CN209307296U - A kind of system that tri-mixed fractions are adopted in tar vacuum distillation - Google Patents
A kind of system that tri-mixed fractions are adopted in tar vacuum distillation Download PDFInfo
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- CN209307296U CN209307296U CN201821955431.3U CN201821955431U CN209307296U CN 209307296 U CN209307296 U CN 209307296U CN 201821955431 U CN201821955431 U CN 201821955431U CN 209307296 U CN209307296 U CN 209307296U
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Abstract
The utility model relates to a kind of tar to be evaporated under reduced pressure the system for adopting tri-mixed fractions, including one section of evaporator, tube furnace and fraction tower；The raw tar entrance of one section of evaporator connects raw tar conveyance conduit through tar-carbolineum heat exchanger；The tower bottom anhydrous tar outlet of one section of evaporator connects fraction tower by tube furnace；Fraction tower side sets tri-mixed fractions extraction mouth and carbolineum extraction mouth, and fraction tower tower bottom sets mid temperature pitch extraction mouth.The utility model is suitable for producing 15~200,000 tons of coal tar processing enterprises per year, the tar distillation technique that phenol naphthalene washes mixed fraction is produced to improve naphthalene concentration degree, process flow is short, easy to operate, low equipment investment, energy conservation and environmental protection.
Description
Technical field
The utility model relates to coal tar processing technology fields more particularly to a kind of vacuum distillation of tar to adopt tri-mixed fractions
System.
Background technique
Currently, the tar distillation technique that generallys use of coal chemical enterprise can be divided into air-distillation, vacuum distillation and often both at home and abroad
It is evaporated under reduced pressure three categories.Wherein:
(1) process flow of air-distillation is used are as follows: enter removing in one section of evaporator after raw tar and carbolineum heat exchange
Water and light oil distillate, after bottom anhydrous tar enters the heating of tube furnace radiant section, into flash evaporator, flash evaporator bottom
Mid temperature pitch is produced, tower top oil and gas enters fraction tower, various fractions are then cut into fraction tower.Fraction, which is cut, both may be used
By narrow fraction, can also be carried out by two mixed fractions, tri-mixed fractions.In order to reduce operation temperature, flash evaporator, fraction tower tower bottom
It is passed through the direct steam of overheat.
Above-mentioned process flow is short, investment is low, control is easy, but be evaporated under reduced pressure and atmospheric and vacuum distillation compared with coal gas consumption compared with
It is high.And the direct steam being passed through becomes phenol wastewater after water-oil separating, increases water pollution.
(2) using the process flow of vacuum distillation are as follows: distillation process is made of dehydration and fraction distillation.Tar is being dehydrated
Moisture and light oil distillate are removed in tower under normal pressure, fraction tower is entered after then anhydrous tar heats in tube furnace and carries out decompression steaming
It evaporates, isolated carbolic oil, naphtalene oil, washing oil, carbolineum fraction, maltha or mid temperature pitch.
In above-mentioned technique, fraction tower operates at reduced pressure conditions, reduces vapo(u)rizing temperature, reduces the coking of tube furnace；
And decompression operation can improve operating environment, be conducive to environmental protection.But since anhydrous tar needs to be separated into single column
Multiple fractions, cut between each fraction not fine enough, and high value added product is caused to be easy to be lost.
(3) be divided to two kinds using the process flow of atmospheric and vacuum distillation, the first is the patented technology of foreign countries: distillation process by
Normal pressure dehydration, normal pressure fore-running and vacuum fractionation composition.Raw material crude tar oil is after raw tar preheating in the dehydrating tower of atmospheric operation
Water in interior abjection tar, and light oil distillate is produced, tower bottom anhydrous tar is sent into pre-distillation column.Initial gross separation is carried out in tower.
Tower bottom obtains mid temperature pitch, and tower top oil and gas enters chilling tower, in chilling tower condensed miscella through plus alkali after be sent into and subtract
Pressure fractionating system.Fractionator overhead produces carbolic oil fraction, and the side line of tower cuts carbolic oil, naphtalene oil, washing oil and a carbolineum fraction respectively,
Tower bottom produces anthracene oil fraction, and heat needed for being fractionated column distillation is provided by tower bottom anthracene oil into tube furnace circulating-heating.The technique
Fraction segmentation is thinner, reduces the Repeat-heating of following process fraction.But complex process, equipment is various, and investment is big.It is main in tar
Fraction is wanted to heat twice during fore-running and vacuum fractionation, gas consumption amount is big.
