CN106367110A - Energy-saving tar processing technology - Google Patents
Energy-saving tar processing technology Download PDFInfo
- Publication number
- CN106367110A CN106367110A CN201610903037.4A CN201610903037A CN106367110A CN 106367110 A CN106367110 A CN 106367110A CN 201610903037 A CN201610903037 A CN 201610903037A CN 106367110 A CN106367110 A CN 106367110A
- Authority
- CN
- China
- Prior art keywords
- tar
- oil
- tower
- heat exchanger
- heat exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/12—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one alkaline treatment step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides an energy-saving tar processing technology. The energy-saving tar processing technology includes: 1), dehydrating and deslagging raw material tar; 2), performing pressurization and heat exchange; 3), performing flash dehydration; 4), performing pressurization, heat exchange and heating on tower-bottom water-free tar; 5), flashing the tower-bottom water-free tar to obtain tower-top oil gas and tower-bottom pitch, and injecting the tower-bottom pitch into a modified-pitch device; 6), injecting the tower-top oil gas in the step 5) into a fractionating tower, and extracting anthracene oil from the bottom of the fractionating tower through automatic flowing; 7), side-extracting three-mix oil from the fractionating tower; 8), performing alkali wash and dephenolization on the three-mix oil; 9), exchanging heat between the three-mix oil and crude naphthalene; 10), performing flashing, and allowing the tower-bottom oil to enter a rectifying tower; 11) extracting the crude naphthalene. The energy-saving tar processing technology has the advantages that processing cost is low, compressive utilization of energy resources is reasonable, and quality of obtained products is high.
Description
Technical field
The present invention relates to tar production field, specifically refer to a kind of energy-saving tar production technique.
Background technology
Under the background that current crude oil price sharp rises, petrochemical materials cost is constantly climbed to a higher point, and petroleum chemicals compete
Power weakens significantly, the arrival of " Waste Era of Oil ", the coalification industry for being chronically at competitive disadvantages provide one very rare
Opportunity to develop.Tar, as one in process of coking important recovery product, is the complex mixture of up to ten thousand kinds an of component,
The single compound about more than 500 therefrom having separated at present and having assert is planted, and accounts for the 55% of tar total amount, including benzene, diformazan
174 kinds of neutral component such as benzene, naphthalene；63 kinds of acidic components such as phenol, cresol and 113 kinds of basic components.A lot of compounds in tar
It is the valuable raw material of plastics, synthetic rubber, pesticide, medicine, exotic material and national defense industry, also some polycyclic hydrocarbon chemical combination
Thing is that petrochemical industry can not produce and substitute.
At present, China's tar is mainly used to processing light oil, carbolic oil, naphtalene oil and modified coal tar pitch etc., then after deep processing
Produce multiple industrial chemicals such as phenol, naphthalene, anthracene, product quantity is numerous, purposes is quite varied.Expert thinks, after the simple processing of tar
Value less, generally have an optimistic view of both at home and abroad is the application of its deep processing purified product.Introduce according to the insiders, both at home and abroad
Tar production technique is similar, is all dehydration, fractional distillation, and the main direction of studying of tar production is to increase product variety, raising
Product quality grade, energy saving and environmental protection.Tar production project belongs to high pollution industry, dangerization industry it is necessary to build
Corresponding environmental protection and safety devices.Both at home and abroad tar production technique needs the main bugbear solving at present is that how to improve tar each
How the separation efficiency of single group, improve the purity of products obtained therefrom and how to improve supporting production technology, carry as much as possible
Take more valuable components, deep processing industrial chain, improve resource utilization.
Although China achieves some achievements in terms of tar production, yet suffer from scientific research strength compared with developed countries
Weak, less investment, existing apparatus small scale, technique fall behind and excessively disperse, deep processing dynamics not, serious environment pollution etc. prominent
Go wrong.Importantly, the potential energy can not make full use of and the energy of all steps turns in most of production system
Change is required for extraneous energy consumption and supports, loss is big, high processing costs, and the comprehensive utilization of the energy is unreasonable, is also a kind of very big simultaneously
The wasting of resources.
