CN207143178U - A kind of device of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon - Google Patents
A kind of device of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon Download PDFInfo
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- CN207143178U CN207143178U CN201721099944.4U CN201721099944U CN207143178U CN 207143178 U CN207143178 U CN 207143178U CN 201721099944 U CN201721099944 U CN 201721099944U CN 207143178 U CN207143178 U CN 207143178U
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Abstract
The device of a kind of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon, including coal tar reactor, coal tar product component solvent dewaxing unit and fatty aromatic hydrocarbons and aromatic hydrocarbon process units；Coal tar reactor bottom is connected with solvent orange 2 A recovery column overhead, the tower reactor discharge pipe of solvent orange 2 A recovery tower is through coal tar reaction product extractive reaction kettle with being connected at the top of modified coal tar pitch knockout drum, modified coal tar pitch knockout drum bottom is connected with coal tar product component solvent dewaxing unit, and coal tar product component solvent dewaxing unit is connected with fatty aromatic hydrocarbons and aromatic hydrocarbon process units.The utility model makes full use of the property feature of coal tar each component reasonably to utilize separation method, coal tar high-effective classifying sub-prime is set to utilize, and be follow-up coal tar deep processing using having established good basis, while separating step is few, obvious energy conservation, to the release agent economical and efficient repeated recycling utilize in separation process, operating condition is gentle, continuously-running is easily enlarged production scale.
Description
Technical field
It the utility model is related to coal tar processing technology field, and in particular to a kind of coal tar production modified coal tar pitch, fat
The device of hydrocarbon and aromatic hydrocarbon.
Background technology
China is oil starvation, few gas, the country of relatively rich coal, is big coal country again, recently as the development of coal chemical industry, is made
Also rise year by year for the yield of byproduct coal tar.Falling sharply with petroleum resources simultaneously so that the processing and utilization day of coal tar
Benefit is paid attention to by country.Coal tar is the liquid by-product that coal obtains in pyrolytic process.It is higher for value
It mainly contains aliphatic compound, compound fragrant hydrocarbon and phenolic compound etc. for middle coalite tar.Wherein fat
Fat hydrocarbon compound is the important component of the fuel oil such as gasoline, diesel oil, is that hydrogenation produces the excellent of high cetane number diesel oil
Raw material；Compound fragrant hydrocarbon has petrochemical industry to obtain or can not the high added value essence such as economy obtained naphthalene, anthracene, phenanthrene and pyrene
Thin chemicals；Phenolic compound is important industrial chemicals, in synthetic fibers, engineering plastics, agricultural chemicals, medicine, preservative, plasticising
Agent, spices and dyestuff intermediate etc. have extensive purposes, belong to high added value fine chemical product.Therefore how efficiently,
Economic, environmental protection separation coal tar has seemed particularly significant.
The processing mode of current traditional coal tar is mainly cut into different boiling using the method for distillation to coal tar
Cut, then further separated in the cut to different boiling, the method such as neutralized to light fraction by alkali cleaning, pickling separates
Crude phenols component and neutral oil ingredient are obtained, obtains coal tar pitch through distilling tower reactor generation heavy end, or use solvent-extracted side
Method obtains coal tar with respect to enriched composition.
Traditional method using distillation is that coal tar is cut into the cut of different boiling, is then used.But
Some components are wider with boiling point distribution, are cut according to boiling point and preliminary separation is simply carried out to coal tar, not to mesh
Mark cut and carry out more accurate and more efficient separation and concentration, necessarily result in the complex energy consumption of separating step of subsequent product
It is higher.
Phenol method such as is carried for the separation of phenols, the industrialized acid-base method of tradition, not only operating procedure is more, Er Qieneng
Consumption is higher, produces more reluctant phenol wastewater, causes the problems such as serious environmental pollution.Phase in recent years simultaneously
After there are some demonstrative projects such as middle coalite tar hydrogenation of total effluent made fuel oil and delayed coking-hydrogenation made fuel oil,
Due to not carrying out separation removal to the phenols in coal tar, hydrogenated products deterioration is caused to be difficult to reach target level of product quality.
Therefore the separation for phenols in coal tar is particularly significant.
Utilization for coal tar pitch, due to the compositing characteristic and property of coal tar pitch, and the domestic application for coal tar pitch
Research gap compared with international is larger, and the domestic utilization for coal tar asphalt at present is relatively simple, while also generates
Environmental problem.Burning generation is carried out as directly the later coal tar heavy component (coal tar pitch) of distillation is mixed with light-weight fuel oil
Larger pollution, or it is relatively low to its utilization rate.
The processing method that patent 105316034A discloses carbolic oil in a kind of coal tar, mainly pass through the method for etherificate
Conversion coal tar has the aldehydes matter of kind containing phenol, and conversion ratio is limited and etherification reaction temperature is higher general all more than 220 DEG C, most
Height can reach 400 DEG C, will certainly increase conversion process energy consumption and separating step.
Patent CN105316018A discloses a kind of using centrifugation, gas back-flushing filtering, distillation, high voltage electric field pair
Coal tar carries out traditional processing after being pre-processed, and simply coal tar is improved in terms of pretreatment, and pretreatment process
Longer, the actual later separation processing substantially not to coal tar is improved, or entered with traditional processing method
The separation processing of row coal tar.
Patent CN103540352A discloses a kind of coal tar processing method for improving light liquids yield, although by slurry
Bed hydroprocessing processing, fixed bed hydrogenation handling process organic assembling, can be processed to full fraction of coal tar, improve coal tar
Utilization rate.But separating treatment, hydrogen when will certainly increase hydrogenation are not carried out to phenolic compound in cut fraction hydrogenation
Consumption, while can also influence the quality of light oil subsequently produced.
Patent CN105131999A discloses a kind of technique and device of single stove one-pot production modified coal tar pitch, and the technique passes through
Thermal cracking is mainly carried out to coal tar asphalt by reactor and heating furnace and thermal polymerization produces modified coal tar pitch, although can realize pair
The control of restructuring process, realize that production meets the modified coal tar pitch requirement of a certain index.But restructuring process reaction temperature needs to control
At 350-450 DEG C, reaction temperature is higher, and energy consumption is higher.
In summary, separation process complexity during traditional coal tar separation at present be present, separation process energy consumption is big, each group
Point separative efficiency is relatively low, separation process pollution is more serious, and pollution of the caused three wastes to environment is more serious.Simultaneously for mesh
Before have been enter into the part coal tar separation processing project of demonstration some major defects to be also more or less present urgently to be resolved hurrily.Therefore develop
The method of new efficient, economic, environmentally friendly separation processing coal tar, it has also become coal tar separates the important topic of application and development.
Utility model content
The problem of to overcome in currently available technology, the purpose of this utility model are to provide a kind of coal tar production modification drip
The device of blue or green, aliphatic hydrocarbon and aromatic hydrocarbon.
