CN109852413A - A kind of method of coal tar production modified coal tar pitch - Google Patents
A kind of method of coal tar production modified coal tar pitch Download PDFInfo
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- CN109852413A CN109852413A CN201910132758.3A CN201910132758A CN109852413A CN 109852413 A CN109852413 A CN 109852413A CN 201910132758 A CN201910132758 A CN 201910132758A CN 109852413 A CN109852413 A CN 109852413A
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Abstract
The present invention relates to a kind of methods of coal tar production modified coal tar pitch, raw tar is by removing moisture in dehydrating tower, distillation separation is carried out in atmospheric distillation tower, vacuum distillation tower is evaporated under reduced pressure, modified coal tar pitch reaction tower is reacted, modified coal tar pitch flash column is flashed, and qualified modified coal tar pitch product is finally obtained.The present invention has process flow short, and good operation, with low investment, low energy consumption, environment protecting is good, adapts to the advantage of enlargement.
Description
Technical field
The present invention relates to a kind of methods of coal tar production modified coal tar pitch, it belongs to metallurgical coking industry coal tar processing skill
Art field.
Background technique
Coal tar is directly obtained by condensing recovery in coke-oven gas, and yield accounts for about the 3-4% of coking dry coal, group
At extremely complex, containing up to ten thousand kinds of substances, identified substance has more than 500 kinds, and the product being capable of processing has more than 200 kinds, wherein naphthalene
Oil, carbolineum, washing oil and phenols are distinctive very rare chemical products in coal tar, and account for coal tar content more than half
It is then pitch.Producing asphalt from coal tar is generally carried out by tar distillation technique, current enterprise both at home and abroad generallys use, skill
The reliable tar distillation technique of comparative maturity has three kinds of air-distillation, atmospheric and vacuum distillation and vacuum distillation in art.
Chinese patent CN 102634363A describes the production procedure and advantage and disadvantage of above-mentioned 3 kinds of tar distillation technique in detail,
And invented a kind of three-tower type Atmospheric vacuum tar distillation technique, process flow is relatively reasonable, and be suitable for produce per year 200,000 tons with
On tar production processing, but the technique has certain deficiency: first is that it is to pass through circulating heat conduction that the technique, which has multiple heat exchangers,
Oil causes entire process flow that need to add a set of Heat-conduction oil circulation system, increases the technique as heating and cooling medium
Equipment investment, second is that carbolic oil, naphtalene oil and washing oil, by two destilling tower extraction, these three oil contents are needed in preparing high-purity product again
Enter rectifying column after mixing heating, this makes these three oil contents first pass through cooling using heating, and heating is repeated, and wastes
Heat, has seriously affected the economy of the technique；Third is that the technique only produces mid temperature pitch or maltha is taken out,
And on the market since the adhesive property of modified coal tar pitch is good, the advantages that carboloy residue is high, the market price is always above mid temperature pitch
Or the price of maltha, therefore the economy that this point also results in the technique needs to be further increased.
Chinese patent CN101139527A discloses a kind of method that a variety of chemical products are extracted from coal tar, technique
Tri-mixed fractions are cut in tar king-tower atmospheric operation by dehydration for tar, tower bottom cuts heavy oil fraction, and overhead fraction is by washing
Wash and obtain naphtalene oil after dephenolize, obtain 95 naphthalene of methyl naphthalene and finished product after naphtalene oil purification, obtained after heavy oil fraction air-distillation carbolineum and
Asphaltic products, the technique mainly produce naphthalene and pitch, not consider modified pitch production, and the patent technique do not account for it is whole
The energy consumption of a technique and the comprehensive utilization of energy.
Chinese patent CN101775304A discloses the method for a kind of coal tar production modified coal tar pitch and medium temperature modified coal tar pitch,
The technique obtains mid temperature pitch by simple distillation to after coal tar heating, and mid temperature pitch is then sent into reaction tower and modification
Tower respectively obtains medium temperature modified coal tar pitch and modified coal tar pitch after certain time reacts, and the technique is in addition to using tube furnace to original
Expect not needing in addition to increase heat source except tar heating, energy consumption consumption is relatively low, reduces environmental pollution, meets low-carbon economy
Trend, but the technique in a destilling tower all oil contents, including light oil, washing oil, naphtalene oil, carbolic oil and carbolineum, entirely
Portion, which distills, to be gone to refine again, this makes the thermic load of the tower excessively huge, more demanding to the material of tower, and the technique does not have
Have and consider heat exchange, so that the heat of mixing oil content and modified coal tar pitch is not all reasonably utilized.
Chinese patent CN104726122A discloses a kind of Production Process for Modified Pitch, which is modified using primary heating
Process for preparing asphalt only uses a tube furnace and is heated, and energy-saving effect is obvious, but only one pitch of the technique is detained tower
Asphalt production is carried out, pitch can only carry out thermal polycondensation modification and can not be flashed in the delay tower, and the pitch produced is only
It can be medium temperature modified coal tar pitch, cannot get that softening point is higher, the better modified coal tar pitch of price, and the process tars pretreatment stage is used
One ultracentrifuge carries out the separation of weight component to tar, by the rotating cylinder material property and ultracentrifuge of ultracentrifuge
Environment temperature and humidity high request is limited, which is difficult to large-scale promotion application.
Chinese patent CN102161902A discloses a kind of coal tar deep processing technique based on four mixed fractions, the technique kind
Raw tar after dehydrating tower is dehydrated enter tar king-tower distilled, tower top cuts light phenol naphthalene and washes four contaminated product fractions, tower
Bottom produces the production that miscella carries out carbolineum and mid temperature pitch, and the method that four contaminated products which provides are cut simultaneously can be solved effectively
Certainly common process phenol naphthalene concentration degree and the not high problem of yield, the invention can also be realized flexible according to different pitches class products scheme
It is adjustable: perhaps to produce carbon black oil and perhaps produce I carbolineum and maltha or production I carbolineum, II carbolineum and maltha, but the work
Skill still cannot produce that softening point is higher, the better modified coal tar pitch of price, this affects the economic performance of the technique, and the technique
Still waste heat recycling is carried out with conventional conduction oil, needs to increase a set of Heat-conduction oil circulation system in process flow, increases
The cost of investment of the technique.