Therefore it provides a kind of processing cost is low, reasonably energy-saving tar production technique seems have very much for comprehensive utilization of energy
Necessity, also highly significant.
Content of the invention
Present invention aim to providing a kind of energy-saving tar production technique, its processing cost is low, Integrated Energy is sharp
With reasonable.
For achieving the above object, a kind of energy-saving tar production technique involved in the present invention, comprises the steps:
1) raw tar is carried out being dehydrated de- Slag treatment by ultracentrifuge；
2) by step 1) pressurizeed with one section of tar pump through the raw tar that dehydration takes off after Slag treatment, the raw tar after pressurization
Carry out heat exchange through mixed triolein heat exchanger, carbolineum heat exchanger with mixed triolein, carbolineum respectively；
3) by step 2) raw tar after heat exchange carries out flash-evaporation dehydration process, obtains tower top oil gas and anhydrous Jiao of bottom of towe
Oil；The condensed cooler of tower top oil gas cools down laggard oil water separator and carries out oil-water separation, and light oil enters backflash, and waste water enters waste water
Groove；
4) use two-stage nitration tar pump to step 3) described in bottom of towe anhydrous tar pressurization, then pass through modified coal tar pitch heat exchanger and drip
Blue or green heat exchange, carries out temperature raising heating with tube furnace；
5) flash distillation, obtains tower top oil gas and bottom of towe Colophonium, bottom of towe Colophonium is passed through modified coal tar pitch reactor, modified coal tar pitch is anti-
Answer the oil gas that device top flashes off to be cooled down, upgrading carried out to the Colophonium in modified coal tar pitch reactor, through with tar heat exchange after
Enter pitch storage tank；
6) by step 5) described in tower top oil gas be passed through fractionating column, Fractionator Bottom gravity flow extraction carbolineum, through carbolineum heat exchanger
Enter carbolineum storage tank with being cooled to technological requirement after raw tar heat exchange；
7) enter oil water separator after the tower top oil gas condensed cooler cooling of described fractionating column, light oil enters backflow
Groove, waste water enters wastewater trough, the side take-off mixed triolein of described fractionating column, cools down with raw tar heat exchange through mixed triolein heat exchanger
Enter mixed triolein storage tank afterwards；
8) by step 7) mixed triolein of mixed triolein storage tank is through alkali cleaning dephenolize；
9) by step 8) mixed triolein of alkali cleaning is through crude naphthalene heat exchanger and crude naphthalene heat exchange；
10) flash distillation, enters oil water separator after the cooling of tower top oil gas condensed cooler and carries out oil-water separation, carbolic oil enters back
Chute, waste water is sent to laundry and is washed wastewater trough；Bottom of towe oil is circulated provides heat into heating furnace to primary distillation tower, is partly into rectification
Tower；
11) step 10) described in rectifying column tower top extraction crude naphthalene, described crude naphthalene is through crude naphthalene heat exchanger and raw material three
After contaminated product heat exchange, backflash is entered by blister cooler, flowing full enters crude naphthalene product groove；Bottom of towe washing oil circulates into heating furnace
There is provided heat to rectifying column.
Preferably, step 2) in, after heat exchange, the temperature control of raw tar is 120-150 DEG C.
Further, step 3) in, after flash-evaporation dehydration is processed, the water content control of the bottom of towe anhydrous tar obtaining is
Less than 0.3%.
Further, step 4) in, after tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 395-
410℃.
Further, step 4) in, tube furnace flue gas heat reclaims through residual neat recovering system, and flue gas passes through outside chimney
Row, exhaust gas temperature controls at 120-150 DEG C.
Further, step 5) in, upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: a.
Colophonium in modified coal tar pitch reactor is polymerized 6h at 380-410 DEG C,；B., after being polymerized, the Colophonium in modified coal tar pitch reactor leads to
Cross modified coal tar pitch heat exchanger and step 4) in bottom of towe anhydrous tar heat exchange after pressurization, the Colophonium after modified coal tar pitch heat exchanger
Temperature control is 230-280 DEG C, then the Colophonium after heat exchange is proceeded to cooling shaping in Colophonium cooler.