To achieve these goals, the technical solution adopted in the utility model is as follows：
The device of a kind of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon, including coal tar reactor, solvent orange 2 A return
Receive tower, modified coal tar pitch knockout drum, coal tar product component solvent dewaxing unit and fatty aromatic hydrocarbons and aromatic hydrocarbon process units；
Coal tar reactor bottom is connected with solvent orange 2 A recovery column overhead, and the tower reactor discharge pipe of solvent orange 2 A recovery tower is through coal
Tar reaction product extractive reaction kettle at the top of modified coal tar pitch knockout drum with being connected, modified coal tar pitch knockout drum bottom and coal tar oily product
Component solvent dewaxing device is connected, and coal tar product component solvent dewaxing unit is connected with fatty aromatic hydrocarbons and filled with aromatic hydrocarbon production
Put.
The utility model, which further improves, to be, the tower reactor discharge pipe of solvent orange 2 A recovery tower also with solvent orange 2 A recovery tower tower
Kettle reboiler entrance is connected, and the outlet of solvent orange 2 A recovery tower tower reactor reboiler is connected with solvent orange 2 A recovery tower bottom of towe；Coal tar reactor
Bottom is connected through solvent orange 2 A recovery tower feed pump, solvent orange 2 A recovery tower feed exchanger with solvent orange 2 A recovery column overhead.
The utility model, which further improves, to be, solvent orange 2 A recovery column overhead also enters with solvent orange 2 A recovery tower overhead condenser
Mouth is connected, and the outlet of solvent orange 2 A recovery tower overhead condenser is connected with solvent orange 2 A recovery column overhead knockout drum upper end, solvent orange 2 A recovery tower tower
Top knockout drum lower end is connected with solvent orange 2 A recovery tower overhead reflux pump intake, and solvent orange 2 A recovery tower tower backflow pump discharge is divided into two branch pipes
Road, a bye-pass are connected with solvent orange 2 A storage tank, and another bye-pass is connected with solvent orange 2 A recovery column overhead.
The utility model, which further improves, to be, tower reactor discharge pipe and the coal tar reaction product of solvent orange 2 A recovery tower
Desolventizing A coal tar product reservoir and desolventizing A coal tar oily product feed pumps are provided between extractive reaction kettle；Coal tar reacts
Solvent B storage tanks are also associated with the top of product extractive reaction kettle.
The utility model further improve is, coal tar product component solvent dewaxing unit include solvent B recovery towers,
Crystallizer and closed rotary drum vacuum filter；
The tower reactor discharge pipe of solvent B recovery towers is divided into two-way, all the way with solvent B recovery tower tower reactor reboiler entrance phases
Even, solvent B recovery towers tower reactor reboiler outlet is connected with solvent B recovery towers bottom, heat exchanger and knot before the crystallized device of another way
Brilliant device entrance is connected, and crystallizer outlet is connected with closed rotary drum vacuum filter entrance, closed rotary drum vacuum filter
It is connected at rotary drum scraper with paraffin storage tank, the distribution pipe of closed rotary drum vacuum filter fills with fatty aromatic hydrocarbons and aromatic hydrocarbon production
Put connected；Modified coal tar pitch knockout drum bottom is connected with solvent B recovery towers.
The utility model, which further improves, to be, the distribution pipe of closed rotary drum vacuum filter through the oil tank that dewaxes,
Dewaxed oil feed pump is connected with fatty aromatic hydrocarbons with aromatic hydrocarbon process units.
The utility model, which further improves, to be, vavuum pump is also associated with the top of the oil tank that dewaxes.
The utility model, which further improves, to be, fatty aromatic hydrocarbons includes solvent C recovery tower, extraction with aromatic hydrocarbon process units
Take rectifying column and extractant recovery tower；
The tower reactor discharge pipe of solvent C recovery tower is divided into two-way, all the way with solvent C recovery tower tower reactor reboiler entrance phase
Even, solvent C recovery tower tower reactor reboiler outlet is connected with solvent C recovery tower bottom of towe, and another way is connected with extractive distillation column；
The tower reactor discharge pipe of extractive distillation column is divided into two-way, is connected all the way with extractive distillation column tower reactor reboiler entrance,
The outlet of extractive distillation column tower reactor reboiler is connected with extractive distillation column bottom of towe；Another way is connected with extractant recovery tower, extractant
The tower reactor discharge pipe of recovery tower is divided into two-way, is connected all the way with extractant recovery tower tower reactor reboiler entrance, extractant recovery
The outlet of tower tower reactor reboiler is connected with extractant recovery tower bottom of towe, and another way is connected with extracting rectifying column overhead；Closed rotary drum
The distribution pipe of vacuum filter is connected with solvent C recovery tower.
The utility model, which further improves, to be, solvent C recovery column overhead and solvent C recovery tower overhead condenser entrance
It is connected, the outlet of solvent C recovery tower overhead condenser is connected with solvent C recovery tower return tank of top of the tower upper end, solvent C recovery column overhead
Return tank lower end is connected with solvent C recovery tower overhead reflux pump intake, and solvent C recovery tower overhead reflux pump discharge is divided into two branch pipes
Road, a bye-pass are connected with solvent C storage tank, and another bye-pass is connected with solvent C recovery column overhead；
The another way of the tower reactor discharge pipe of solvent C recovery tower is through desolventizing C coal tar product components storage tank, desolventizing C
Coal tar product component feed pump, extractive distillation column feed exchanger are connected with extractive distillation column.
The utility model, which further improves, to be, extracting rectifying column overhead is through extractive distillation column overhead condenser, extraction
Rectifying column top return tank is connected with extractive distillation column overhead reflux pump intake, and extractive distillation column tower backflow pump discharge is divided into two
Pipeline, a bye-pass are connected with extracting rectifying column overhead, and another bye-pass is connected with aliphatic hydrocarbon storage tank；
Extracting rectifying column overhead is through extractant recovery tower overhead condenser, extractant recovery tower return tank of top of the tower and extractant
Recovery tower overhead reflux pump intake is connected, and extractant recovery tower overhead reflux pump discharge is divided into two-way, is reclaimed all the way with extractant
Column overhead is connected, and another way is connected with aromatic hydrocarbon storage tank；
Extractant enters extracting rectifying column overhead and is also connected with extractant storage tank.