From above relatively as can be seen that existing Tar production pitch technique respectively has feature, there is its shortcoming: or
Economic performance is bad, perhaps can not produce next high-quality modified pitch or energy consumption is too high, therefore it is excellent to be badly in need of a kind of economic performance
It is different, low energy consumption, adapt to enlargement coal tar processing production modified coal tar pitch technique.
Summary of the invention
The object of the present invention is to provide a kind of process flow is short, good operation, with low investment, low energy consumption, environment protecting is good, energy is suitable
The method for answering the coal tar production modified coal tar pitch of enlargement.
To achieve the above object, the technical solution adopted by the present invention is that:
A kind of method of coal tar production modified coal tar pitch comprising following steps:
1) raw tar is changed by raw tar light oil heat exchanger, raw tar mixed triolein heat exchanger, raw tar I carbolineum
Hot device and raw tar II carbolineum heat exchanger are warming up to 190- with the heat exchange of light oil, mixed triolein, I carbolineum and II anthracene oil fraction respectively
Enter dehydrating tower after 220 DEG C；
2) moisture is removed under raw tar condition of normal pressure in dehydrating tower, dehydration column overhead pressure is controlled in absolute pressure
101~107kPa, 95~120 DEG C of the moisture and light oil fraction come out from dehydrating tower top are cooled to through recirculated water cooling condenser
40-50 DEG C enters oil water separator, and 180~210 DEG C of tower bottom component is heated to by No.1 tubular heater after dehydration of tar
Distillation separation is carried out in 290-320 DEG C of entrance atmospheric distillation tower；
3) control of atmospheric distillation tower tower top pressure comes out in 101~107kPa of absolute pressure from air-distillation column overhead
110~130 DEG C of light oil fraction is cooled to 40-50 DEG C of entrance by raw tar light oil heat exchanger and recirculated water light oil condenser
Oil water separator；200~240 DEG C of the phenol naphthalene cut from atmospheric distillation tower side line washes mixed triolein fraction through raw tar mixed triolein
Heat exchanger and mixed triolein cooler obtain phenol naphthalene after being cooled to 60-90 DEG C and wash mixed triolein fraction, evaporate from the tower bottom of atmospheric distillation tower
265~295 DEG C of mixed components out pass through modified coal tar pitch oil gas anhydrous tar heat exchanger and modified coal tar pitch anhydrous tar heat exchanger
Enter after No. two tubular heaters are heated to 370-390 DEG C after heat exchange and is evaporated under reduced pressure into vacuum distillation tower；
4) oil water separator separation water outlet and light oil, light oil are divided into three parts after the pressurization of light oil reflux pump and convey, and first
Part light oil enters dehydrating tower top, reflux ratio 3-6 as phegma, and second part light oil enters normal pressure as phegma and steams
Tower top, reflux ratio 5-9 are evaporated, Part III removes oil depot as light oil products, and water is directly entered oil depot wastewater trough；
5) control of vacuum distillation tower tower top pressure is in 10~30kPa of absolute pressure, and be evaporated under reduced pressure that column overhead comes out 250~
280 DEG C of I anthracene oil fraction is cooled to 85-95 DEG C by raw tar I carbolineum heat exchanger and I carbolineum cooler and enters I carbolineum tank,
The I carbolineum flowed out from I carbolineum tank except part as reflux it is outer remaining be all used as product to be delivered to oil depot, I carbolineum reflux ratio is 10-
20；It is 310~330 DEG C that II anthracene oil fraction, which produces temperature, and II anthracene oil fraction passes through raw tar II carbolineum heat exchanger and II carbolineum
Cooler be cooled to 85-95 DEG C enter II carbolineum tank, from II carbolineum tank flow out II carbolineum except part as reflux in addition to remaining all
It is delivered to oil depot as product, II carbolineum reflux ratio is 10-20；340~370 DEG C of mixing groups distillated from vacuum distillation tower tower bottom
Divide and is reacted into modified coal tar pitch reaction tower；
6) mixed component carries out thermal polycondensation reaction, modified coal tar pitch reaction tower top of tower pressure control in modified coal tar pitch reaction tower
System temperature in 101~107kPa of absolute pressure, tower is 380~400 DEG C, and the reaction time in modified coal tar pitch reaction tower is 4~10
Hour；The modified pitch oil gas anhydrous tar heat exchanger of the oil-gas component that tower top distillates and modified coal tar pitch oil-gas condenser condense to
Enter oil depot after 80-90 DEG C, tower bottom outflow component enters No. three tubular heaters and is heated to 400-420 DEG C, the modification after heating
Pitch mixed component except part enter pitch modification tower carry out heat offer in addition to remaining fully enter modified coal tar pitch flash column into
Row flash distillation, reflux ratio 2-5；
7) for the pressure control in modified coal tar pitch flash column in 10~60KPa of absolute pressure, temperature controls the flash distillation at 360~380 DEG C
Time is 5~120 minutes；The modified pitch anhydrous tar heat exchanger of modified coal tar pitch flash column the bottomsstream and modified coal tar pitch are cold
But device is cooled to 100-120 DEG C and obtains qualified modified coal tar pitch product, the group lease making flash oil condensing device condensation that flash overhead goes out
Enter flash oil tank after to 80-90 DEG C, and is delivered to oil depot through flashing oil pump.