Second is the burnt resistance to patented technology of middle smelting.Distillation process is divided into three dehydration, air-distillation and vacuum distillation mistakes
Journey.Dehydration carries out under normal pressure, and the separation of lighter component carbolic oil, naphtalene oil is also to carry out under normal pressure in tar, washing oil, carbolineum
Etc. the distillation separation of heavy constituents and pitch be performed under reduced pressure.Raw material crude tar oil passes through and a carbolineum, tar heating furnace cigarette
Enter predehydration after the heat exchange such as gas and preheating, abjection oil and gas enters oil water separator after condensation is cooling；Tower bottom tar enters de-
Water tower.Oil and gas is distillated at the top of dehydrating tower also enters oil water separator after condensation is cooling；Dehydrating tower is recycled by bottom reboiler and is supplied
Heat.Tower bottom tar enters 1# destilling tower.1# destilling tower is atmospheric operation, and tower top adopts carbolic oil, and side line adopts naphtalene oil, and mixing part is sent into 2#
Destilling tower, 2# destilling tower are decompression operation.From tower top to tower bottom, successively produce washing oil, a carbolineum and each fraction of anthracene oil and in
Warm pitch.1# destilling tower, 2# destilling tower are by tube furnace circulation heating.
Three of the above tar distillation technique respectively has feature, and technique (one) and technique (two) are the technologies of domestic contrast maturation.
The first in technique (three) is external patented technology, and once there was the precedent of introduction in the country, and due to complex process, equipment is various, then
In addition the introduction expense of patented technology and capital equipment, engineering is once invested very greatly, and the complexity of technique determines operation
Complexity, execute-in-place difficulty is larger.The second technique kind in technique (three) is suitable for 300,000 tons or more extensive tar and adds
Work and fraction is required to cut thin project.
Summary of the invention
The utility model provides a kind of system that tri-mixed fractions are adopted in tar vacuum distillation, is suitable for producing 15~200,000 tons per year
Coal tar processing enterprise produces the tar distillation technique that phenol naphthalene washes mixed fraction to improve naphthalene concentration degree, and process flow is short, behaviour
Make simple, low equipment investment, energy conservation and environmental protection.
In order to achieve the above object, the utility model is implemented with the following technical solutions:
A kind of system that tri-mixed fractions are adopted in tar vacuum distillation, including one section of evaporator, tube furnace and fraction tower；Described one
The raw tar entrance of section evaporator connects the outlet of tar-carbolineum heat exchanger raw tar, tar-carbolineum heat exchange by pipeline
The raw tar entrance of device connects raw tar conveyance conduit；It is air-cooled that the overhead gas outlet of one section of evaporator passes sequentially through light oil
Device, light oil cooler connect light oil separator；The tower bottom anhydrous tar outlet of one section of evaporator is connected by evaporator column bottoms pump
The anhydrous tar of the anhydrous tar entrance of tube furnace side, the anhydrous tar outlet connection fraction tower lower part of the tube furnace other side enters
Mouthful；The light oil oil and gas outlet of fraction column overhead connects light oil oil-water separation tank, light oil water-oil separating by light oil condensate cooler
The light oil outlet of trench bottom connects the reflux light oil entrance on fraction tower top by light oil reflux line, sets on light oil return pipe light
Oil pump and light oil produce mouth；Incoagulable gas outlet connection external vacuum system at the top of light oil oil-water separation tank, light oil grease
Separation trench bottom sets separation water out；Fraction tower side sets tri-mixed fractions extraction mouth and carbolineum extraction mouth, and tri-mixed fractions produce mouth
Connection tri-mixed fractions send pipeline outside, and tri-mixed fractions, which are sent outside, sets mixed fraction cooler and mixed fraction extraction pump on pipeline；Carbolineum
Extraction mouth connection carbolineum sends pipeline outside, and carbolineum, which is sent outside, sets tar-carbolineum heat exchanger, carbolineum extraction pump and carbolineum cooling on pipeline
Device；Fraction tower tower bottom sets mid temperature pitch extraction mouth, and mid temperature pitch extraction mouth connection mid temperature pitch sends pipeline outside, and mid temperature pitch is sent outside
Fraction tower column bottoms pump is set on pipeline.
The fraction tower is valve tower, and tower body material is stainless steel, inside sets 50~57 blocks of column plates, the 15th~24 block of plate of upper number
Position be tri-mixed fractions produce Board position.
The tube furnace is vertical coil cylindrical furnace, and furnace tube material is stainless steel, and burner selects low nitrogen oxygen burner.
