CN209508153U - Distillation produces various asphalt Product Process device in conjunction with extraction phase - Google Patents
Distillation produces various asphalt Product Process device in conjunction with extraction phase Download PDFInfo
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- CN209508153U CN209508153U CN201822190713.5U CN201822190713U CN209508153U CN 209508153 U CN209508153 U CN 209508153U CN 201822190713 U CN201822190713 U CN 201822190713U CN 209508153 U CN209508153 U CN 209508153U
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- extraction
- heating furnace
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- 238000000605 extraction Methods 0.000 title claims abstract description 102
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000010426 asphalt Substances 0.000 title claims abstract description 27
- 238000004821 distillation Methods 0.000 title claims abstract description 27
- 239000011295 pitch Substances 0.000 claims abstract description 64
- 238000012986 modification Methods 0.000 claims abstract description 39
- 230000004048 modification Effects 0.000 claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 claims abstract description 25
- 239000011338 soft pitch Substances 0.000 claims abstract description 23
- 239000011294 coal tar pitch Substances 0.000 claims abstract description 22
- 239000011269 tar Substances 0.000 claims abstract description 21
- 239000011305 binder pitch Substances 0.000 claims abstract description 12
- 238000002407 reforming Methods 0.000 claims abstract description 11
- 238000010438 heat treatment Methods 0.000 claims description 71
- 239000000203 mixture Substances 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 15
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 14
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 claims description 14
- 239000012046 mixed solvent Substances 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000000638 solvent extraction Methods 0.000 claims description 4
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 abstract description 14
- 239000011280 coal tar Substances 0.000 abstract description 14
- 239000002994 raw material Substances 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 description 13
- 238000001816 cooling Methods 0.000 description 6
- 238000004939 coking Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 238000005292 vacuum distillation Methods 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000011230 binding agent Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000895 extractive distillation Methods 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 238000011112 process operation Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000007772 electrode material Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Working-Up Tar And Pitch (AREA)
Abstract
The utility model relates to distill to produce various asphalt Product Process device in conjunction with extraction phase, including dehydrating tower, Distallation systm, extracting system and pitch reforming system, using coal tar as raw material, using distillation, extraction combines joint production process production soft pitch with pitch modification, mid temperature pitch, modified coal tar pitch, low quinoline insolubles refined bitumen, impregnating pitch, pitch, the products such as binder pitch, the asphaltic products for producing a variety of high added values simultaneously with a set of process units can be achieved, the utilization rate of device is improved to the maximum extent, adapt to the demand of extensive tar production.
Description
Technical field
The utility model relates to metallurgical coking industry coal tar processing technical field, more particularly to a kind of distillation with
Extraction phase combines production various asphalt Product Process device.
Background technique
In recent years, with the development of coking industry, tar production increasingly tends to centralization, large-scale, fine separation
Developing with deep processing direction, coal tar pitch is the bulk product that coal tar processing is isolated in the process, account for about the 50-60% of tar,
A kind of important industrial chemicals, electrode material, refractory material, carbon industry, build the road, the industries such as building materials suffer from widely
Using.
Currently, the asphaltic products of existing tar production production mainly have soft pitch, mid temperature pitch and modified coal tar pitch, phase
The production technology answered is as follows:
1) soft pitch production technology
Soft pitch softening point is 40-60 DEG C, different by softening point, can be a carbolineum fraction that coal tar isolates,
The mixture of anthracene oil fraction, mid temperature pitch is also possible to the mixture of anthracene oil fraction and mid temperature pitch.Production low temperature at present
There are mainly three types of the methods of pitch, the first is a carbolineum, anthracene oil and mid temperature pitch point in normal pressure coal tar distillation technique
It does not produce, then a set of oil product preparation facility is set, prepare production soft pitch with carbolineum and mid temperature pitch；Second is to depressurize
In coal tar distillation technique, by adjusting process operation parameter, soft pitch is directly produced in king-tower tower bottom；The third is normal
It depressurizes in coal tar distillation technique, by adjusting process operation parameter, produces soft pitch in vacuum tower tower bottom.