Further, the atmospheric distillation tower and vacuum distillation tower are large aperture float valve plate column, and material is stainless steel,
Atmospheric distillation tower is equipped with 15~22 blocks of theoretical trays, and vacuum distillation tower is equipped with 30~45 blocks of theoretical trays.
Further, the No.1 tubular heater, No. two tubular heaters and No. three tubular heaters are vertical disc
Pipe cylindrical furnace, lower portion of furnace body are radiant section, and furnace tube material is stainless steel.
Further, the raw tar light oil heat exchanger, raw tar I carbolineum heat exchanger, modified coal tar pitch anhydrous tar
Heat exchanger, modified coal tar pitch oil gas anhydrous tar heat exchanger, raw tar II carbolineum heat exchanger, raw tar mixed triolein heat exchanger,
Recirculated water cooling condenser, recirculated water light oil condenser, I carbolineum cooler, modified coal tar pitch oil-gas condenser, modified coal tar pitch cooler,
Flash oil condensing device, II carbolineum cooler and mixed triolein cooler are shell-and-tube heat exchanger, and shell-and-tube heat exchanger is according to fluid
Different selection fixed tube sheets, U-tube or the floating head type of property, heat exchanger material is according to the corrosion condition of medium selection carbon steel or not
Become rusty steel.
Compared with existing tar distillation produces pitch technique, the invention has the following advantages that
1, the separation of dehydration of tar and light oil and mixed triolein carries out under normal pressure, and the separation of I carbolineum and II carbolineum is being depressurized
Lower progress, temperature, pressure regime distribution are reasonable.Compared with two vacuum tower operating systems, reduce vacuum pump, vacuum condenser etc.
A set of vacuum equipment, reduces one-time investment, also reduces the complexity of operation, vacuum distillation both reduced operation temperature,
Reduce gas consumption amount, improves operating environment again, is conducive to environmental protection；
2, cutting for each fraction is completed in two destilling towers, and You Liangtai tube furnace distinguishes heat supply, is solved with single suit
Set the technical problem for handling extensive tar；
3, present invention process process is short, and control is easy, easily operated, stable product quality, capital expenditure, equipment operation,
Maintenance cost is lower；
4, carbolic oil, naphtalene oil and washing oil fraction produce together as three mixed fractions, improve the high value added products such as phenol, naphthalene
Yield；
5, UTILIZATION OF VESIDUAL HEAT IN is abundant, and the heat of modified coal tar pitch and each fraction adequately can be recycled and be utilized by heat exchange,
The consumption for reducing tubular type producer gas, reduces operating cost, meets the development trend of low-carbon economy；
6, distillation process is not required to be passed through direct steam, does not generate containing phenol, ammonia waste water；
7, the fraction easily crystallize, easily solidified is cooling with warm water, reduces the blocking of equipment and pipeline
8, each fraction and raw tar have carried out sufficient heat exchange, eliminate Heat-conduction oil circulation system, so that technique
Whole investment reduces.
It is a variety of attached to can get light oil, mixed triolein, I carbolineum, II carbolineum and modified coal tar pitch etc. in terms of product for the method for the present invention
Value added higher product；In terms of energy consumption, the comprehensive utilization of the energy is considered, technique Atmospheric vacuum combines, and each level analysis is comprehensive
It closes and utilizes；In terms of construction investment, weighs product structure and technique length, used relatively reasonable process flow.
Detailed description of the invention
Fig. 1 is process flow diagram of the invention；
In figure: 1 is dehydrating tower, and 2 be recirculated water cooling condenser, and 3 be oil water separator, and 4 be recirculated water light oil condenser, and 5 are
Raw tar light oil heat exchanger, 6 be raw tar I carbolineum heat exchanger, and 7 be I carbolineum cooler, and 8 be modified coal tar pitch oil gas condensation
Device, 9 for flash distillation oil tank, 10 for flash distillation oil pump, 11 be modified coal tar pitch cooler, 12 be modified coal tar pitch anhydrous tar heat exchanger, 13
It is modified coal tar pitch flash column for flash oil condensing device, 14,15 pump for modified coal tar pitch, and 16 be No. three tubular heaters, and 17 be modification
Pitch oil gas anhydrous tar heat exchanger, 18 be modified coal tar pitch reaction tower, and 19 be modified coal tar pitch tower bottom circulating pump, and 20 be No. two tubular types
Heating furnace, 21 be vacuum distillation tower, and 22 be vacuum distillation tower tower bottom component delivery pump, and 23 be I carbolineum reflux pump, and 24 be II carbolineum
Reflux pump, 25 be I carbolineum tank, 26 be raw tar II carbolineum heat exchanger, 27 be II carbolineum cooler, 28 be II carbolineum tank, 29
It is mixed triolein cooler for raw tar mixed triolein heat exchanger, 30,31 pump for mixed triolein, and 32 be No. two tar pumps, and 33 be normal pressure
Destilling tower, 34 be No.1 tubular heater, and 35 be light oil reflux pump, and 36 pump for No.1 tar.
Specific embodiment
The invention will be further described with reference to the accompanying drawings and examples.