Compared with prior art, the utility model has the advantage that：
The utility model is by setting coal tar reactor, coal tar reaction product extractive reaction kettle, coal tar oily product group
Point solvent dewaxing unit and fatty aromatic hydrocarbons and aromatic hydrocarbon process units, using heterogeneous polymerization method, coal in the presence of solvent
Reacted under tar, aldehyde material and catalyst action, solvent in reactant is reclaimed after reaction, extracted by solvent
Take separation to can obtain modified coal tar pitch resin, realize the production of modified coal tar pitch；Pass through coal tar product component solvent dewaxing unit
Depitching coal tar product component is dewaxed, obtains dewaxed oil, dewaxed oil is filled by fatty aromatic hydrocarbons and aromatic hydrocarbon production
Put extracting rectifying and obtain aliphatic hydrocarbon and aromatic hydrocarbon.The utility model apparatus structure is simple, and can efficiently realize coal tar
Produce the purpose of modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon.
Further, crystallizer of the product after depitching through subsequently setting is realized de- with closed vacuum filter of changing shares
Wax, the separation for follow-up aromatic hydrocarbon and aliphatic hydrocarbon provide good condition.
Further, in order to maintain closed rotary drum vacuum filter that there is certain vacuum, so being stored up in dewaxed oil
Vavuum pump is provided with tank, to maintain certain vacuum to enable closed rotary drum vacuum filter continuous and steady operation.
The utility model utilizes heterogeneous polymerization method, and coal tar, aldehyde material and catalyst are made in the presence of solvent
Reacted under, solvent in reactant is reclaimed after reaction, modified coal tar pitch tree can obtain by solvent extraction and separation
Fat, solvent dewaxing is carried out after then reclaiming extractant to deasphalting coal tar product component, the product after dewaxing is carried out
Separation of extractive distillation obtains aliphatic hydrocarbon and aromatic hydrocarbon.Efficiently the phenols in coal tar is divided by the step of polymerisation one
From rationally making it by the use of reacted product, then process dewaxing, is later separation aromatic hydrocarbons and fat as the component of pitch modification
Fat hydrocarbon creates good separation condition.The property feature of the process makes full use coal tar each component reasonably utilizes separation side
Method, coal tar high-effective classifying sub-prime is utilized, and utilized for follow-up coal tar deep processing and established good basis, while work
Skill separating step is few, obvious energy conservation, being capable of economical and efficient repeated recycling utilize, operating condition temperature to the release agent in separation process
With, green, environmentally friendly, equipment investment is few, continuously-running is easily enlarged production scale, be coal tar separation processing
New method.
Brief description of the drawings
Fig. 1 is that coal tar of the present utility model produces modified coal tar pitch flow chart；
Fig. 2 is coal tar component solvent of the present utility model dewaxing flow chart；
Fig. 3 is that coal tar of the present utility model produces aromatic hydrocarbons and aliphatic hydrocarbon flow chart；
Fig. 4 is middle coalite tar heavy oil>The total ion chromatogram of 300 DEG C of cuts；
Fig. 5 is middle coalite tar heavy oil>The total ion chromatogram of 300 DEG C of cut depitching coal tar product components
(base catalysis)；
Coalite tar heavy oil in Fig. 6>The total ion current color of 300 DEG C of cut depitching coal tar product components (benzaldehyde)
Spectrogram (acid catalysis)；
In figure, 1, aldehyde material storage tank, 2, coal tar oil tank, 3, catalyst storage tank, 4, solvent orange 2 A storage tank, 5, coal tar it is anti-
Answer kettle, 6, solvent orange 2 A recovery tower feed pump, 7, solvent orange 2 A recovery tower feed exchanger, 8, solvent orange 2 A recovery tower, 9, solvent orange 2 A recovery tower
Overhead condenser, 10, solvent orange 2 A recovery column overhead knockout drum, 11, solvent orange 2 A recovery tower overhead reflux pump, 12, solvent orange 2 A recovery tower tower
Kettle reboiler, 13, desolventizing A coal tar product reservoirs, 14, desolventizing A coal tar oily product feed pumps, 15, solvent B storage tanks, 16,
Coal tar reaction product extractive reaction kettle, 17, modified coal tar pitch knockout drum, 18, modified coal tar pitch storage tank, 19, the production of depitching coal tar
Thing component feed pump, 20, solvent B recovery tower feed exchangers, 21, solvent B recovery towers, 22, solvent B recovery tower overhead condensations
Device, 23, solvent B recovery tower return tank of top of the tower, 24, solvent B recovery tower tower reflux pumps, 25, solvent B recovery tower tower reactor reboilers,
26th, desolventizing B coal tar product component storage tank, 27, desolventizing B coal tar product component feed pumps, 28, solvent C force (forcing) pump,
29th, solvent C storage tank, 30, heat exchanger before crystallizer, 31, crystallizer, 32, closed rotary drum vacuum filter, 33, paraffin storage tank,
34th, dewax oil tank, and 35, vavuum pump, 36, dewaxed oil feed pump, 37, solvent C recovery tower feed exchanger, 38, solvent C recovery
Tower, 39, solvent C recovery tower overhead condenser, 40, solvent C recovery tower return tank of top of the tower, 41, solvent C recovery tower overhead reflux
Pump, 42, solvent C recovery tower tower reactor reboiler, 43, desolventizing C coal tar product component storage tanks, 44, desolventizing C coal tar oily products
Component feed pump, 45, extractive distillation column feed exchanger, 46, extractive distillation column, 47, extractive distillation column overhead condenser, 48,
Extractive distillation column return tank of top of the tower, 49, extractive distillation column tower reflux pump, 50, aliphatic hydrocarbon storage tank, 51, extractive distillation column tower reactor again
Boil device, 52, extractant recovery tower, 53, extractant recovery tower overhead condenser, 54, extractant recovery tower return tank of top of the tower, 55,
Extractant recovery tower tower reflux pump, 56, aromatic hydrocarbon storage tank, 57, extractant recovery tower tower reactor reboiler, 58, extractant storage tank.
Embodiment
The utility model is described in further detail by embodiment below in conjunction with accompanying drawing.
Closed rotary drum vacuum filter 32 is on the basis of existing rotary drum vacuum filter in the utility model, is entered
Row improves, and makes enclosed construction, other structures are still identical with the structure of rotary drum vacuum filter in the prior art.
Certain temperature, certain reflux ratio etc. are arrived according to specific coal tar distillation according to heat exchange in the utility model
Point, solvent determine, how to determine be those skilled in the art common knowledge.