2) mid temperature pitch production technology
Mid temperature pitch softening point is 75-95 DEG C, and producing mid temperature pitch at present, there are mainly three types of techniques, first is that normal pressure coal tar
Distillation technique produces mid temperature pitch at flash evaporator bottom；Second is that decompression coal tar distillation technique, produces medium temperature in king-tower tower bottom
Pitch；Third is that Atmospheric vacuum coal tar distillation technique, can produce mid temperature pitch in vacuum tower tower bottom.
3) Production Process for Modified Pitch
The softening point of modified coal tar pitch is 105-120 DEG C, the content 26-34% of toluene insolubles, the content of quinoline insolubles
For 6-15%.The method of production modified coal tar pitch at present, the mid temperature pitch mainly obtained using coal tar distillation is raw material, using heat
Condensation methods produce modified coal tar pitch, and thermal polycondensation process can be divided into autoclave heating and diamond heating method by heating method again.
In conclusion asphalt product less varieties, added value is not high, and a set of life at present in tar production production technology
A kind of asphaltic products can only generally be produced by producing device, not adapt to the demand in the market to various asphalt product.
Utility model content
To overcome prior art defect, the technical issues of the utility model solves, is to provide a kind of distillation in conjunction with extraction phase
Various asphalt Product Process device is produced, using coal tar as raw material, joint production process is combined with pitch modification using distillation, extraction
Produce soft pitch, mid temperature pitch, modified coal tar pitch, low quinoline insolubles refined bitumen, impregnating pitch, pitch, binder drip
The products such as blueness, it can be achieved that produce the asphaltic products of a variety of high added values with a set of process units simultaneously, and raising fills to the maximum extent
The utilization rate set adapts to the demand of extensive tar production.
In order to achieve the above object, the utility model is implemented with the following technical solutions:
Distillation produces various asphalt Product Process device, including dehydrating tower, Distallation systm, extracting system in conjunction with extraction phase
With pitch reforming system, which is characterized in that the dehydrating tower is equipped with tar entrance, and water/light oil produces mouth, boiled tar extraction
Mouthful；
The Distallation systm is by 1#Heating furnace, 1#Destilling tower, 2#Heating furnace and 2#Destilling tower composition, wherein 1#Destilling tower and 1#
Heating furnace connection, tower top are equipped with carbolic oil and produce mouth, and side line is equipped with naphtalene oil extraction mouth and washing oil produces mouth, and tower bottom is equipped with four road low temperature
Pitch produces mouth, is recycled back to 1 after merging all the way with boiled tar extraction mouth#Heating furnace goes storage facility or export trade, all the way all the way
Go 2#Heating furnace removes extracting system all the way；2#Destilling tower and 2#Heating furnace connection, tower top are equipped with carbolineum and produce mouth, and side line is equipped with two
Carbolineum produces mouth, and tower bottom is equipped with three road mid temperature pitches and produces mouth, is recycled back to 2 after merging all the way with soft pitch extraction mouth#Heating
Furnace goes storage facility or export trade, all the way deasphalting reforming system all the way；
The extracting system is steamed by extraction settlement separator, light phase heating furnace, light phase destilling tower, heavy phase heating furnace and heavy phase
Tower composition is evaporated, wherein extraction settlement separator is connect with soft pitch extraction mouth, light phase extraction mouth is equipped with and heavy phase produces mouth；Gently
Phase destilling tower is connect with light phase heating furnace, and tower top is equipped with mixed solvent and produces mouth, and side line is equipped with changeable carbolineum and produces mouth, tower
Bottom is equipped with two-way refined bitumen and produces mouth, is recycled back to light phase heating furnace after merging all the way with light phase extraction mouth, goes storage to set all the way
It applies or export trade；Heavy phase destilling tower is connect with heavy phase heating furnace, and tower top is equipped with mixed solvent extraction mouth and light phase overhead
Mixed solvent extraction mouth removes extraction settlement separator after merging, side line is equipped with carbolineum and produces mouth, and tower bottom is dripped equipped with three road binders
Blueness extraction mouth is recycled back to heavy phase heating furnace, goes storage facility or export trade all the way, goes to drip all the way after merging all the way with heavy phase extraction mouth
Green reforming system；
The pitch reforming system is made of modification heater and modification kettle, wherein modification kettle is connect with modification heater,
Kettle top is equipped with flash oil and produces mouth, and bottom is equipped with two-way modified coal tar pitch and produces mouth, produces mouth/binder drip with mid temperature pitch all the way
Blueness extraction mouth is recycled back to modification heating furnace after merging, and goes storage facility or export trade all the way.