Embodiment 1
As shown in Figure 1, the method for one of the present embodiment coal tar production modified coal tar pitch comprising following steps:
1) raw tar initially enters raw tar light oil heat exchanger 5, raw tar mixed triolein heat exchanger 29, raw tar
I carbolineum heat exchanger 6 and raw tar II carbolineum heat exchanger 26 exchange heat with light oil, mixed triolein, I carbolineum and II anthracene oil fraction respectively to be risen
Temperature is to entering dehydrating tower 1 after 190 DEG C；
2) dehydrating tower 1 operates in atmospheric conditions, removes moisture in dehydrating tower 1 under raw tar condition of normal pressure, dehydration
1 absolute pressure of top of the tower of tower is 107kPa, and 95 DEG C of the moisture and light oil fraction distillated from dehydrating tower top is through recirculated water cooling condenser 2
It is cooled to 40 DEG C and enters oil water separator 3,180 DEG C of boiled tars of tower bottom are added by 36 extraction of No.1 tar pump by No.1 tubular type
Hot stove 34 is heated to carrying out distillation separation in 290 DEG C of entrance atmospheric distillation towers 33；
3) atmospheric distillation tower 33 is atmospheric operation, and the control of atmospheric distillation tower tower top pressure is in absolute pressure 101kPa, from normal
130 DEG C of the light oil fraction that pressure overhead distillates enters after raw tar light oil heat exchanger 5 and raw tar heat exchange to follow
In ring water light oil condenser 4,50 DEG C are cooled to, into oil water separator 3；220 DEG C of phenol is cut from 33 side line of atmospheric distillation tower
Naphthalene washes mixed triolein fraction, is introduced into raw tar mixed triolein heat exchanger 29 to tar heating, then through mixed triolein cooler 30
After being cooled to 75 DEG C, then 31 are pumped with mixed triolein and is extracted out, send mixed triolein intermediate tank farm to store, through subsequent dephenolize washing system and work
Industry naphthalene system is further processed, and finally obtains carbolic oil, crude naphthalene product and high-quality washing oil；From atmospheric distillation tower 33
265 DEG C of miscellas that tower bottom distillates are delivered to modified coal tar pitch oil gas anhydrous tar heat exchanger 17 through No. two tar pumps 32 and modification drips
Green anhydrous tar heat exchanger 12 enter after No. two tubular heaters 20 are heated to 370 DEG C after exchanging heat enter vacuum distillation tower 21 into
Row vacuum distillation；
4) enter the light oil fraction in oil water separator 3 in step 2) by the separation of oil water separator 3 water outlet and light oil, gently
Oil is divided into three parts conveying after the pressurization of light oil reflux pump 35, and first part's light oil enters 1 top of dehydrating tower as phegma, returns
Stream is than being 4, and second part light oil enters 33 top of atmospheric distillation tower as phegma, and reflux ratio 7, Part III is as light oil
Product removes oil depot, and water is directly entered oil depot wastewater trough；
5) vacuum distillation tower 21 is decompression operation, and the control of 21 tower top pressure of vacuum distillation tower is in absolute pressure 20kPa, decompression
250 DEG C of the I anthracene oil fraction that 21 tower top of destilling tower comes out is sent into I anthracene after raw tar I carbolineum heat exchanger 6 and tar heat exchange
Oil cooler 7 is cooled to 95 DEG C and enters I carbolineum tank 25, and the I carbolineum extracted out from I carbolineum tank 25 through I carbolineum reflux pump 23 removes part
It is that 20 work reflux are sent to 21 tower top of vacuum distillation tower by reflux ratio, rest part is delivered to I carbolineum oil depot as product；Decompression is steamed
21 side take-off II carbolineum of tower is evaporated, II anthracene oil fraction produces 310 DEG C of temperature, and II carbolineum passes through raw tar II carbolineum heat exchanger 26
Enter II carbolineum tanks 28 with being cooled to 95 DEG C by II carbolineum cooler 27 after tar heat exchange, with II carbolineum reflux pump 24 from II carbolineum
The II carbolineum that tank 18 is extracted out in addition to part is sent as reflux to the middle part of vacuum distillation tower 21 remaining be all used as product to be delivered to II anthracene
Oil depot, II carbolineum reflux ratio are 15；I carbolineum tank 25 and II carbolineum tank 28 are connected to vacuum system to guarantee vacuum distillation tower
The vacuum degree of 21 tower tops；The 340 DEG C of mixed components distillated from 21 tower bottom of vacuum distillation tower are conveyed by vacuum distillation tower tower bottom component
22 extraction of pump, which is sent to modified coal tar pitch reaction tower 18, is reacted；
6) mixed component carries out thermal polycondensation reaction, 18 top of tower pressure of modified coal tar pitch reaction tower in modified coal tar pitch reaction tower 18
Power control temperature in absolute pressure 101kPa, tower is 390 DEG C, and the reaction time is 10 hours；The oil-gas component that tower top distillates is modified
Pitch oil gas anhydrous tar heat exchanger 17 is upgraded after pitch oil-gas condenser 8 is cooled to 90 DEG C after exchanging heat with anhydrous tar to be entered
Flash oil oil depot is sent after modified 19 extraction of asphalt tower bottoming cycle pump of 18 tower bottom asphalt mixture of modified coal tar pitch reaction tower to No. three
Tubular heater 16 is heated to 410 DEG C, and the modified coal tar pitch mixed component after heating is except partial reflux to modified coal tar pitch reaction tower 18
Remaining the outer whole of offer for carrying out heat is sent into modified coal tar pitch flash column 14 and is flashed, reflux ratio 5；
7) pressure control in modified coal tar pitch flash column 14 is in 370 DEG C, flash-off time in absolute pressure 60KPa, temperature control
60 minutes；The flash oil that 14 flash overhead of modified coal tar pitch flash column goes out is sent into flash distillation after flash oil condensing device 13 is condensed to 90 DEG C
It in oil tank 9, and is flashed oil pump 10 and is delivered to flash oil oil depot, flash distillation oil tank 9 is connected to vacuum system to guarantee modified coal tar pitch
Vacuum degree in 14 tower of flash column；The modified extraction of bitumenpump 15 of 14 the bottomsstream of modified coal tar pitch flash column is sent to modified coal tar pitch
Enter after anhydrous tar heat exchanger 12 and anhydrous tar heat exchange and is cooled to 120 DEG C in modified coal tar pitch cooler 11 and obtains qualified change
Matter asphaltic products, modified coal tar pitch product are sent into modified coal tar pitch tank field.