Referring to Fig. 1, Fig. 2 and Fig. 3, the device of a kind of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon includes：Aldehydes
Material storage tank 1, coal tar oil tank 2, catalyst storage tank 3, solvent orange 2 A storage tank 4, coal tar reactor 5, solvent orange 2 A recovery tower feed pump
6th, solvent orange 2 A recovery tower feed exchanger 7, solvent orange 2 A recovery tower 8, solvent orange 2 A recovery tower overhead condenser 9, solvent orange 2 A recovery column overhead
Knockout drum 10, solvent orange 2 A recovery tower overhead reflux pump 11, solvent orange 2 A recovery tower tower reactor reboiler 12, the storage of desolventizing A coal tars oily product
Tank 13, desolventizing A coal tar oily products feed pump 14, solvent B storage tanks 15, coal tar reaction product extractive reaction kettle 16, modification drip
Blue or green knockout drum 17, modified coal tar pitch storage tank 18, depitching coal tar product component feed pump 19, solvent B recovery tower feed exchangers
20th, solvent B recovery towers 21, solvent B recovery towers overhead condenser 22, solvent B recovery towers return tank of top of the tower 23, solvent B recovery towers
Tower reflux pump 24, solvent B recovery towers tower reactor reboiler 25, desolventizing B coal tar product components storage tank 26, desolventizing B coal tar
Heat exchanger 30 before product component feed pump 27, solvent C force (forcing) pump 28, solvent C storage tank 29, crystallizer, crystallizer 31, closed turn
Drum vacuum filter 32, paraffin storage tank 33, dewaxing oil tank 34, vavuum pump 35, dewaxed oil feed pump 36, solvent C recovery tower enter
Expect heat exchanger 37, solvent C recovery tower 38, solvent C recovery tower overhead condenser 39, solvent C recovery tower return tank of top of the tower 40, solvent
C recovery tower overhead refluxes pump 41, solvent C recovery tower tower reactor reboiler 42, desolventizing C coal tar product components storage tank 43, precipitation
Agent C coal tar product components feed pump 44, extractive distillation column feed exchanger 45, extractive distillation column 46, extracting rectifying column overhead
Condenser 47, extractive distillation column return tank of top of the tower 48, extractive distillation column tower reflux pump 49, aliphatic hydrocarbon storage tank 50, extractive distillation column
Tower reactor reboiler 51, extractant recovery tower 52, extractant recovery tower overhead condenser 53, extractant recovery tower return tank of top of the tower
54th, extractant recovery tower tower reflux pump 55, aromatic hydrocarbon storage tank 56, extractant recovery tower tower reactor reboiler 57 and extractant storage tank
58。
Referring to Fig. 1, the bottom of aldehyde material storage tank 1 is connected with the top of coal tar reactor 5；The bottom of coal tar oil tank 2 and coal
The top of tar reactor 5 is connected；The bottom of catalyst storage tank 3 is connected with the top of coal tar reactor 5；The bottom of solvent orange 2 A storage tank 4 and coal
The top of tar reactor 5 is connected；The bottom of coal tar reactor 5 is connected with the entrance of solvent orange 2 A recovery tower feed pump 6, solvent orange 2 A recovery
Tower feed pump 6 outlet is connected with the entrance of solvent orange 2 A recovery tower feed exchanger 7, solvent orange 2 A recovery tower feed exchanger 7 export with it is molten
The tower top of agent A recovery towers 8 is connected, and the tower top of solvent orange 2 A recovery tower 8 is also connected with the entrance of solvent orange 2 A recovery tower overhead condenser 9, solvent orange 2 A
Recovery tower overhead condenser 9 exports to be connected with the upper end of solvent orange 2 A recovery column overhead knockout drum 10, solvent orange 2 A recovery column overhead knockout drum
10 lower ends are connected with the entrance of solvent orange 2 A recovery tower overhead reflux pump 11, and the outlet of solvent orange 2 A recovery tower tower reflux pump 11 is divided into two branch pipes
Road, a bye-pass are connected with solvent orange 2 A storage tank 4, and another bye-pass is connected with the tower top of solvent orange 2 A recovery tower 8, the tower of solvent orange 2 A recovery tower 8
Kettle discharge pipe is divided into two-way, is connected all the way with the entrance of solvent orange 2 A recovery tower tower reactor reboiler 12, solvent orange 2 A recovery tower tower reactor is boiled again
The outlet of device 12 is connected with the bottom of towe of solvent orange 2 A recovery tower 8；Another way is connected with the entrance of desolventizing A coal tar product reservoir 13, desolventizing
The outlet of A coal tar product reservoir 13 is connected with the entrance of desolventizing A coal tar oily products feed pump 14, and desolventizing A coal tar oily products are entered
The outlet of material pump 14 is connected with the top of coal tar reaction product extractive reaction kettle 16；Produced with coal tar reaction the bottom of solvent B storage tanks 15
The top of thing extractive reaction kettle 16 is connected；The bottom of coal tar reaction product extractive reaction kettle 16 and the top phase of modified coal tar pitch knockout drum 17
Even, the bottom side of modified coal tar pitch knockout drum 17 is connected with modified coal tar pitch storage tank 18, opposite side and depitching coal tar product component
The entrance of feed pump 19 is connected, and the outlet of depitching coal tar product component feed pump 19 enters with solvent B recovery towers feed exchanger 20
Mouth is connected.
Referring to Fig. 2, coal tar product component solvent dewaxing unit includes solvent B recovery towers 21, crystallizer 31 and closing
Formula rotary drum vacuum filter 32；Specifically, the outlet of solvent B recovery towers feed exchanger 20 is connected with solvent B recovery towers 21, solvent
The tower top of B recovery towers 21 is connected with the entrance of solvent B recovery towers overhead condenser 22, solvent B recovery towers overhead condenser 22 outlet with
The upper end of solvent B recovery tower towers return tank 23 is connected, and the lower end of solvent B recovery towers return tank of top of the tower 23 is returned with solvent B recovery column overheads
The stream entrance of pump 24 is connected；The outlet of solvent B recovery tower towers reflux pump 24 is divided into two bye-passes, a bye-pass and the phase of solvent B storage tanks 15
Even, another bye-pass is connected with the tower top of solvent B recovery towers 21；The tower reactor discharge pipe of solvent B recovery towers 21 is divided into two-way, all the way
It is connected with the entrance of solvent B recovery towers tower reactor reboiler 25, the outlet of solvent B recovery towers tower reactor reboiler 25 and solvent B recovery towers 21
Bottom is connected, and another way enters through desolventizing B coal tar product components storage tank 26 and desolventizing B coal tar product components feed pump 27
Mouth is connected, and the outlet of desolventizing B coal tar product components feed pump 27 converges rear with being changed before crystallizer with the outlet of solvent C force (forcing) pump 28
The hot entrance of device 30 is connected；The entrance of solvent C force (forcing) pump 28 is connected with solvent C storage tank 29；The outlet of heat exchanger 30 and crystallization before crystallizer
The entrance of device 31 is connected；The outlet of crystallizer 31 is connected with the closed entrance of rotary drum vacuum filter 32, closed rotating drum vacuum filtration
It is connected at the rotary drum scraper of machine 32 with paraffin storage tank 33, distribution pipe and the dewaxing oil tank 34 of closed rotary drum vacuum filter 32
Top is connected, and the top of dewaxing oil tank 34 is also connected with the entrance of vavuum pump 35, the outlet of dewaxing oil tank 34 and dewaxed oil feed pump
36 entrances are connected.