When the light phase destilling tower side line carbolineum adopts port opening and cuts carbolineum, tower bottom obtains impregnating pitch product, otherwise
Obtain refined bitumen product.
The modification kettle bottom modified coal tar pitch extraction mouth and mid temperature pitch extraction mouth are recycled back to modification heating furnace after merging, and obtain
To modified coal tar pitch product, pitch product is otherwise obtained.
Distillation produces various asphalt Product Process in conjunction with extraction phase, includes the following steps:
1) feedstock processing
Water content is 1%-3%, 80-90 DEG C of temperature of coal tar after exchanging heat with fraction and being preheating to 130-140 DEG C by
Tar entrance enters dehydrating tower removing moisture, overhead extraction light oil distillate, and tower bottom extraction boiled tar enters Distallation systm；
Dehydrating tower operates in atmospheric conditions, 101~107kPa of absolute pressure of top of the tower, and 95~120 DEG C of tower top temperature, tower bottom
180~210 DEG C of temperature；
2) air-distillation
By dehydrating tower Lai boiled tar and 1#The circulation soft pitch that destilling tower comes is mixed into 1#Heating furnace is heated to
Enter 1 after 350~390 DEG C#Destilling tower, through air-distillation separation, (tower top pressure is controlled in 101~107kPa of absolute pressure, tower
Push up 170~185 DEG C of temperature), overhead extraction carbolic oil, side line produces naphtalene oil (210~240 DEG C of temperature of extraction) respectively and washing oil (is adopted
260~280 DEG C of temperature out), carbolic oil, naphtalene oil and washing oil fraction are sent into subsequent production unit or export trade after heat exchange and cooling；Tower
Bottom produces soft pitch (about 330~360 DEG C of temperature of extraction, softening point are 40~60 DEG C), and there are three whereabouts altogether, first is that directly making
For international sale, second is that going 2#Destilling tower produces mid temperature pitch, third is that extracting system is gone to produce other asphaltic products；
3) secondary pressure is distilled
1#The soft pitch and 2 that destilling tower comes#The circulation mid temperature pitch mixing laggard 2 that destilling tower comes#Heating furnace is heated to
350~380 DEG C enter 2#Destilling tower, through vacuum distillation separation (absolute pressure of top of the tower be 15~25kPa, tower top temperature be 260~
280 DEG C), one carbolineum of overhead extraction, side line cuts anthracene oil (300~320 DEG C of temperature of extraction), and tower bottom produces mid temperature pitch (temperature
330~360 DEG C of degree, 80~90 DEG C of softening point), first is that directly as international sale, second is that being sent into modification kettle produces modified coal tar pitch；
4) sedimentation separation is extracted
By 1#The soft pitch that destilling tower comes is mixed with extractant agent, separates (separation temperature into extraction settlement separator
100~150 DEG C, disengaging time 8~12 hours), light phase send light phase destilling tower after separation, and heavy phase send heavy phase destilling tower；
The extractant is the mixture of kerosene, washing oil；
5) light phase is distilled
By extraction settlement separator light phase, the circulation refined bitumen come with light phase destilling tower bottom mixes, through light phase plus
Hot stove heating after enter light phase destilling tower, be evaporated under reduced pressure (absolute pressure of top of the tower be 10~30kPa, tower top temperature 180~230
DEG C), overhead extraction mixed solvent is back to extraction settlement separator after cooling and is recycled, and tower bottom produces low quinoline non-soluble
The refined bitumen (250~300 DEG C of temperature of extraction) of object, can be used as the direct export trade of product (side line carbolineum produces mouth and closes)；Adjustment
The operating duty of light phase destilling tower, absolute pressure of top of the tower are 10~30kPa, and 180~230 DEG C of tower top temperature, side line carbolineum produces
Mouth opens extraction carbolineum (280~330 DEG C of temperature of extraction), then tower bottom can produce impregnating pitch (350~370 DEG C of temperature of extraction),
It can be used as the direct export trade of product；
6) heavy phase is distilled
By extraction settlement separator heavy phase, with heavy phase destilling tower bottom come circulation binder pitch mix, through heavy phase
Enter heavy phase destilling tower after heating stove heating, is evaporated under reduced pressure (absolute pressure of top of the tower is 10~30kPa), overhead extraction mixing is molten
Agent is back to extraction settlement separator after cooling and is recycled, side take-off carbolineum (280~330 DEG C of temperature of extraction), tower bottom
Binder pitch (extraction temperature is 350~370 DEG C) is produced, first is that as the direct export trade of product, second is that being sent into modification kettle production
Pitch；
7) pitch modifies
By 2#The mid temperature pitch that destilling tower comes, the circulation modified coal tar pitch come with modification bottom mix, and modified heating furnace adds
Enter modification kettle after heat, modified operation (temperature is 350~400 DEG C, and the residence time is 6~10 hours), kettle top is flashed
Oil, bottom obtain modified coal tar pitch, can be used as the direct export trade of product；
By heavy phase destilling tower Lai binder pitch, with modification bottom come circulation modified coal tar pitch mix, modified heating
Enter modification kettle after stove heating, modified operation (temperature is 350~400 DEG C, and the residence time is 6~10 hours), kettle top obtains
Flash oil, bottom obtain pitch, can be used as the direct export trade of product.