The atmospheric distillation tower 33 and vacuum distillation tower 21 are large aperture float valve plate column, and material is stainless steel,
Atmospheric distillation tower 33 is equipped with 20 blocks of theoretical trays, and vacuum distillation tower 21 is equipped with 30 blocks of theoretical trays.
34, No. two tubular heaters 20 of the No.1 tubular heater and No. three tubular heaters 16 are vertical coil circle
Cylinder furnace, lower portion of furnace body is radiant section, and furnace tube material is stainless steel.
The raw tar light oil heat exchanger 5, raw tar I carbolineum heat exchanger 6, modified coal tar pitch anhydrous tar heat exchanger
17, modified coal tar pitch anhydrous tar heat exchanger 12, raw tar II carbolineum heat exchanger 26, raw tar mixed triolein heat exchanger 29, follow
Ring water condenser 2, recirculated water light oil condenser 4, I carbolineum cooler 7, modified coal tar pitch oil-gas condenser 8, modified coal tar pitch cooler
11, flash oil condensing device 13, II carbolineum cooler 27 and mixed triolein cooler 30 are U-tube shell-and-tube heat exchanger, heat exchanger
Material selects stainless steel.
Embodiment 2
As shown in Figure 1, the method for one of the present embodiment coal tar production modified coal tar pitch comprising following steps:
1) raw tar initially enters raw tar light oil heat exchanger 5, raw tar mixed triolein heat exchanger 29, raw tar
It exchanges heat respectively with light oil, mixed triolein, I carbolineum and II anthracene oil fraction in I carbolineum heat exchanger 6 and raw tar II carbolineum heat exchanger 26
Enter dehydrating tower 1 after being warming up to 210 DEG C；
2) dehydrating tower 1 operates in atmospheric conditions, removes moisture in dehydrating tower 1 under raw tar condition of normal pressure, dehydration
1 absolute pressure of top of the tower of tower is 104kPa, and 110 DEG C of the moisture and light oil fraction distillated from dehydrating tower top is through recirculated water cooling condenser
2, which are cooled to 45 DEG C, enters oil water separator 3, and 190 DEG C of boiled tars of tower bottom are added by 36 extraction of No.1 tar pump by No.1 tubular type
Hot stove 34 is heated to carrying out distillation separation in 310 DEG C of entrance atmospheric distillation towers 33；
3) atmospheric distillation tower 33 is atmospheric operation, the control of 33 tower top pressure of atmospheric distillation tower in absolute pressure 105kPa, from
120 DEG C of the light oil fraction that 33 tower top of atmospheric distillation tower distillates is laggard in raw tar light oil heat exchanger 5 and raw tar heat exchange
Enter in recirculated water light oil condenser 4, be cooled to 45 DEG C, into oil water separator 3；200 DEG C are cut from 33 side line of atmospheric distillation tower
Phenol naphthalene wash mixed triolein fraction, be introduced into raw tar mixed triolein heat exchanger 29 to tar heating, it is then cooling through mixed triolein
After device 30 is cooled to 60 DEG C, then 31 are pumped with mixed triolein and is extracted out, send mixed triolein intermediate tank farm to store, through subsequent dephenolize washing system
It is further processed with crude naphthalene system, finally obtains removal phenol carbolic oil, crude naphthalene product and high-quality washing oil；It is steamed from normal pressure
It evaporates 280 DEG C of miscellas that the tower bottom of tower 33 distillates and is delivered to modified coal tar pitch oil gas anhydrous tar heat exchanger 17 through No. two tar pumps 32
Enter after No. two tubular heaters 20 are heated to 380 DEG C after exchanging heat with modified coal tar pitch anhydrous tar heat exchanger 12 and enters decompression steaming
It evaporates and is evaporated under reduced pressure in tower 21；
4) enter the light oil fraction in oil water separator 3 in step 2) by the separation of oil water separator 3 water outlet and light oil, gently
Oil is divided into three parts conveying after the pressurization of light oil reflux pump 35, and first part's light oil enters 1 top of dehydrating tower as phegma, returns
Stream is than being 3, and second part light oil enters 33 top of atmospheric distillation tower as phegma, and reflux ratio 5, Part III is as light oil
Product removes oil depot, and water is directly entered oil depot wastewater trough；
5) vacuum distillation tower 21 is decompression operation, and the control of 21 tower top pressure of vacuum distillation tower is in absolute pressure 30kPa, decompression
270 DEG C of the I anthracene oil fraction that 21 tower top of destilling tower comes out is sent into I anthracene after raw tar I carbolineum heat exchanger 6 and tar heat exchange
Oil cooler 7 is cooled to 95 DEG C and enters I carbolineum tank 25, and the I carbolineum extracted out from I carbolineum tank 25 through I carbolineum reflux pump 23 removes part
It is that 15 work reflux are sent to 21 tower top of vacuum distillation tower by reflux ratio, rest part is delivered to I carbolineum oil depot as product；Decompression is steamed
21 side take-off II carbolineum of tower is evaporated, it is 320 DEG C that II anthracene oil fraction, which produces temperature, and II carbolineum passes through raw tar II carbolineum heat exchanger
26 be cooled to 90 DEG C by II carbolineum cooler 27 after tar heat exchange and enter II carbolineum tanks 28, with II carbolineum reflux pump 24 from II anthracene
The II carbolineum that oil tank 18 is extracted out in addition to part is sent as reflux to the middle part of vacuum distillation tower 21 remaining all product is used as to be delivered to II
Carbolineum oil depot, II carbolineum reflux ratio are 20；I carbolineum tank 25 and II carbolineum tank 28 are connected to vacuum system to guarantee to be evaporated under reduced pressure