The tar-carbolineum heat exchanger, light oil cooler, mixed fraction cooler, carbolineum cooler are changed using shell-and-tube
Hot device, fixed tube-sheet exchanger, U-shaped pipe heat exchanger or movable tube sheets heat exchanger, the material of heat exchanger are carbon steel or stainless steel.
Compared with prior art, the utility model has the beneficial effects that
1) compared with external Atmospheric vacuum process flow, process flow described in the utility model is short, low equipment investment, control
Simplicity, easily operated, equipment operation, maintenance cost are lower；
2) compared with existing air-distillation technique, dehydration of tar carries out under normal pressure, and distillation carries out under reduced pressure, temperature
Rationally, vacuum distillation reduces operation temperature, and gas consumption amount is low for degree, pressure regime distribution；
3) compared with existing reduced pressure distillation process, dehydration carries out under one section of evaporator, avoids dehydrating tower bottom again
Heat supply is reduced investment outlay；
4) heat-supplying mode of diamond heating is used, convenient for operation and is adjusted；
5) fraction column distillation process is not required to be passed through direct steam, does not generate phenol wastewater；
6) since distillation is to operate under negative pressure, operating environment can be improved, be conducive to environmental protection.
Detailed description of the invention
Fig. 1 is the structural schematic diagram for the system that tri-mixed fractions are adopted in a kind of tar vacuum distillation described in the utility model.
In figure: 1. 1 sections of 5. light oil cooler of evaporator 2. fraction tower, 3. tube furnace, 4. light oil air cooler, 6. light oil
7. light oil condensate cooler of separator, 8. light oil oil-water separation tank, 9. light oil pumps the mixing of 10. mixed fraction coolers 11. and evaporates
Divide extraction pump 12. tar-carbolineum heat exchanger, 13. 14. evaporator column bottoms pump of fraction tower column bottoms pump, 15. carbolineum extraction pump 16.
Carbolineum cooler
Specific embodiment
Specific embodiment of the present utility model is described further with reference to the accompanying drawing:
As shown in Figure 1, a kind of tar described in the utility model is evaporated under reduced pressure the system for adopting tri-mixed fractions, including one section of evaporation
Device 1, tube furnace 3 and fraction tower 2；The raw tar entrance of one section of evaporator 1 connects tar-carbolineum heat exchanger by pipeline
12 raw tar outlet, tar-carbolineum heat exchanger 12 raw tar entrance connect raw tar conveyance conduit；One section of evaporation
The overhead gas outlet of device 1 passes sequentially through light oil air cooler 4, light oil cooler 5 connects light oil separator 6；One section of evaporator 1
Tower bottom anhydrous tar exports the anhydrous tar entrance for connecting 14 take-over type furnace, 3 side by evaporator column bottoms pump, 3 other side of tube furnace
Anhydrous tar outlet connection 2 lower part of fraction tower anhydrous tar entrance；The light oil oil and gas outlet of 2 tower top of fraction tower passes through light oil
Condensate cooler 7 connects light oil oil-water separation tank 8, and the light oil outlet of 8 bottom of light oil oil-water separation tank passes through light oil reflux line
The reflux light oil entrance on 2 top of fraction tower is connected, light oil pump 9 and light oil extraction mouth are set on light oil return pipe；Light oil water-oil separating
The incoagulable gas outlet connection external vacuum system at 8 top of slot, 8 bottom of light oil oil-water separation tank sets separation water out；Fraction
2 side of tower sets tri-mixed fractions extraction mouth and carbolineum extraction mouth, and tri-mixed fractions extraction mouth connection tri-mixed fractions send pipeline outside, and three mixed evaporate
It exceptionally send and sets mixed fraction cooler 10 and mixed fraction extraction pump 11 on pipeline；Carbolineum extraction mouth connection carbolineum sends pipeline outside,
Carbolineum, which is sent outside, sets tar-carbolineum heat exchanger 12, carbolineum extraction pump 15 and carbolineum cooler 16 on pipeline；During 2 tower bottom of fraction tower is set
Warm pitch produces mouth, and mid temperature pitch extraction mouth connection mid temperature pitch sends pipeline outside, and mid temperature pitch, which is sent outside, sets fraction tower tower on pipeline
Bottom pump 13.
The fraction tower 2 is valve tower, and tower body material is stainless steel, inside sets 50~57 blocks of column plates, the 15th~24 piece of upper number
The position of plate is that tri-mixed fractions produce Board position.
The tube furnace 3 is vertical coil cylindrical furnace, and furnace tube material is stainless steel, and burner selects low nitrogen oxygen burner.