Referring to Fig. 3, fatty aromatic hydrocarbons includes solvent C recovery tower 38, extractive distillation column 46 and extraction with aromatic hydrocarbon process units
Take agent recovery tower 52；Specifically, the outlet of dewaxed oil feed pump 36 is connected with the entrance of solvent C recovery tower feed exchanger 37, solvent C
The outlet of recovery tower feed exchanger 37 is connected with solvent C recovery tower 38；
The tower top of solvent C recovery tower 38 is connected with the entrance of solvent C recovery tower overhead condenser 39, and solvent C recovery column overhead is cold
The outlet of condenser 39 is connected with the upper end of solvent C recovery tower return tank of top of the tower 40, the lower end of solvent C recovery tower return tank of top of the tower 40 and solvent
The entrance of C recovery tower overhead refluxes pump 41 is connected, and the outlet of solvent C recovery tower overhead reflux pump 41 is divided into two bye-passes, a bye-pass
It is connected with solvent C storage tank 29, another bye-pass is connected with the tower top of solvent C recovery tower 38；The tower reactor discharge nozzle of solvent C recovery tower 38
Road is divided into two-way, is connected all the way with the entrance of solvent C recovery tower tower reactor reboiler 42, solvent C recovery tower tower reactor reboiler 42 exports
It is connected with the bottom of towe of solvent C recovery tower 38；Another way is connected with the entrance of desolventizing C coal tar product components storage tank 43, desolventizing C coals
The outlet of tar product component storage tank 43 is connected with the entrance of desolventizing C coal tar product components feed pump 44, the production of desolventizing C coal tar
The outlet of thing component feed pump 44 is connected with the entrance of extractive distillation column feed exchanger 45, and extractive distillation column feed exchanger 45 exports
It is connected with extractive distillation column 46；
The tower top of extractive distillation column 46 is connected with the entrance of extractive distillation column overhead condenser 47, extractive distillation column overhead condenser
47 outlets are connected with the upper end of extractive distillation column tower return tank 48, the lower end of extractive distillation column return tank of top of the tower 48 and extractive distillation column tower
The top entrance of reflux pump 49 is connected, and the outlet of extractive distillation column tower reflux pump 49 is divided into two bye-passes, a bye-pass and extractive distillation column
46 tower tops are connected, and another bye-pass is connected with aliphatic hydrocarbon storage tank 50；The tower reactor discharge pipe of extractive distillation column 46 is divided into two-way, and one
Road is connected with the entrance of extractive distillation column tower reactor reboiler 51, the outlet of extractive distillation column tower reactor reboiler 51 and the tower of extractive distillation column 46
Bottom is connected；Another way is connected with extractant recovery tower 52, the tower top of extractant recovery tower 52 and extractant recovery tower overhead condenser
53 entrances are connected, and the outlet of extractant recovery tower overhead condenser 53 is connected with the upper end of extractant recovery tower tower return tank 54, extracts
The lower end of agent recovery tower return tank of top of the tower 54 is connected with the entrance of extractant recovery tower overhead reflux pump 55, and extractant recovery column overhead is returned
The outlet of stream pump 55 is divided into two-way, is connected all the way with the tower top of extractant recovery tower 52, another way is connected with aromatic hydrocarbon storage tank 56；Extraction
The tower reactor discharge pipe of agent recovery tower 52 is divided into two-way, is connected all the way with the entrance of extractant recovery tower tower reactor reboiler 57, extraction
The outlet of agent recovery tower tower reactor reboiler 57 is connected with the bottom of towe of extractant recovery tower 52, another way and the tower top phase of extractive distillation column 46
Even；The lower end of extractant storage tank 58 is entered the tower top pipe of extractive distillation column 46 with extractant and is connected.
The technique of coal tar modified coal tar pitch of the present utility model, aliphatic hydrocarbon and aromatic hydrocarbon comprises the following steps：
(1) Production Process for Modified Pitch flow：
Respectively by the aldehyde material in aldehyde material storage tank 1, the coal tar in coal tar oil tank 2, catalyst storage tank 3
Reacted in the coal tar reactor 5 that solvent orange 2 A in catalyst, solvent orange 2 A storage tank 4 is added continuously to continuously stir, control coal
The temperature of tar reactor 5 is at 40~180 DEG C and reacts 1.5~6h, obtains coal tar reaction product.By coal tar reaction product
After the pressurization of solvent orange 2 A recovery tower feed pump 6 solvent orange 2 A recovery tower feed exchanger 7 is sent into be exchanged heat, heat exchange to certain temperature with
Enter solvent orange 2 A recovery tower 8 afterwards and carry out rectifying separation, obtain a small amount of water, solvent orange 2 A and coal tar oily product.The tower top of solvent orange 2 A recovery tower 8
Solvent orange 2 A and a small amount of water are produced, solvent orange 2 A is returned in solvent orange 2 A storage tank 4, completes recycling design A.The tower reactor of solvent orange 2 A recovery tower 8 obtains
To desolventizing A coal tar reaction product, it is stored in desolventizing A coal tar product reservoir 13；
Specifically, solvent orange 2 A reclaims column overhead upflowing vapor enters solvent orange 2 A after the condensation of solvent orange 2 A recovery tower overhead condenser 9
Column overhead knockout drum 10 is reclaimed, after knockout drum separates, obtained solvent orange 2 A is through solvent orange 2 A recovery tower overhead reflux pump 11 by certain
A reflux ratio part be sent into solvent orange 2 A recovery tower top, a part returns to solvent orange 2 A storage tank 4.The tower reactor output of solvent orange 2 A recovery tower 8 takes off
A coal tar reaction product part for solvent orange 2 A gasifies to solvent orange 2 A recovery tower after the heating of solvent orange 2 A recovery tower tower reactor reboiler 12
It is interior, it is partly into desolventizing A coal tar product reservoir 13 and stores.
Then the desolventizing A coal tars oily product in desolventizing A coal tar product reservoir 13 is entered through desolventizing A coal tar oily products
It is continuous to expect that the pressurization of pump 14 is carried out after entering in coal tar reaction product extractive reaction kettle 16 with the solvent B from solvent B storage tanks 15
Heating, stirring, extraction, obtain extracting mixture after certain residence time, extraction mixture is sent into modified coal tar pitch point
From tank 17, depitching coal tar product component and modified pitch are obtained after sedimentation separation, obtained modified coal tar pitch is stored
In modified pitch storage tank 18.