The vacuum degree of 21 tower top of tower；The 360 DEG C of mixed components distillated from 21 tower bottom of vacuum distillation tower are defeated by vacuum distillation tower tower bottom component
It send 22 extraction of pump to send to modified coal tar pitch reaction tower 18 to be reacted；
6) mixed component carries out thermal polycondensation reaction, 18 top of tower pressure of modified coal tar pitch reaction tower in modified coal tar pitch reaction tower 18
Power control temperature in absolute pressure 105kPa, tower is 380 DEG C, and the reaction time is 7 hours；The modified drip of the oil-gas component that tower top distillates
It is upgraded to enter after pitch oil-gas condenser 8 is cooled to 85 DEG C after green oil gas anhydrous tar heat exchanger 17 and anhydrous tar heat exchange and dodge
Steam oil oil depot send to No. three after modified 19 extraction of asphalt tower bottoming cycle pump of 18 tower bottom asphalt mixture of modified coal tar pitch reaction tower and manages
Formula heating furnace 16 is heated to 420 DEG C, the modified coal tar pitch mixed component after heating except partial reflux to modified coal tar pitch reaction tower 18 into
Remaining outer whole of the offer of row heat is sent into modified coal tar pitch flash column 14 and is flashed, reflux ratio 5；
7) pressure control in modified coal tar pitch flash column 14 is in absolute pressure 40KPa, and temperature control is at 380 DEG C, flash-off time 5
Minute；The flash oil that 14 flash overhead of modified coal tar pitch flash column goes out is sent into flash oil after flash oil condensing device 13 is condensed to 85 DEG C
It in tank 9, and is flashed oil pump 10 and is delivered to flash oil oil depot, flash distillation oil tank 9 is connected to vacuum system to guarantee that modified coal tar pitch dodges
Steam the vacuum degree in 14 tower of tower；Modified bitumenpump 15 extraction of 14 the bottomsstream of modified coal tar pitch flash column send to modified coal tar pitch without
Enter after water tar heat exchanger 12 and anhydrous tar heat exchange and is cooled to 110 DEG C in modified coal tar pitch cooler 11 and obtains qualified modification
Asphaltic products, qualified modified coal tar pitch product are sent into modified coal tar pitch tank field.
The atmospheric distillation tower 33 and vacuum distillation tower 21 are plate column, and using large aperture float valve, material is not
Become rusty steel, and atmospheric distillation tower 33 is equipped with 22 blocks of theoretical trays, and vacuum distillation tower 21 is equipped with 38 blocks of theoretical trays.
The raw tar light oil heat exchanger 5, raw tar I carbolineum heat exchanger 6, modified coal tar pitch anhydrous tar heat exchanger
17, modified coal tar pitch anhydrous tar heat exchanger 12, raw tar II carbolineum heat exchanger 26, raw tar mixed triolein heat exchanger 29 are
Fixed tube-sheet exchanger, heat exchanger material selection stainless steel；Recirculated water cooling condenser 2, recirculated water light oil condenser 4, I carbolineum are cold
But device 7, modified coal tar pitch oil-gas condenser 8, modified coal tar pitch cooler 11, flash oil condensing device 13, II carbolineum cooler 27 and three
Contaminated product cooler 30 is U-tube shell-and-tube heat exchanger, heat exchanger material selection stainless steel.Remaining is the same as embodiment 1.
Embodiment 3
As shown in Figure 1, the method for one of the present embodiment coal tar production modified coal tar pitch comprising following steps:
1) raw tar initially enters raw tar light oil heat exchanger 5, raw tar mixed triolein heat exchanger 29, raw tar
It exchanges heat respectively with light oil, mixed triolein, I carbolineum and II anthracene oil fraction in I carbolineum heat exchanger 6 and raw tar II carbolineum heat exchanger 26
Enter dehydrating tower 1 after being warming up to 220 DEG C；
2) dehydrating tower 1 operates in atmospheric conditions, removes moisture in dehydrating tower 1 under raw tar condition of normal pressure, dehydration
1 absolute pressure of top of the tower of tower is 101kPa, and 120 DEG C of the moisture and light oil fraction distillated from dehydrating tower top is through recirculated water cooling condenser
2, which are cooled to 50 DEG C, enters oil water separator 3, and 210 DEG C of boiled tars of tower bottom are added by 36 extraction of No.1 tar pump by No.1 tubular type
Hot stove 34 is heated to carrying out distillation separation in 320 DEG C of entrance atmospheric distillation towers 33；
3) atmospheric distillation tower 33 is atmospheric operation, the control of 33 tower top pressure of atmospheric distillation tower in absolute pressure 107kPa, from
110 DEG C of the light oil fraction that 33 tower top of atmospheric distillation tower distillates is laggard in raw tar light oil heat exchanger 5 and raw tar heat exchange
Enter in recirculated water light oil condenser 4, be cooled to 40 DEG C, into oil water separator 3；240 DEG C are cut from 33 side line of atmospheric distillation tower
Phenol naphthalene wash mixed triolein fraction, be introduced into raw tar mixed triolein heat exchanger 29 to tar heating, it is then cooling through mixed triolein
After device 30 is cooled to 90 DEG C, then 31 are pumped with mixed triolein and is extracted out, send mixed triolein intermediate tank farm to store, through subsequent dephenolize washing system
It is further processed with crude naphthalene system, finally obtains removal phenol carbolic oil, crude naphthalene product and high-quality washing oil；It is steamed from normal pressure