Further, step 8) in, mixed triolein is controlled to 2-5 time through alkali cleaning dephenolize, the number of times of alkali cleaning dephenolize.
Again further, ultracentrifuge, one section of tar pump, mixed triolein heat exchanger, carbolineum heat exchanger, flash distillation are used
Equipment, modified coal tar pitch heat exchanger, tube furnace, modified coal tar pitch reactor, fractionating column, the control of rectifying column is all by dcs system
Control.
The invention has the beneficial effects as follows: high treating effect of the present invention, environmental protection, system carries out the waste heat of product and raw material
Rational heat exchange design, reduces energy consumption, reduces 20% than same device, year saves 1280 tons of standard coal, Colophonium and tar
Direct heat transfer, year saves 2060 tons of standard coal；Tubular type kiln gas reclaims heat by residual heat system, greatly reduces flue gas temperature
Degree；Simple to operate, product quality is stable, adaptable.Mixed triolein, through 2-5 alkali cleaning dephenolize, reduces alkaline consumption；Crude naphthalene
By with mixed triolein heat exchange, reduce heat consumption；Bottom of towe washing oil circulates provides heat into heating furnace to rectifying column, and heat is basic
Meet needed for system, boiler can disable, reduce fuel consumption；Produce control and adopt computer long-distance control, automatization level is high,
System stability.Environmental protection facility equipment is high, by centralized recovery waste gas, is recycled using washing oil double absorption.Drip
Green grass or young crops, by own technology and technique, can meet the requirement of different clients.Tube furnace flue gas heat is returned through residual neat recovering system
Receive, energy height utilizes.The rational technology of modified coal tar pitch reactor for treatment Colophonium, gained asphalt quality is stable, and ash is low, and three mix
During oily alkali cleaning dephenolize, alkali liquor reasonable mixture ratio, phenol easily removes.
Specific embodiment
The enforcement it is clear that described will be clearly and completely described to the technical scheme in the embodiment of the present invention below
Example is only a part of embodiment of the present invention, rather than whole embodiments.Based on the embodiment in the present invention, this area is common
The every other embodiment that technical staff is obtained under the premise of not making creative work, broadly falls into the model of present invention protection
Enclose.
Embodiment 1
Energy-saving tar production technique, comprises the steps:
1) raw tar is carried out being dehydrated de- Slag treatment by ultracentrifuge；
2) by step 1) pressurizeed with one section of tar pump through the raw tar that dehydration takes off after Slag treatment, the raw tar after pressurization
Carry out heat exchange through mixed triolein heat exchanger, carbolineum heat exchanger with mixed triolein, carbolineum respectively；After heat exchange, the temperature control of raw tar is
120℃.
3) by step 2) raw tar after heat exchange carries out flash-evaporation dehydration process, obtains tower top oil gas and anhydrous Jiao of bottom of towe
Oil；The condensed cooler of tower top oil gas cools down laggard oil water separator and carries out oil-water separation, and light oil enters backflash, and waste water enters waste water
Groove；After flash-evaporation dehydration is processed, the water content control of the bottom of towe anhydrous tar obtaining is less than 0.3%.
4) use two-stage nitration tar pump to step 3) described in bottom of towe anhydrous tar pressurization, then pass through modified coal tar pitch heat exchanger and drip
Blue or green heat exchange, carries out temperature raising heating with tube furnace；After tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 410
℃；Tube furnace flue gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 130 DEG C.
5) flash distillation, obtains tower top oil gas and bottom of towe Colophonium, bottom of towe Colophonium is passed through modified coal tar pitch reactor, modified coal tar pitch is anti-
Answer the oil gas that device top flashes off to enter fractionating column, the Colophonium in modified coal tar pitch reactor is carried out with upgrading, warp and tar heat exchange
Laggard pitch storage tank；Upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: in a. modified coal tar pitch reactor
Colophonium be polymerized 6h at 400 DEG C；B., after being polymerized, the Colophonium in modified coal tar pitch reactor passes through modified coal tar pitch heat exchanger and step
4) the bottom of towe anhydrous tar heat exchange after pressurization in, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 230-250 DEG C, so
Afterwards the Colophonium after heat exchange is proceeded to cooling shaping in Colophonium cooler.