Compared with prior art, the utility model has the beneficial effects that
1) in such a way that distillation, extraction, modification combine, multi items pitch is produced simultaneously using set of device, is operated
Flexibly, it can satisfy demand of the market to different pitches product, solve the single added value of asphaltic products in previous tar production
It is low that problem, market adaptability are strong；
2) process is simple and direct, and logistics is smooth, compact arrangement of equipment, reduces land occupation, shortens the conveying distance of asphaltene, reduces
Line clogging；
3) mode that destilling tower selects normal pressure, vacuum distillation to combine according to medium feature, temperature, pressure regime distribution are closed
Reason, vacuum distillation both reduce operation temperature, reduce the consumption of fuel and cooling water, and can improve operating environment, are conducive to
Environmental protection；
4) each destilling tower tower bottom that is, convenient for operation and adjusting, and can effectively be prevented using the hydronic heat-supplying mode of oil
The only generation of coking；
5) technical process is not passed through steam, does not generate waste water；
6) stepped heat exchange is used, medium waste heat is made full use of, saves the energy；
7) extractive distillation system extractant is recycled, basic free of losses, saves operating cost；
8) slective extraction sedimentation separation mode isolates quinoline insolubles, and low operation temperature avoids high-temperature coking.
Detailed description of the invention
Fig. 1 is the principle schematic diagram of the utility model.
In figure: 1- dehydrating tower 2-1#Heating furnace 3-1#Destilling tower 4-2#Heating furnace 5-2#Destilling tower 6- extraction sedimentation point
Change from device 7- light phase heating furnace 8- light phase destilling tower 9- heavy phase heating furnace 10- heavy phase destilling tower 11- modification heating furnace 12-
Matter kettle
Specific embodiment
Specific embodiment of the present utility model is described further with reference to the accompanying drawing:
As shown in Figure 1, the utility model relates to a kind of distillation produced in conjunction with extraction phase various asphalt Product Process dress
It sets, including dehydrating tower 1, Distallation systm, extracting system and pitch reforming system, which is characterized in that the dehydrating tower 1 is equipped with tar
Entrance, water/light oil produce mouth, and boiled tar produces mouth；
The Distallation systm is by 1#Heating furnace 2,1#Destilling tower 3,2#Heating furnace 4,2#Destilling tower 5 forms, wherein 1#Destilling tower 2
With 1#Heating furnace 3 connects, and tower top is equipped with carbolic oil and produces mouth, and side line is equipped with naphtalene oil extraction mouth and washing oil produces mouth, and tower bottom is equipped with four
Road soft pitch produces mouth, is recycled back to 1 after merging all the way with boiled tar extraction mouth#Heating furnace 2 removes storage facility or straight all the way
It connects as international sale, go 2 all the way#Heating furnace 4 removes extracting system all the way；2#Destilling tower 4 and 2#Heating furnace 5 connects, and tower top is set
There is carbolineum to produce mouth, side line is equipped with anthracene oil and produces mouth, and tower bottom is equipped with three road mid temperature pitches and produces mouth, adopts all the way with soft pitch
Outlet is recycled back to 2 after merging#Heating furnace 4, go all the way storage facility or as the direct export trade of product, all the way deasphalting modification system
System；
The extracting system is by extraction settlement separator 6, light phase heating furnace 7, light phase destilling tower 8, heavy phase heating furnace 9 and again
Phase destilling tower 10 forms, wherein extraction settlement separator 6 is connect with soft pitch extraction mouth, produces mouth equipped with light phase and heavy phase is adopted