It evaporates 295 DEG C of miscellas that the tower bottom of tower 33 distillates and is delivered to modified coal tar pitch oil gas anhydrous tar heat exchanger 17 through No. two tar pumps 32
Enter after No. two tubular heaters 20 are heated to 390 DEG C after exchanging heat with modified coal tar pitch anhydrous tar heat exchanger 12 and enters decompression steaming
It evaporates and is evaporated under reduced pressure in tower 21；
4) enter the light oil fraction in oil water separator 3 in step 2) by the separation of oil water separator 3 water outlet and light oil, gently
Oil is divided into three parts conveying after the pressurization of light oil reflux pump 35, and first part's light oil enters 1 top of dehydrating tower as phegma, returns
Stream is than being 6, and second part light oil enters 33 top of atmospheric distillation tower as phegma, and reflux ratio 9, Part III is as light oil
Product removes oil depot, and water is directly entered oil depot wastewater trough；
5) vacuum distillation tower 21 is decompression operation, and the control of 21 tower top pressure of vacuum distillation tower is in absolute pressure 10kPa, decompression
280 DEG C of the I anthracene oil fraction that 21 tower top of destilling tower comes out is sent into I anthracene after raw tar I carbolineum heat exchanger 6 and tar heat exchange
Oil cooler 7 is cooled to 85 DEG C and enters I carbolineum tank 25, and the I carbolineum extracted out from I carbolineum tank 25 through I carbolineum reflux pump 23 removes part
It is that 10 work reflux are sent to 21 tower top of vacuum distillation tower by reflux ratio, rest part is delivered to I carbolineum oil depot as product；Decompression is steamed
21 side take-off II carbolineum of tower is evaporated, it is 330 DEG C that II anthracene oil fraction, which produces temperature, and II carbolineum passes through raw tar II carbolineum heat exchanger
26 be cooled to 85 DEG C by II carbolineum cooler 27 after tar heat exchange and enter II carbolineum tanks 28, with II carbolineum reflux pump 24 from II anthracene
The II carbolineum that oil tank 18 is extracted out in addition to part is sent as reflux to the middle part of vacuum distillation tower 21 remaining all product is used as to be delivered to II
Carbolineum oil depot, II carbolineum reflux ratio are 10；I carbolineum tank 25 and II carbolineum tank 28 are connected to vacuum system to guarantee to be evaporated under reduced pressure
The vacuum degree of 21 tower top of tower；The 370 DEG C of mixed components distillated from 21 tower bottom of vacuum distillation tower are defeated by vacuum distillation tower tower bottom component
It send 22 extraction of pump to send to modified coal tar pitch reaction tower 18 to be reacted；
6) mixed component carries out thermal polycondensation reaction, 18 top of tower pressure of modified coal tar pitch reaction tower in modified coal tar pitch reaction tower 18
Power control temperature in absolute pressure 107kPa, tower is 400 DEG C, and the reaction time is 4 hours；The modified drip of the oil-gas component that tower top distillates
It is upgraded to enter after pitch oil-gas condenser 8 is cooled to 80 DEG C after green oil gas anhydrous tar heat exchanger 17 and anhydrous tar heat exchange and dodge
Steam oil oil depot send to No. three after modified 19 extraction of asphalt tower bottoming cycle pump of 18 tower bottom asphalt mixture of modified coal tar pitch reaction tower and manages
Formula heating furnace 16 is heated to 400 DEG C, the modified coal tar pitch mixed component after heating except partial reflux to modified coal tar pitch reaction tower 18 into
Remaining outer whole of the offer of row heat is sent into modified coal tar pitch flash column 14 and is flashed, reflux ratio 3；
7) pressure control in modified coal tar pitch flash column 14 is in 360 DEG C, flash-off time in absolute pressure 10KPa, temperature control
120 minutes；The flash oil that 14 flash overhead of modified coal tar pitch flash column goes out is sent into after flash oil condensing device 13 is condensed to 80 DEG C to be dodged
It in steam oil tank 9, and is flashed oil pump 10 and is delivered to flash oil oil depot, flash distillation oil tank 9 is connected to vacuum system to guarantee modification drip
Vacuum degree in green 14 tower of flash column；The modified extraction of bitumenpump 15 of 14 the bottomsstream of modified coal tar pitch flash column, which is sent to modification, to be dripped
Enter in modified coal tar pitch cooler 11 after green anhydrous tar heat exchanger 12 and anhydrous tar heat exchange be cooled to 100 DEG C obtain it is qualified
Modified coal tar pitch product, qualified modified coal tar pitch product are sent into modified coal tar pitch tank field.
The atmospheric distillation tower 33 and vacuum distillation tower 21 are plate column, and using large aperture float valve, material is not
Become rusty steel, and atmospheric distillation tower 33 is equipped with 15 blocks of theoretical trays, and vacuum distillation tower 21 is equipped with 45 blocks of theoretical trays.
The raw tar light oil heat exchanger 5, raw tar I carbolineum heat exchanger 6, modified coal tar pitch anhydrous tar heat exchanger
17, modified coal tar pitch anhydrous tar heat exchanger 12, raw tar II carbolineum heat exchanger 26, raw tar mixed triolein heat exchanger 29 are
Movable tube sheets heat exchanger, heat exchanger material selection stainless steel；Recirculated water cooling condenser 2, recirculated water light oil condenser 4, I carbolineum cooler
7, modified coal tar pitch oil-gas condenser 8, modified coal tar pitch cooler 11, flash oil condensing device 13, II carbolineum cooler 27 and mixed triolein
Cooler 30 is fixed tube-sheet exchanger, heat exchanger material selection stainless steel.Remaining is the same as embodiment 1.
