavy end entrance
Change in reactor 8, carry out delayed coking reaction and prepare needle coke, cooking gas, coking liquid, and respectively via needle coke
Outlet, cooking gas outlet, coking liquid outlet discharge delayed coking reaction device 8.
Step E, extraction are containing the oil phase in oil residue：The coking liquid discharged in above-mentioned steps D is via coking liquid inlet
In feeding washing tank 9.Meanwhile, the discharge of the first filter 4 is also fed into washing containing oil residue via oil-containing residue entrance in step B
In tank 9.Coking liquid is sufficiently mixed stirring in washing tank 9 and obtains mixed material as the extractant containing oil residue, and via
Mixed material outlet discharge washing tank 9.
Said mixture material is sent into the second filter 10 via mixed material entrance, is filtrated to get oil phase, residue, and divide
The second filter 10 is not discharged via oil phase outlet, solid discharge.
In the step, coking liquid can be reclaimed fully containing the oil phase in oil residue as the extractant containing oil residue.Obtained
During the oil phase for obtaining is via the liquid phase entrance feeding hydrofining reactor 5 of hydrofining reactor 5, as hydrofining reaction
Charging, so as to significantly improve light fraction yield.
The residue that extraction process is obtained in the step is used for metallurgical raw material.
Embodiment 1
The catalyst choice josephinite (iron content 48.5wt%, nickeliferous 1.5wt%) of floating bed hydrogenation reaction in the present embodiment,
Particle diameter is 100~200 mesh, and addition is 1.5wt%.The reaction condition of hydrocracking reaction is：Reaction pressure is 18MPa, instead
It is 440 DEG C to answer temperature.
Active component selection Ni, W composition metal of hydrofining reaction catalyst, wherein NiO and WO3Content be respectively
4.1wt%, 18.7wt%, carrier are γ-Al2O3.The reaction condition of hydrofining reaction is：Reaction pressure is 10MPa, reaction
Temperature is 400 DEG C, and volume space velocity is 1.0h during liquid-1, hydrogen is 800 with the percent by volume of oil phase：1.
The condition of delayed coking reaction is：Reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
In the present embodiment, coking liquid after stirring is sufficiently mixed in washing tank 9, is passed through as the extractant containing oil residue
Second filter 10 filters to isolate oil phase and residue, and the liquid phase that oil phase and the first filter 4 are isolated is together as hydrogenation essence
Make the charging of reaction.
The main character of the fast pyrogenation coal tar that embodiment 1 is used is shown in Table 1, and the primary product distribution for obtaining is shown in Table 2.
Embodiment 2
The catalyst choice nitric acid molybdenum of floating bed hydrogenation reaction in the present embodiment, the addition of the catalyst is 0.5wt%
(pressing the content meter of Mo elements), the reaction condition of hydrocracking reaction is：Reaction pressure is 22MPa, and reaction temperature is 460 DEG C.
Active component selection Ni, W, Mo composition metal of hydrofining reaction catalyst, wherein NiO, MoO, WO3Content
Respectively 4.1wt%, 5.2wt%, 20.7wt%, carrier are γ-Al2O3.The reaction condition of hydrofining reaction is：Reaction pressure
Power is 12MPa, and reaction temperature is 420 DEG C, and volume space velocity is 1.5h during liquid-1, hydrogen is 1000 with the percent by volume of oil phase：1.
The condition of delayed coking reaction is：Reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
In the present embodiment, coking liquid after stirring is sufficiently mixed in washing tank 9, is passed through as the extractant containing oil residue
Second filter 10 filters to isolate oil phase and residue, and the liquid phase that oil phase and the first filter 4 are isolated is together as hydrogenation essence
Make the charging of reaction.
The main character of the fast pyrogenation coal tar that embodiment 1 is used is shown in Table 1, and the primary product distribution for obtaining is shown in Table 2.
The main character of the fast pyrogenation coal tar of table 1
The embodiment 1 of table 2 and the primary product of embodiment 2 are distributed
As shown in Tables 1 and 2, the operating condition of embodiment 1 and embodiment 2 can realize the comprehensive profit of fast pyrogenation coal tar
With producing light Fuel and needle coke with industrial application value.
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 (3)
1. the system that a kind of coal tar maximizes production light Fuel and needle coke, it is characterised in that the system includes mixing
Tank, floating bed hydrogenation reactor, the first separator, the first filter, hydrofining reactor, the second separator, air-distillation
Tower, delayed coking reaction device, washing tank, the second filter；
There is the blending tank coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material to export；
There is the floating bed hydrogenation reactor mixed material entrance, hydrogen inlet, crackate to export, the mixed material entrance
It is connected with the mixed material outlet of the blending tank；
There is first separator crackate entrance, cracked gas product outlet, hydrocracked liquid product to export, and the cracking is produced
Thing entrance is connected with the crackate outlet of the floating bed hydrogenation reactor；
First filter has hydrocracked liquid product entrance, liquid-phase outlet, the hydrocracked liquid product entrance and described first
The hydrocracked liquid product outlet connection of separator；
There are the hydrofining reactor liquid phase entrance, hydrogen inlet, refined products to export, the liquid phase entrance and described first
The liquid-phase outlet connection of filter；
Second separator has refined products entrance, processed gas product exit, purification product exit, the refined product
Thing entrance is connected with the refined products outlet of the hydrofining reactor；
There is the atmospheric distillation tower purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy end to go out
Mouthful, the purification product inlet is connected with the purification product exit of second separator；
The delayed coking reaction utensil has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid outlet,
The heavy end entrance is connected with the heavy end outlet of the air-distillation device；
The washing tank have coking liquid inlet, oil-containing residue entrance, mixed material export, the coking liquid inlet with it is described
The coking liquid outlet connection of delayed coking reaction device；
Second filter has mixed material entrance, and the mixed material entrance is exported with the mixed material of the washing tank and connected
Connect.
2. system according to claim 1, it is characterised in that first filter also has oil-containing solid discharge.
3. system according to claim 1, it is characterised in that also there is second filter oil phase outlet and residue to go out
Mouthful, oil phase outlet is connected with the liquid phase entrance of the hydrofining reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621128524.XU CN206279164U (en) | 2016-10-17 | 2016-10-17 | The system that a kind of coal tar maximizes production light Fuel and needle coke |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621128524.XU CN206279164U (en) | 2016-10-17 | 2016-10-17 | The system that a kind of coal tar maximizes production light Fuel and needle coke |
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| Publication Number | Publication Date |
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| CN206279164U true CN206279164U (en) | 2017-06-27 |
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| CN201621128524.XU Withdrawn - After Issue CN206279164U (en) | 2016-10-17 | 2016-10-17 | The system that a kind of coal tar maximizes production light Fuel and needle coke |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106281447A (en) * | 2016-10-17 | 2017-01-04 | 北京神雾环境能源科技集团股份有限公司 | A kind of coal tar maximizes and produces light Fuel and the method and system of needle coke |
-
2016
- 2016-10-17 CN CN201621128524.XU patent/CN206279164U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106281447A (en) * | 2016-10-17 | 2017-01-04 | 北京神雾环境能源科技集团股份有限公司 | A kind of coal tar maximizes and produces light Fuel and the method and system of needle coke |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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Granted publication date: 20170627 Effective date of abandoning: 20180608 |
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| AV01 | Patent right actively abandoned |