6) by step 5) described in tower top oil gas be passed through fractionating column, Fractionator Bottom gravity flow extraction carbolineum, through carbolineum heat exchanger
Enter carbolineum storage tank with being cooled to technological requirement after raw tar heat exchange；
7) enter oil water separator after the tower top oil gas condensed cooler cooling of described fractionating column, light oil enters backflow
Groove, waste water enters wastewater trough, the side take-off mixed triolein of described fractionating column, cools down with raw tar heat exchange through mixed triolein heat exchanger
Enter mixed triolein storage tank afterwards；
8) by step 7) mixed triolein of mixed triolein storage tank is through alkali cleaning dephenolize；Mixed triolein is through alkali cleaning dephenolize, alkali cleaning dephenolize
Number of times be controlled to 3 times.
9) by step 8) mixed triolein of alkali cleaning is through crude naphthalene heat exchanger and crude naphthalene heat exchange；
10) flash distillation, enters oil water separator after the cooling of tower top oil gas condensed cooler and carries out oil-water separation, carbolic oil enters back
Chute, waste water is sent to laundry and is washed wastewater trough；Bottom of towe oil enters rectifying column；
11) step 10) described in rectifying column tower top extraction crude naphthalene, described crude naphthalene is through crude naphthalene heat exchanger and raw material three
After contaminated product heat exchange, backflash is entered by blister cooler, flowing full enters crude naphthalene product groove；Bottom of towe washing oil circulates into heating furnace
There is provided heat to rectifying column.
Gained asphalt softening point is 98.8 DEG C, and ash is 0.04%.
Embodiment 2
Step 2) in, after heat exchange, the temperature control of raw tar is 140 DEG C.
Step 4) in, after tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 395 DEG C.Tube furnace cigarette
Gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 150 DEG C.
Step 5) in, upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: that a. modified coal tar pitch reacts
Colophonium in device is polymerized 6h at 405 DEG C；B. after being polymerized, Colophonium in modified coal tar pitch reactor pass through modified coal tar pitch heat exchanger with
Step 4) in bottom of towe anhydrous tar heat exchange after pressurization, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 230-250
DEG C, then the Colophonium after heat exchange is proceeded to cooling shaping in Colophonium cooler.
Step 8) in, mixed triolein is controlled to 2 times through alkali cleaning dephenolize, the number of times of alkali cleaning dephenolize.
Other steps of energy-saving tar production technique such as embodiment 1.
Gained asphalt softening point is 96.3 DEG C, and ash is 0.05%.
Embodiment 3
Step 2) in, after heat exchange, the temperature control of raw tar is 150 DEG C.
Step 4) in, after tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 405 DEG C.Tube furnace cigarette
Gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 140 DEG C.
Step 5) in, upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: that a. modified coal tar pitch reacts
Colophonium in device is polymerized 6h at 403 DEG C；B. after being polymerized, Colophonium in modified coal tar pitch reactor pass through modified coal tar pitch heat exchanger with
Step 4) in bottom of towe anhydrous tar heat exchange after pressurization, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 255 DEG C, so
Afterwards the Colophonium after heat exchange is proceeded to and in Colophonium cooler, use mixture of ice and water cooling shaping.
Step 8) in, mixed triolein is controlled to 4 times through alkali cleaning dephenolize, the number of times of alkali cleaning dephenolize.
Other steps of energy-saving tar production technique such as embodiment 1.
Gained asphalt softening point is 97.1 DEG C, and ash is 0.03%.
Embodiment 4
Step 2) in, after heat exchange, the temperature control of raw tar is 135 DEG C.
Step 4) in, after tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 400 DEG C.Tube furnace cigarette
Gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 120 DEG C.
Step 5) in, upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: that a. modified coal tar pitch reacts
Colophonium in device is polymerized 6h at 395 DEG C；B. after being polymerized, Colophonium in modified coal tar pitch reactor pass through modified coal tar pitch heat exchanger with
Step 4) in bottom of towe anhydrous tar heat exchange after pressurization, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 240 DEG C, so
Afterwards the Colophonium after heat exchange is proceeded to cooling shaping in Colophonium cooler.