Outlet；Light phase destilling tower 8 is connect with light phase heating furnace 7, and tower top is equipped with mixed solvent and produces mouth, and side line is equipped with changeable carbolineum
Mouth is produced, tower bottom is equipped with two-way refined bitumen and produces mouth, is recycled back to light phase heating furnace 7, one after merging all the way with light phase extraction mouth
Road removes storage facility or as the direct export trade of product；Heavy phase destilling tower 10 is connect with heavy phase heating furnace 9, and tower top is equipped with mixed solvent
The mixed solvent of extraction mouth and 8 tower top of light phase destilling tower extraction mouth removes extraction settlement separator 6 after merging, and side line is adopted equipped with carbolineum
Outlet, tower bottom are equipped with three road binder pitch and produce mouth, are recycled back to heavy phase heating furnace 9, one after merging all the way with heavy phase extraction mouth
Storage facility or export trade, all the way deasphalting reforming system are gone in road；
The pitch reforming system is made of modification heater 11 and modification kettle 12, wherein modification kettle 12 and modification heater
11 connection, kettle top be equipped with flash oil produce mouth, bottom be equipped with two-way modified coal tar pitch produce mouth, all the way with mid temperature pitch extraction mouth/
Binder pitch extraction mouth is recycled back to modification heating furnace 11 after merging, and goes storage facility or export trade all the way.
When the 8 side line carbolineum of light phase destilling tower adopts port opening and cuts carbolineum, tower bottom obtains impregnating pitch product, otherwise
Obtain refined bitumen product.
12 bottom modified coal tar pitch of the modification kettle extraction mouth and mid temperature pitch extraction mouth are recycled back to modification heating furnace after merging
11, modified coal tar pitch product is obtained, pitch product is otherwise obtained.
All heating furnaces are vertical coil cylindrical furnace, and furnace tube material is stainless steel, and are changed using air with flue gas
Heat, burner select low nitrogen oxygen burner, energy conservation and environmental protection.
Distillation produces various asphalt Product Process in conjunction with extraction phase, includes the following steps:
1) feedstock processing
Water content is 1%-3%, 80-90 DEG C of temperature of coal tar after exchanging heat with fraction and being preheating to 130-140 DEG C by
Tar entrance enters dehydrating tower 1 and removes moisture, and overhead extraction light oil distillate can be used as the direct export trade of product, and tower bottom extraction dehydration is burnt
Oil enters Distallation systm；
Dehydrating tower 1 operates in atmospheric conditions, 101~107kPa of absolute pressure of top of the tower, and 95~120 DEG C of tower top temperature, tower
180~210 DEG C of bottom temperature；
2) air-distillation
By dehydrating tower 1 boiled tar and 1#The circulation soft pitch of destilling tower 3 is mixed into 1#Heating furnace 2, heating
Enter 1 after to 350~390 DEG C#Destilling tower 3, through air-distillation separation (tower top pressure control in 101~107kPa of absolute pressure,
170~185 DEG C of tower top temperature), overhead extraction carbolic oil, side line produces naphtalene oil (210~240 DEG C of temperature of extraction) and washing oil respectively
(260~280 DEG C of temperature of extraction), carbolic oil, naphtalene oil and washing oil fraction are sent into subsequent production unit or export trade after heat exchange and cooling；
Tower bottom produces soft pitch (about 330~360 DEG C of temperature of extraction, softening point are 40~60 DEG C), and there are three whereabouts altogether, first is that directly
As international sale, second is that going 2#Destilling tower produces mid temperature pitch, third is that extracting system is gone to produce other asphaltic products；