(2) coal tar product component solvent dewaxing process flow：
Depitching coal tar product component is fed through depitching coal tar product component feed pump 19, solvent B recovery towers
Heat exchanger 20 enters solvent B recovery towers 21 after exchanging heat to certain temperature, after solvent B recovery towers change 21 thermal rectifications separation, obtains
Solvent B and desolventizing B coal tar product components.Specifically, the tower top upflowing vapor of solvent B recovery towers 21 is through solvent B recovery tower towers
Top condenser 22 enters solvent orange 2 A recovery tower return tank of top of the tower 23 after condensing, and then presses one through solvent B recovery tower overhead refluxes pump 24
A fixed reflux ratio part is sent into the tower top of solvent B recovery towers 21, and a part returns to solvent B storage tanks 15, completes solvent B and returns
Receive.The tower reactor output desolventizing B of a solvent B recovery towers 21 coal tar reaction product part is through solvent B recovery tower tower reactor reboilers
After 25 heating in gasification to solvent B recovery towers, it is partly into desolventizing B coal tar product components storage tank 26 and stores.
Then by the desolventizing B coal tar product components of storage in desolventizing B coal tar product components storage tank 26 through precipitation
Agent B coal tar product components feed pump 27 is changed with solvent C through heat exchanger 30 before being sent into crystallizer together with solvent C force (forcing) pump 28
Heat, crystallizer 31 is entered after exchanging heat to certain temperature and carries out Crystallization Separation, the mixture after the completion of crystallization enters closed rotary drum
Filtered in vacuum filter 32, obtain paraffin and dewaxed oil, paraffin is stored in paraffin storage tank, dewaxed oil is stored in dewaxed oil
Storage tank；Specifically, the slurry vessel that the mixture after the completion of crystallization enters closed rotary drum vacuum filter 32 carries out filter operation,
Then the fillter section through rotary drum filters to feed liquid, and filtrate enters filter chamber through the filter cloth on rotary drum, by filter chamber distribution pipe
Into in dewaxing oil tank 34, filter cake reaches scraper and goes out to be scraped into paraffin storage tank 33, in order to maintain closed rotary drum true
Empty filter 32 has certain vacuum, so vavuum pump 35 is provided with dewaxing oil tank 34, to maintain necessarily true
Reciprocal of duty cycle enables the closed continuous and steady operation of rotary drum vacuum filter 32；Then the dewaxed oil of storage is sent into solvent C recovery
Tower 38.
(3) fatty aromatic hydrocarbons and the aromatic hydrocarbon technological process of production：
From dewaxing oil tank 34 through the dewaxed oil that dewaxed oil feed pump 36 is sent through solvent C recovery tower feed exchanger 37
Exchange heat to after certain temperature, carry out rectifying separation into solvent C recovery tower 38, obtain solvent C and desolventizing C coal tar oily products
Component；Specifically, the tower top upflowing vapor of solvent C recovery tower 38 enters solvent C after the condensation of solvent C recovery tower overhead condenser 39
Recovery tower return tank of top of the tower 40, then it is sent into solvent C by certain reflux ratio part through solvent C recovery tower overhead reflux pump 41
Tower top is reclaimed, a part returns to solvent C storage tank 29, completes the recovery of solvent C.The tower reactor output desolventizing C of solvent C recovery tower 38
A coal tar reaction product component part after the heating of solvent C recovery tower tower reactor reboiler 42 gasification to solvent C recovery tower 38
It is interior, it is partly into desolventizing C coal tar product components storage tank 43 and stores.
Desolventizing C coal tar product component enters extraction essence after the pressurization of desolventizing C coal tar product components feed pump 44
Evaporate tower feed exchanger 45 to be exchanged heat, extractive distillation column 46 is entered after exchanging heat to certain temperature, and and by extractive distillation column 46
The extractant that tower top part adds carries out separation of extractive distillation together, obtains the mixture and aliphatic hydrocarbon of extractant and aromatic hydrocarbon,
By the isolated extractant of the mixture rectifying of extractant and aromatic hydrocarbon and aromatic hydrocarbon.Specifically, on the tower top of extractive distillation column 46
Rise steam and enter extractive distillation column return tank of top of the tower 48 after the condensation of extractive distillation column overhead condenser 47, then through extracting rectifying
Tower tower reflux pump 49 is sent into extracting rectifying column overhead 46 by certain reflux ratio part, and a part is fed through aliphatic hydrocarbon storage tank 50
In.A mixture part for the tower reactor output extractant of extractive distillation column 46 and aromatic hydrocarbon adds through extractive distillation column tower reactor reboiler 51
After heat in gasification to extractive distillation column 46, it is partly into extractant recovery tower 52.
The tower top upflowing vapor of extractant recovery tower 52 enters extractant after the condensation of extractant recovery tower overhead condenser 53
Recovery tower return tank of top of the tower 54, then it is sent into extractant by certain reflux ratio part through extractant recovery tower tower reflux pump 55
The tower top of recovery tower 52, a part are fed through in aromatic hydrocarbon storage tank 56.The tower reactor output extractant of extractant recovery tower 52 part warp
After extractant recovery tower tower reactor reboiler 57 heats in gasification to the tower of extractant recovery tower 52, extractive distillation column 46 is partly into
Tower top, it can be supplemented in extractant deficiency by the extractant in extractant storage tank 58.
The mass ratio of the coal tar and aldehyde material, solvent orange 2 A and catalyst is 1：(0.9~1.2)：(1~10)：
(0.03~0.2)；
The coal tar is the distillation fraction of middle coalite tar or middle coalite tar；
The aldehyde material is formaldehyde, furfural, benzaldehyde or paraformaldehyde；
The catalyst is the mixture of sulfuric acid, oxalic acid, benzene sulfonic acid, any one or two kinds in hydrochloric acid, or catalyst
For any one in sodium hydroxide, potassium hydroxide or two kinds of mixture；
The solvent orange 2 A is the mixture that solvent is any one or two kinds in benzene, toluene, ortho-xylene；
The solvent B is one or more of mixtures in C5~C8 alkane；Wherein C5~C8 alkane is included just
Structure alkane or branched paraffin；Desolventizing A coal tars oily product is 1 with solvent B mass ratioes:(1~20)；
The solvent C is one or both of MEK, acetone；Desolventizing B coal tars oily product is with solvent C mass ratio
1:(4~6)；
The extractant is DMF (DMF), N- N-formyl morpholine Ns, Ν-methyl pyrrolidone (NMP)
Or sulfolane；
Content of the present utility model is furtherd elucidate with reference to embodiment.
Experimental raw is to be derived from the coal tar of semi-coke factory of northern Shensi Fugu County, light oil (coal tar depositing reservoir layer waterborne) heavy oil
The fundamental property that (tar depositing reservoir subsurface layer oil) is determined by national standard is shown in Table 1.