Claims (4)
1. a kind of method of coal tar production modified coal tar pitch, which comprises the steps of:
1) raw tar passes through raw tar light oil heat exchanger, raw tar mixed triolein heat exchanger, raw tar I carbolineum heat exchanger
190-220 DEG C is warming up to the heat exchange of light oil, mixed triolein, I carbolineum and II anthracene oil fraction respectively with II carbolineum heat exchanger of raw tar
Enter dehydrating tower afterwards；
2) remove moisture under raw tar condition of normal pressure in dehydrating tower, the control of dehydration column overhead pressure absolute pressure 101~
107kPa, 95~120 DEG C of the moisture and light oil fraction come out from dehydrating tower top are cooled to 40-50 DEG C through recirculated water cooling condenser
Into oil water separator, 180~210 DEG C of tower bottom component is heated to 290-320 by No.1 tubular heater after dehydration of tar
DEG C enter atmospheric distillation tower in carry out distillation separation；
3) atmospheric distillation tower tower top pressure is controlled in 101~107kPa of absolute pressure, and 110 come out from air-distillation column overhead~
130 DEG C of light oil fraction is cooled to 40-50 DEG C by raw tar light oil heat exchanger and recirculated water light oil condenser and enters grease
Separator；200~240 DEG C of the phenol naphthalene cut from atmospheric distillation tower side line washes mixed triolein fraction and exchanges heat through raw tar mixed triolein
Device and mixed triolein cooler obtain phenol naphthalene after being cooled to 60-90 DEG C and wash mixed triolein fraction, distillate from the tower bottom of atmospheric distillation tower
265~295 DEG C of mixed components exchange heat by modified coal tar pitch oil gas anhydrous tar heat exchanger and modified coal tar pitch anhydrous tar heat exchanger
Enter after No. two tubular heaters are heated to 370-390 DEG C afterwards and is evaporated under reduced pressure into vacuum distillation tower；
4) oil water separator separation water outlet and light oil, light oil are divided into three parts conveying, first part after the pressurization of light oil reflux pump
Light oil enters dehydrating tower top, reflux ratio 3-6 as phegma, and second part light oil enters atmospheric distillation tower as phegma
Top, reflux ratio 5-9, Part III remove oil depot as light oil products, and water is directly entered oil depot wastewater trough；
5) control of vacuum distillation tower tower top pressure is evaporated under reduced pressure column overhead comes out 250~280 in 10~30kPa of absolute pressure
DEG C I anthracene oil fraction be cooled to 85-95 DEG C by raw tar I carbolineum heat exchanger and I carbolineum cooler and enter I carbolineum tank, from I
The I carbolineum of carbolineum tank outflow except part as reflux it is outer remaining be all used as product to be delivered to oil depot, I carbolineum reflux ratio is 10-20；
It is 310~330 DEG C that II anthracene oil fraction, which produces temperature, and II anthracene oil fraction is cooling by raw tar II carbolineum heat exchanger and II carbolineum
Device is cooled to 85-95 DEG C and enters II carbolineum tank, II carbolineum flowed out from II carbolineum tank remaining all conduct in addition to part is as reflux
Product is delivered to oil depot, and II carbolineum reflux ratio is 10-20；340~370 DEG C of mixed components distillated from vacuum distillation tower tower bottom into
Enter modified coal tar pitch reaction tower to be reacted；
6) mixed component carries out thermal polycondensation reaction in modified coal tar pitch reaction tower, and the control of modified coal tar pitch reaction tower top of tower pressure exists
101~107kPa of absolute pressure, temperature is 380~400 DEG C in tower, and the reaction time in modified coal tar pitch reaction tower is 4~10 hours；
The modified pitch oil gas anhydrous tar heat exchanger of the oil-gas component that tower top distillates and modified coal tar pitch oil-gas condenser are condensed to 80-90
Enter oil depot after DEG C, tower bottom outflow component enters No. three tubular heaters and is heated to 400-420 DEG C, and the modified coal tar pitch after heating is mixed
It is combined point in addition to part enters pitch modification tower to carry out the offer of heat remaining and fully enters modified coal tar pitch flash column and flashed,
Reflux ratio is 2-5；
7) pressure control in modified coal tar pitch flash column is in 10~60KPa of absolute pressure, and temperature control is at 360~380 DEG C, flash-off time
It is 5~120 minutes；The modified pitch anhydrous tar heat exchanger of modified coal tar pitch flash column the bottomsstream and modified coal tar pitch cooler
It is cooled to 100-120 DEG C and obtains qualified modified coal tar pitch product, the group lease making flash oil condensing device that flash overhead goes out is condensed to 80-
Enter flash oil tank after 90 DEG C, and is delivered to oil depot through flashing oil pump.
2. a kind of method of coal tar production modified coal tar pitch according to claim 1, it is characterised in that: the air-distillation
Tower and vacuum distillation tower are large aperture float valve plate column, and material is stainless steel, and atmospheric distillation tower is equipped with 15~22 pieces of theoretical towers
Plate, vacuum distillation tower are equipped with 30~45 blocks of theoretical trays.
3. a kind of method of coal tar production modified coal tar pitch according to claim 1, it is characterised in that: the No.1 tubular type
Heating furnace, No. two tubular heaters and No. three tubular heaters are vertical coil cylindrical furnace, and lower portion of furnace body is radiant section, boiler tube
Material is stainless steel.
4. a kind of method of coal tar production modified coal tar pitch according to claim 1, it is characterised in that: the raw tar
Light oil heat exchanger, raw tar I carbolineum heat exchanger, modified coal tar pitch anhydrous tar heat exchanger, modified coal tar pitch oil gas anhydrous tar change
Hot device, raw tar II carbolineum heat exchanger, raw tar mixed triolein heat exchanger, recirculated water cooling condenser, recirculated water light oil condenser,
I carbolineum cooler, modified coal tar pitch oil-gas condenser, modified coal tar pitch cooler, flash oil condensing device, II carbolineum cooler and three are mixed
Oil cooler is shell-and-tube heat exchanger, and shell-and-tube heat exchanger is according to the different selection fixed tube sheets of fluid properties, U-tube or floats
Hair style, heat exchanger material select carbon steel or stainless steel according to the corrosion condition of medium.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114015468A (en) * | 2021-11-30 | 2022-02-08 | 宝钢化工湛江有限公司 | Method and system for producing modified asphalt and carbon black oil from coal tar |
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