3) secondary pressure is distilled
1#The soft pitch of destilling tower 3 and 2#The circulation mid temperature pitch mixing laggard 2 of destilling tower 5#Heating furnace 4, heating
Enter 2 to 350~380 DEG C#Destilling tower 5, through vacuum distillation separation, (absolute pressure of top of the tower is 15~25kPa, and tower top temperature is
260~280 DEG C), one carbolineum of overhead extraction, side line cuts anthracene oil (300~320 DEG C of temperature of extraction), and tower bottom produces medium temperature drip
Green (330~360 DEG C of temperature, 80~90 DEG C of softening point), first is that changing directly as international sale second is that being sent into the modification production of kettle 12
Matter pitch；
4) sedimentation separation is extracted
By 1#The soft pitch of destilling tower 3 is mixed with extractant agent, into extraction settlement separator 6 separation (separation temperature
100~150 DEG C of degree, disengaging time 8~12 hours), light phase send light phase destilling tower 8 after separation, and heavy phase send heavy phase destilling tower 10；
The extractant is the mixture of kerosene, washing oil；
5) light phase is distilled
By extraction settlement separator 6 light phase, with 8 bottom of light phase destilling tower come circulation refined bitumen mix, through light phase
Heating furnace 7 heat after enter light phase destilling tower 8, be evaporated under reduced pressure (absolute pressure of top of the tower be 10~30kPa, tower top temperature 180~
230 DEG C), overhead extraction mixed solvent is back to extraction settlement separator 6 after cooling and is recycled, and tower bottom produces low quinoline
The refined bitumen (content of 250~300 DEG C of temperature of extraction, quinoline insolubles (QI) is not more than 0.5%) of insoluble matter, can be used as production
The direct export trade of product (side line carbolineum produces mouth and closes)；Adjust light phase destilling tower 8 operating duty, absolute pressure of top of the tower be 10~
30kPa, 180~230 DEG C of tower top temperature, side line carbolineum adopts port opening extraction carbolineum (280~330 DEG C of temperature of extraction), then tower
Bottom can produce impregnating pitch (350~370 DEG C of temperature of extraction), can be used as the direct export trade of product；
6) heavy phase is distilled
By extraction settlement separator 6 heavy phase, with 10 bottom of heavy phase destilling tower come circulation binder pitch mix, through weigh
It is added after hot stove 9 heats and enters heavy phase destilling tower 10, be evaporated under reduced pressure (absolute pressure of top of the tower is 10~30kPa), overhead extraction
Mixed solvent is back to extraction settlement separator 6 after cooling and is recycled, side take-off carbolineum (extraction temperature 280~330
DEG C), tower bottom produces binder pitch (extraction temperature is 350~370 DEG C), first is that changing as the direct export trade of product second is that being sent into
Matter kettle 12 produces pitch；
7) pitch modifies
By 2#The mid temperature pitch of destilling tower 5, the circulation modified coal tar pitch come with modification 12 bottom of kettle mix, modified heating furnace
Enter modification kettle 12 after 11 heating, modified operation (temperature is 350~400 DEG C, and the residence time is 6~10 hours), kettle top obtains
To flash oil, bottom obtains modified coal tar pitch, can be used as the direct export trade of product；
If using extractive distillation system heavy phase destilling tower bottom come binder pitch as raw material, i.e., by heavy phase destilling tower 10
Binder pitch, the circulation modified coal tar pitch come with modification 12 bottom of kettle mix, and modified heating furnace 11 enters modification kettle 12 after heating,
Modified operation (temperature is 350~400 DEG C, and the residence time is 6~10 hours) (operating duty is constant), kettle top is flashed
Oil, bottom obtain pitch, can be used as the direct export trade of product.