Step 8) in, mixed triolein is controlled to 5 times through alkali cleaning dephenolize, the number of times of alkali cleaning dephenolize.
Other steps of energy-saving tar production technique such as embodiment 1.
Gained asphalt softening point is 94.3 DEG C, and ash is 0.06%.
Embodiment 5
Step 2) in, after heat exchange, the temperature control of raw tar is 145 DEG C.
Step 4) in, after tube furnace carries out temperature raising heating, the temperature control of bottom of towe anhydrous tar is 405 DEG C.Tube furnace cigarette
Gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 125 DEG C.
Step 5) in, upgrading is carried out to the Colophonium in modified coal tar pitch reactor, comprises the steps: that a. modified coal tar pitch reacts
Colophonium in device is polymerized 6h at 410 DEG C；B. after being polymerized, Colophonium in modified coal tar pitch reactor pass through modified coal tar pitch heat exchanger with
Step 4) in bottom of towe anhydrous tar heat exchange after pressurization, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 250 DEG C, so
Afterwards the Colophonium after heat exchange is proceeded to cooling shaping in Colophonium cooler.
Step 8) in, mixed triolein is controlled to 3 times through alkali cleaning dephenolize, the number of times of alkali cleaning dephenolize.
Other steps of energy-saving tar production technique such as embodiment 1.
Gained asphalt softening point is 99.3 DEG C, and ash is 0.05%.
It is obvious to a person skilled in the art that the invention is not restricted to the details of above-mentioned one exemplary embodiment, Er Qie
In the case of the spirit or essential attributes of the present invention, the present invention can be realized in other specific forms.Therefore, no matter
From the point of view of which point, embodiment all should be regarded as exemplary, and be nonrestrictive, the scope of the present invention is by appended power
Profit requires rather than described above limits, it is intended that all in the implication and scope of the equivalency of claim by falling
Change is included in the present invention.
Moreover, it will be appreciated that although this specification is been described by according to embodiment, not each embodiment only wraps
Containing an independent technical scheme, only for clarity, those skilled in the art should for this narrating mode of description
Using description as an entirety, the technical scheme in each embodiment can also form those skilled in the art through appropriately combined
Understandable other embodiment.
Claims (8)
1. a kind of energy-saving tar production technique is it is characterised in that comprise the steps:
1) raw tar is carried out being dehydrated de- Slag treatment by ultracentrifuge；
2) by step 1) raw tar after the de- Slag treatment of dehydration pressurizes with one section of tar pump, and the raw tar after pressurization is through three
Contaminated product heat exchanger, carbolineum heat exchanger carry out heat exchange with mixed triolein, carbolineum respectively；
3) by step 2) raw tar after heat exchange carries out flash-evaporation dehydration process, obtains tower top oil gas and bottom of towe anhydrous tar；Tower
The top condensed cooler of oil gas cools down laggard oil water separator and carries out oil-water separation, and light oil enters backflash, and waste water enters wastewater trough；
4) use two-stage nitration tar pump to step 3) described in the pressurization of bottom of towe anhydrous tar, then changed by modified coal tar pitch heat exchanger and Colophonium
Heat, carries out temperature raising heating with tube furnace；
5) flash distillation, obtains tower top oil gas and bottom of towe Colophonium, and bottom of towe Colophonium is passed through modified coal tar pitch reactor, modified coal tar pitch reactor
The oil gas that top flashes off enters fractionating column, and the Colophonium in modified coal tar pitch reactor is carried out with upgrading, through laggard with tar heat exchange
Pitch storage tank；
6) by step 5) described in tower top oil gas be passed through fractionating column, Fractionator Bottom gravity flow extraction carbolineum, through carbolineum heat exchanger with former
It is cooled to technological requirement after material tar heat exchange and enter carbolineum storage tank；
7) enter oil water separator after the tower top oil gas condensed cooler cooling of described fractionating column, light oil enters backflash, gives up
Water enters wastewater trough, the side take-off mixed triolein of described fractionating column, cools down laggard through mixed triolein heat exchanger and raw tar heat exchange
Enter mixed triolein storage tank；
8) by step 7) mixed triolein of mixed triolein storage tank is through alkali cleaning dephenolize；
9) by step 8) mixed triolein of alkali cleaning is through crude naphthalene heat exchanger and crude naphthalene heat exchange；
10) flash distillation, enters oil water separator after the cooling of tower top oil gas condensed cooler and carries out oil-water separation, carbolic oil enters backflow
Groove, waste water is sent to laundry and is washed wastewater trough；Bottom of towe oil is circulated provides heat into heating furnace to primary distillation tower, is partly into rectifying column；
11) step 10) described in rectifying column tower top extraction crude naphthalene, described crude naphthalene is through crude naphthalene heat exchanger and raw material mixed triolein
After heat exchange, backflash is entered by blister cooler, flowing full enters crude naphthalene product groove；Bottom of towe washing oil circulates into heating furnace to essence
Evaporating tower provides heat.