The fundamental property of the coal tar heavy oil of table 1
Note：﹡ minusings
Using the method for heterogeneous polymerization, using benzene or toluene as solvent, in utilization in coalite tar or its cut
Phenols, aldehyde material and catalyst are added, carry out phenolic aldehyde polymerization, solvent extraction and separation is carried out to reaction product after reaction, can be with
Modified pitch and depitching coal tar product component are obtained, then carrying out solvent respectively to depitching coal tar product component takes off
Wax, extracting rectifying can obtain aliphatic hydrocarbon and aromatic hydrocarbon.In order to illustrate utility model actual effect, using gas chromatography-mass spectrum
Combined instrument centering coalite tar and depitching coal tar product component have carried out composition measuring.
Embodiment 1
Coalite tar heavy oil in selection>300 DEG C and formalin (37wt%) are reactant, and toluene is solvent, NaOH
(40wt%) is catalyst, wherein, coalite tar heavy oil>300 DEG C distillation part and the mass ratio of formaldehyde are 1:1.17 low temperature
Coal tar heavy oil>300 DEG C distillation part and the mass ratio of solvent are 1:5, coalite tar heavy oil>300 DEG C distillation part is with urging
The mass ratio of agent is 1:0.17, it is 40~90 DEG C to control the interior reaction temperature of coal tar reactor 5, and the reaction time is 1.5~2h.
After above-mentioned flow is carried out, using gas chromatograph-mass spectrometer (GC-MS) to product (predominantly depitching coal tar product component)
Composition analysis is carried out, is shown in Table 2.
Coalite tar heavy oil in table 2>300 DEG C of cuts and its depitching coal tar product component (base catalysis) constituent part
Table
Found with reference to the result of Fig. 4, Fig. 5 and table 2, middle coalite tar heavy oil>After 300 DEG C of cuts react with formaldehyde,
Without discovery phenolic compound in depitching coal tar product component.This shows, can by so simple phenolic aldehyde polymerisation
With coalite tar heavy oil in removing>Phenolic compound in 300 DEG C of cuts, make phenolic compound and aldehyde material in coal tar
Pitch is modified by being reacted into modified pitch component, and can be to heavy oil>300 DEG C of cuts play the work of separation
With.
Embodiment 2
Low temperature coal tar heavy oil in selection>300 DEG C of cuts and benzaldehyde are reactant, and toluene is solvent, and p-methyl benzenesulfonic acid is
Catalyst, reaction temperature are controlled at 140~180 DEG C, middle low temperature coal tar heavy oil>The mass ratio of 300 DEG C of cuts and benzaldehyde is 1:
1.15, middle low temperature coal tar heavy oil>The mass ratio of 300 DEG C of cuts and solvent is 1:12, middle low temperature coal tar heavy oil>300 DEG C of cuts with
The mass ratio of catalyst is 1:0.1, reaction temperature is controlled at 140~180 DEG C, and the reaction time is 4~6h.Above-mentioned flow has been carried out
Bi Hou, composition analysis is carried out to product (predominantly dephenolize oil) using gas chromatograph-mass spectrometer (GC-MS).Carry out above-mentioned flow.Enter
After row, primary product component (depitching coal tar product component) is formed using gas chromatograph-mass spectrometer (GC-MS)
Analysis, is shown in Table 3.
Coalite tar heavy oil in table 3>300 DEG C of cut depitching coal tar product component (benzaldehyde, acid catalysis) parts
Component table
Found with reference to Fig. 4 and Fig. 6, table 2 and table 3 result, middle coalite tar heavy oil>300 DEG C of cuts and benzaldehyde are anti-
Ying Hou, without discovery phenolic compound in depitching coal tar product component.This shows, is polymerize by so simple phenolic aldehyde
Coalite tar heavy oil during reaction can remove>Phenolic compound in 300 DEG C of cuts, make phenolic compound and aldehyde in coal tar
Class material is modified by being reacted into modified pitch component to pitch, and can be to heavy oil>300 DEG C of cuts play point
From effect.Table 4 gives the asphalt performance change before and after modified pitch simultaneously, and three of pitch after being modified are found by contrast
Big index (needle penetration, softening point, ductility) is compared to make moderate progress before modified.
Index contrasts before and after the asphalt modification of table 4
The utility model utilizes heterogeneous polymerization method, and under solvent, catalyst action, coal tar is carried out with aldehyde material
Reaction, reclaims to solvent in reaction product after reaction, modified coal tar pitch is obtained by solvent extraction and separation, to deasphalting coal
Tar reaction product carries out solvent recovery, then carries out solvent dewaxing, and carrying out separation of extractive distillation to the product after dewaxing obtains
Aliphatic hydrocarbon and aromatic hydrocarbon.Efficiently the phenols in coal tar is removed by the step of polymerisation one, after rationally utilizing reaction
Product make its component as pitch modification, then by solvent dewaxing, be later separation aromatic hydrocarbons and aliphatic hydrocarbon create it is good
Separation condition.The property feature of the process makes full use coal tar each component reasonably utilizes separation method, obtains coal tar
Utilized with high-effective classifying sub-prime, and utilized for follow-up coal tar deep processing and established good basis, while separating step is few, energy-conservation
Significantly, it is gentle to release agent economical and efficient repeated recycling utilize, the operating condition in separation process, green, friendly to environment
Well, equipment investment is few, continuously-running is easily enlarged production scale, is the new method of coal tar separation processing.
Claims (10)
1. the device of a kind of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon, it is characterised in that including coal tar reactor
(5), solvent orange 2 A recovery tower (8), modified coal tar pitch knockout drum (17), coal tar product component solvent dewaxing unit and fatty aromatic hydrocarbons
With aromatic hydrocarbon process units；
Coal tar reactor (5) bottom is connected with solvent orange 2 A recovery tower (8) tower top, the tower reactor discharge nozzle of solvent orange 2 A recovery tower (8)
Road is connected through coal tar reaction product extractive reaction kettle (16) with modified coal tar pitch knockout drum (17) top, modified coal tar pitch knockout drum
(17) bottom is connected with coal tar product component solvent dewaxing unit, and coal tar product component solvent dewaxing unit is connected with fat
Aromatic hydrocarbons and aromatic hydrocarbon process units.
2. the device of a kind of coal tar production modified coal tar pitch according to claim 1, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In the tower reactor discharge pipe of solvent orange 2 A recovery tower (8) is also connected with solvent orange 2 A recovery tower tower reactor reboiler (12) entrance, and solvent orange 2 A returns
Tower tower reactor reboiler (12) outlet is received with solvent orange 2 A recovery tower (8) bottom of towe to be connected；Reclaimed through solvent orange 2 A coal tar reactor (5) bottom
Tower feed pump (6), solvent orange 2 A recovery tower feed exchanger (7) are connected with solvent orange 2 A recovery tower (8) tower top.