Claims (5)
1. distillation with extraction phase in conjunction with production various asphalt Product Process device, including dehydrating tower, Distallation systm, extracting system and
Pitch reforming system, which is characterized in that the dehydrating tower is equipped with tar entrance, and water/light oil produces mouth, and boiled tar produces mouth；
The Distallation systm is by 1#Heating furnace, 1#Destilling tower, 2#Heating furnace and 2#Destilling tower composition, wherein 1#Destilling tower and 1#Heating
Furnace connection, tower top are equipped with carbolic oil and produce mouth, and side line is equipped with naphtalene oil extraction mouth and washing oil produces mouth, and tower bottom is equipped with four road soft pitches
Mouth is produced, is recycled back to 1 after merging all the way with boiled tar extraction mouth#Heating furnace goes storage facility or export trade all the way, goes 2 all the way#
Heating furnace removes extracting system all the way；2#Destilling tower and 2#Heating furnace connection, tower top are equipped with carbolineum and produce mouth, and side line is equipped with anthracene oil
Mouth is produced, tower bottom is equipped with three road mid temperature pitches and produces mouth, is recycled back to 2 after merging all the way with soft pitch extraction mouth#Heating furnace, one
Storage facility or export trade, all the way deasphalting reforming system are gone in road；
The extracting system is by extraction settlement separator, light phase heating furnace, light phase destilling tower, heavy phase heating furnace and heavy phase destilling tower
Composition is equipped with light phase extraction mouth and heavy phase produces mouth wherein extraction settlement separator is connect with soft pitch extraction mouth；Light phase is steamed
It evaporates tower to connect with light phase heating furnace, tower top is equipped with mixed solvent and produces mouth, and side line is equipped with changeable carbolineum and produces mouth, and tower bottom is set
Have two-way refined bitumen produce mouth, all the way with light phase extraction mouth merge after be recycled back to light phase heating furnace, all the way go storage facility or
Export trade；Heavy phase destilling tower is connect with heavy phase heating furnace, and tower top is equipped with the mixing of mixed solvent extraction mouth and light phase overhead
Solvent extraction mouth removes extraction settlement separator after merging, side line is equipped with carbolineum and produces mouth, and tower bottom is equipped with three road binder pitch and adopts
Outlet is recycled back to heavy phase heating furnace after merging all the way with heavy phase extraction mouth, goes that storage facility or export trade, deasphalting changes all the way all the way
Matter system；
The pitch reforming system is made of modification heater and modification kettle, wherein modification kettle is connect with modification heater, kettle top
Mouth is produced equipped with flash oil, bottom is equipped with two-way modified coal tar pitch and produces mouth, adopts all the way with mid temperature pitch extraction mouth/binder pitch
Outlet is recycled back to modification heating furnace after merging, and goes storage facility or export trade all the way.
2. distillation according to claim 1 produces various asphalt Product Process device in conjunction with extraction phase, which is characterized in that
When the light phase destilling tower side line carbolineum adopts port opening and cuts carbolineum, tower bottom obtains impregnating pitch product, is otherwise refined
Asphaltic products.
3. distillation according to claim 1 produces various asphalt Product Process device in conjunction with extraction phase, which is characterized in that
The modification kettle bottom modified coal tar pitch extraction mouth and mid temperature pitch extraction mouth are recycled back to modification heating furnace after merging, and obtain modification drip
Otherwise green product obtains pitch product.
4. distillation according to claim 1 produces various asphalt Product Process device in conjunction with extraction phase, which is characterized in that
The dehydrating tower operates in atmospheric conditions, 101~107kPa of absolute pressure of top of the tower, and 95~120 DEG C of tower top temperature, column bottom temperature
180~210 DEG C.
5. distillation according to claim 1 produces various asphalt Product Process device in conjunction with extraction phase, which is characterized in that
The operation temperature of the modification kettle is 350~400 DEG C, and the residence time is 6~10 hours.
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| CN201822190713.5U CN209508153U (en) | 2018-12-26 | 2018-12-26 | Distillation produces various asphalt Product Process device in conjunction with extraction phase |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109517614A (en) * | 2018-12-26 | 2019-03-26 | 中冶焦耐(大连)工程技术有限公司 | Distillation produces various asphalt Product Process and device in conjunction with extraction phase |
| CN115197733A (en) * | 2022-06-29 | 2022-10-18 | 鞍钢化学科技有限公司 | Low-QI impregnant asphalt preparation system and process |
-
2018
- 2018-12-26 CN CN201822190713.5U patent/CN209508153U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109517614A (en) * | 2018-12-26 | 2019-03-26 | 中冶焦耐(大连)工程技术有限公司 | Distillation produces various asphalt Product Process and device in conjunction with extraction phase |
| CN109517614B (en) * | 2018-12-26 | 2024-07-09 | 中冶焦耐(大连)工程技术有限公司 | Process and device for producing various asphalt products by combining distillation and extraction |
| CN115197733A (en) * | 2022-06-29 | 2022-10-18 | 鞍钢化学科技有限公司 | Low-QI impregnant asphalt preparation system and process |
| CN115197733B (en) * | 2022-06-29 | 2024-03-15 | 鞍钢化学科技有限公司 | Low QI impregnant asphalt preparation system and process |
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