2. energy-saving tar production technique according to claim 1 is it is characterised in that described step 2) in, former after heat exchange
The temperature control of material tar is 120-150 DEG C.
3. energy-saving tar production technique according to claim 1 and 2 is it is characterised in that described step 3) in, flash distillation takes off
After water process, the water content control of the bottom of towe anhydrous tar obtaining is less than 0.3%.
4. energy-saving tar production technique according to claim 3 is it is characterised in that described step 4) in, tube furnace enters
After row temperature raising heating, the temperature control of bottom of towe anhydrous tar is 395-410 DEG C.
5. energy-saving tar production technique according to claim 4 is it is characterised in that described step 4) in, tube furnace cigarette
Gas heat reclaims through residual neat recovering system, and flue gas passes through to arrange outside chimney, and exhaust gas temperature controls at 120-150 DEG C.
6. energy-saving tar production technique according to claim 5 is it is characterised in that described step 5) in, to modification drip
Colophonium in blue or green reactor carries out upgrading, comprises the steps: that the Colophonium in a. modified coal tar pitch reactor is poly- at 380-410 DEG C
Close 6h；B., after being polymerized, Colophonium in modified coal tar pitch reactor passes through modified coal tar pitch heat exchanger and step 4) in pressurize after bottom of towe
Anhydrous tar heat exchange, the asphalt temperature after modified coal tar pitch heat exchanger is controlled to 230-280 DEG C, then by the Colophonium after heat exchange
Enter Asphalt tank, the direct entrucking of a part of liquid asphalt is taken out, and is partly into Colophonium former cooling shaping under water.
7. energy-saving tar production technique according to claim 6 is it is characterised in that described step 8) in, mixed triolein warp
Cross alkali cleaning dephenolize, alkali cleaning dephenolize number of times is 2-5 time.
8. energy-saving tar production technique according to claim 7 is it is characterised in that described ultracentrifuge, one section of Jiao
Equipment that oil pump, mixed triolein heat exchanger, carbolineum heat exchanger, flash distillation are used, modified coal tar pitch heat exchanger, tube furnace, modified coal tar pitch
Reactor, fractionating column, the control of rectifying column are all by dcs remotely control.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610903037.4A CN106367110A (en) | 2016-10-17 | 2016-10-17 | Energy-saving tar processing technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610903037.4A CN106367110A (en) | 2016-10-17 | 2016-10-17 | Energy-saving tar processing technology |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106367110A true CN106367110A (en) | 2017-02-01 |
Family
ID=57896434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610903037.4A Pending CN106367110A (en) | 2016-10-17 | 2016-10-17 | Energy-saving tar processing technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106367110A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110776946A (en) * | 2019-10-16 | 2020-02-11 | 宝钢化工湛江有限公司 | Method for recovering naphthalene products |
| CN111334325A (en) * | 2020-03-26 | 2020-06-26 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
| CN111440632A (en) * | 2020-05-21 | 2020-07-24 | 宝舜(河南)新炭材料有限公司 | Production process and system of modified asphalt |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5959787A (en) * | 1982-09-30 | 1984-04-05 | Nippon Steel Chem Co Ltd | Dehydration of coal tar |
| CN101818076A (en) * | 2010-05-07 | 2010-09-01 | 杨东平 | Processing technology for water/ash-containing tar |
| CN103059892A (en) * | 2013-01-25 | 2013-04-24 | 兖矿科蓝煤焦化有限公司 | Tar distillation process for directly producing modified pitch |