3. the device of a kind of coal tar production modified coal tar pitch according to claim 1, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In solvent orange 2 A recovery tower (8) tower top is also connected with solvent orange 2 A recovery tower overhead condenser (9) entrance, solvent orange 2 A recovery tower overhead condensation
Device (9) export with solvent orange 2 A recovery column overhead knockout drum (10) upper end is connected, solvent orange 2 A recovery column overhead knockout drum (10) lower end and
Solvent orange 2 A recovery tower overhead reflux pump (11) entrance is connected, and solvent orange 2 A recovery tower tower reflux pump (11), which exports, is divided into two bye-passes, and one
Bye-pass is connected with solvent orange 2 A storage tank (4), and another bye-pass is connected with solvent orange 2 A recovery tower (8) tower top.
4. the device of a kind of coal tar production modified coal tar pitch according to claim 1, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In being provided with desolventizing between the tower reactor discharge pipe and coal tar reaction product extractive reaction kettle (16) of solvent orange 2 A recovery tower (8)
A coal tar product reservoir (13) and desolventizing A coal tar oily product feed pumps (14)；Coal tar reaction product extractive reaction kettle (16)
Top is also associated with solvent B storage tanks (15).
5. the device of a kind of coal tar production modified coal tar pitch according to claim 1, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In coal tar product component solvent dewaxing unit includes solvent B recovery towers (21), crystallizer (31) and closed rotary-drum vacuum
Filter (32)；
The tower reactor discharge pipe of solvent B recovery towers (21) is divided into two-way, all the way with solvent B recovery towers tower reactor reboiler (25) entrance
It is connected, solvent B recovery towers tower reactor reboiler (25) outlet is connected with solvent B recovery towers (21) bottom, before the crystallized device of another way
Heat exchanger (30) is connected with crystallizer (31) entrance, crystallizer (31) outlet and closed rotary drum vacuum filter (32) entrance phase
Even, it is connected at the rotary drum scraper of closed rotary drum vacuum filter (32) with paraffin storage tank (33), closed rotating drum vacuum filtration
The distribution pipe of machine (32) is connected with fatty aromatic hydrocarbons with aromatic hydrocarbon process units；Modified coal tar pitch knockout drum (17) bottom is returned with solvent B
Tower (21) is received to be connected.
6. the device of a kind of coal tar production modified coal tar pitch according to claim 5, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In the distribution pipe of closed rotary drum vacuum filter (32) is through the oil tank (34) that dewaxes, dewaxed oil feed pump (36) and fat virtue
Hydrocarbon is connected with aromatic hydrocarbon process units.
7. the device of a kind of coal tar production modified coal tar pitch according to claim 6, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In being also associated with vavuum pump (35) at the top of dewaxing oil tank (34).
8. the device of a kind of coal tar production modified coal tar pitch according to claim 5, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In fatty aromatic hydrocarbons includes solvent C recovery tower (38), extractive distillation column (46) and extractant recovery tower with aromatic hydrocarbon process units
(52)；
The tower reactor discharge pipe of solvent C recovery tower (38) is divided into two-way, all the way with solvent C recovery tower tower reactor reboiler (42) entrance
It is connected, solvent C recovery tower tower reactor reboiler (42) outlet is connected with solvent C recovery tower (38) bottom of towe, another way and extracting rectifying
Tower (46) is connected；
The tower reactor discharge pipe of extractive distillation column (46) is divided into two-way, all the way with extractive distillation column tower reactor reboiler (51) entrance phase
Even, extractive distillation column tower reactor reboiler (51) outlet is connected with extractive distillation column (46) bottom of towe；Another way and extractant recovery tower
(52) be connected, the tower reactor discharge pipe of extractant recovery tower (52) is divided into two-way, all the way with extractant recovery tower tower reactor reboiler
(57) entrance is connected, and extractant recovery tower tower reactor reboiler (57) outlet is connected with extractant recovery tower (52) bottom of towe, another way
It is connected with extractive distillation column (46) tower top；The distribution pipe of closed rotary drum vacuum filter (32) and solvent C recovery tower (38) phase
Even.
9. the device of a kind of coal tar production modified coal tar pitch according to claim 8, aliphatic hydrocarbon and aromatic hydrocarbon, its feature exist
In solvent C recovery tower (38) tower top is connected with solvent C recovery tower overhead condenser (39) entrance, solvent C recovery tower overhead condensation
Device (39) outlet is connected with solvent C recovery tower return tank of top of the tower (40) upper end, solvent C recovery tower return tank of top of the tower (40) lower end and
Solvent C recovery tower overhead reflux pump (41) entrance is connected, and solvent C recovery tower overhead reflux pump (41) outlet is divided into two bye-passes,
One bye-pass is connected with solvent C storage tank (29), and another bye-pass is connected with solvent C recovery tower (38) tower top；
The another way of the tower reactor discharge pipe of solvent C recovery tower (38) is through desolventizing C coal tar product component storage tanks (43), precipitation
Agent C coal tar product component feed pumps (44), extractive distillation column feed exchanger (45) are connected with extractive distillation column (46).
10. the device of a kind of coal tar production modified coal tar pitch according to claim 9, aliphatic hydrocarbon and aromatic hydrocarbon, its feature
Be, extractive distillation column (46) tower top through extractive distillation column overhead condenser (47), extractive distillation column return tank of top of the tower (48) with
Extractive distillation column overhead reflux pump (49) entrance is connected, and extractive distillation column tower reflux pump (49), which exports, is divided into two bye-passes, one
Pipeline is connected with extractive distillation column (46) tower top, and another bye-pass is connected with aliphatic hydrocarbon storage tank (50)；
Extractant recovery tower (52) tower top is through extractant recovery tower overhead condenser (53), extractant recovery tower return tank of top of the tower
(54) it is connected with extractant recovery tower overhead reflux pump (55) entrance, extractant recovery tower overhead reflux pump (55) outlet is divided into two
Road, it is connected all the way with extractant recovery tower (52) tower top, another way is connected with aromatic hydrocarbon storage tank (56)；
Extractant enters extractive distillation column (46) tower top and is also connected with extractant storage tank (58).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108384567A (en) * | 2018-05-07 | 2018-08-10 | 西北大学 | A kind of coal tar component separating device and technique |
| CN114540065A (en) * | 2022-02-18 | 2022-05-27 | 山东大学 | Method for extracting asphalt soluble substance by adopting o-xylene and water |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108384567A (en) * | 2018-05-07 | 2018-08-10 | 西北大学 | A kind of coal tar component separating device and technique |
| CN108384567B (en) * | 2018-05-07 | 2024-01-16 | 西北大学 | Coal tar component separation device and process |
| CN114540065A (en) * | 2022-02-18 | 2022-05-27 | 山东大学 | Method for extracting asphalt soluble substance by adopting o-xylene and water |
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