| CN103242902A (en) * | 2013-04-25 | 2013-08-14 | 新疆鑫联煤化工有限公司 | Processing method of coal tar |
| CN105154122A (en) * | 2015-07-14 | 2015-12-16 | 陕西双翼石油化工有限责任公司 | Combined coal tar dehydration method |
-
2016
- 2016-10-17 CN CN201610903037.4A patent/CN106367110A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5959787A (en) * | 1982-09-30 | 1984-04-05 | Nippon Steel Chem Co Ltd | Dehydration of coal tar |
| CN101818076A (en) * | 2010-05-07 | 2010-09-01 | 杨东平 | Processing technology for water/ash-containing tar |
| CN103059892A (en) * | 2013-01-25 | 2013-04-24 | 兖矿科蓝煤焦化有限公司 | Tar distillation process for directly producing modified pitch |
| CN103242902A (en) * | 2013-04-25 | 2013-08-14 | 新疆鑫联煤化工有限公司 | Processing method of coal tar |
| CN105154122A (en) * | 2015-07-14 | 2015-12-16 | 陕西双翼石油化工有限责任公司 | Combined coal tar dehydration method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110776946A (en) * | 2019-10-16 | 2020-02-11 | 宝钢化工湛江有限公司 | Method for recovering naphthalene products |
| CN111334325A (en) * | 2020-03-26 | 2020-06-26 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
| CN111334325B (en) * | 2020-03-26 | 2021-12-28 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
| CN111440632A (en) * | 2020-05-21 | 2020-07-24 | 宝舜(河南)新炭材料有限公司 | Production process and system of modified asphalt |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101654305B (en) | Process for changing phenolic nitrate effluent into useful material by extracting, evaporating, crystallizing and coupling | |
| CN106367110A (en) | Energy-saving tar processing technology | |
| CN103242902A (en) | Processing method of coal tar | |
| CN102199070B (en) | Tubular furnace method pressure-reduced debenzolization and distillation process | |
| CN105154144B (en) | A kind of negative pressure benzene removal device and de- benzene method | |
| CN107628923A (en) | A kind of negative pressure benzene removal system and method for rich oil half | |
| CN110015949B (en) | Method for extracting phenolic substances from raw oil containing phenol | |
| CN107032555A (en) | A kind of method for handling oil-containing coal gasification waste water | |
| CN109423318B (en) | Coal tar deep processing technology for directly extracting industrial naphthalene by adding alkali after atmospheric and vacuum distillation | |
| CN206385105U (en) | A kind of coke-stove gas efficiently elutes benzene series system | |
| CN103319300A (en) | Process method for preparing industrial naphthalene through continuous distillation | |
| CN104045506B (en) | Device and process for extracting phenanthrene, fluoranthene and pyrene products in anthracene oil | |
| CN102504852B (en) | Improved Litwin coal tar processing technic | |
| CN212152190U (en) | Coal tar three-tower continuous deep processing system | |
| CN107572483A (en) | Technique that is a kind of while producing carbon disulfide, sulphur and insoluble sulfur | |
| CN203513617U (en) | Chilling device for removing tar from raw gas containing tar | |
| CN214936767U (en) | Energy-conserving blue charcoal sewage treatment system | |
| CN212482152U (en) | Waste water treatment system of crude phenol extraction technology | |
| CN103242131A (en) | Industrial naphthalene distillation process | |
| CN204939338U (en) | A kind of reactive system of coking crude benzene hydrogenation technique | |
| CN201952379U (en) | Continuous refining and separating device of gasified crude phenol | |
| CN204848544U (en) | Blue charcoal waste water utilization process units | |
| CN112694401A (en) | Ethyl acetate production system and production method thereof | |
| CN206219334U (en) | A kind of semi-coke wastewater pretreatment system | |
| CN105418382A (en) | Purification device and purification method for sodium phenolate containing neutral oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170201 |