The tar-carbolineum heat exchanger 12, light oil cooler 5, mixed fraction cooler 10, carbolineum cooler 16 are using pipe
Shell heat exchanger, fixed tube-sheet exchanger, U-shaped pipe heat exchanger or movable tube sheets heat exchanger, the material of heat exchanger be carbon steel or
Stainless steel.
The technique of tri-mixed fractions is adopted in a kind of tar vacuum distillation, and raw tar enters one section of evaporator 1, takes off under condition of normal pressure
The boiled tar of moisture removal and light oil fraction, tower bottom send fraction tower 2 after the heating of tube furnace 3, at reduced pressure conditions, from fraction tower
2 overhead extraction light oil distillates, side line cut tri-mixed fractions, carbolineum fraction, produce mid temperature pitch from 2 tower bottom of fraction tower；Fraction tower 2
Heat provided by the boiled tar after heated in tube furnace 3.
A kind of technical process of system that tri-mixed fractions are adopted in tar vacuum distillation described in the utility model is as follows:
1) after raw tar initially enters tar-carbolineum heat exchanger 12 and the heat exchange of carbolineum fraction, into one section of evaporator 1；
One section of 1 tower top temperature of evaporator is 100~110 DEG C, and the light oil distillate and water of tower top evolution are first cooled to 50 through light oil air cooler 4
~60 DEG C, then 40~45 DEG C are cooled to through light oil cooler 5, the light oil most isolated afterwards through light oil separator 6 flows into light oil slot；
2) anhydrous tar of one section of 1 tower bottom of evaporator is heated via the radiant section that evaporator column bottoms pump 14 is sent into tube furnace 3
Enter fraction tower 2 after to 370~400 DEG C, fraction tower 2 uses decompression operation, and absolute pressure of top of the tower is 40~50kPa, tower top temperature
Degree is 70~80 DEG C, and column bottom temperature is 330~360 DEG C；It is cold in light oil condensate cooler 7 from the light oil oil and gas of overhead extraction
It is solidifying, then after light oil oil-water separation tank 8 isolates moisture, a part is used as and is recirculated back to 2 tower top of fraction tower, another part conduct
Intermediate products extraction, into light oil slot；The water isolated in light oil oil-water separation tank 8 flows into ammonia vessel；
3) tri-mixed fractions, carbolineum fraction are cut respectively from 2 side line of fraction tower；Tower exit temperature is 190~200 DEG C and three mixed evaporates
Point enter mixed fraction cooler 10, using circulating water to 70~80 DEG C, then with mixed fraction extraction pump 11 extraction, send to
The storage of mixed fraction slot, is periodically pumped to subsequent production unit；Tower exit temperature is that 280~300 DEG C of carbolineum fraction enters tar-
Carbolineum heat exchanger 12 and raw tar exchange heat, and the carbolineum fraction after heat exchange is produced in 15 feeding carbolineum cooler 16 of pump with carbolineum and used
Circulating water is to 70~80 DEG C, then send to carbolineum slot and store, and is periodically pumped to oil depot；
4) it is extracted out, is sent to subsequent production unit by fraction tower column bottoms pump 13 from the mid temperature pitch that 2 tower bottom of fraction tower produces；It evaporates
The incoagulable gas of 2 tower top of tower is divided to enter vacuum system.
The light oil reflux ratio of 2 tower top of fraction tower is light oil: anhydrous tar=0.4~0.7.
The preferable specific embodiment of the above, only the utility model, but the protection scope of the utility model is not
It is confined to this, anyone skilled in the art is within the technical scope disclosed by the utility model, practical according to this
Novel technical solution and its utility model design are subject to equivalent substitution or change, should all cover the protection model in the utility model
Within enclosing.
Claims (4)
1. a kind of tar is evaporated under reduced pressure the system for adopting tri-mixed fractions, including one section of evaporator, tube furnace and fraction tower；Its feature exists
In the raw tar entrance of one section of evaporator connects the outlet of tar-carbolineum heat exchanger raw tar by pipeline, burnt
Oil-carbolineum heat exchanger raw tar entrance connects raw tar conveyance conduit；The overhead gas outlet of one section of evaporator is successively
Light oil separator is connected by light oil air cooler, light oil cooler；The tower bottom anhydrous tar outlet of one section of evaporator passes through evaporation
Device column bottoms pump connects the anhydrous tar entrance of tube furnace side, the anhydrous tar outlet connection fraction tower lower part of the tube furnace other side
Anhydrous tar entrance；The light oil oil and gas outlet of fraction column overhead connects light oil oil-water separation tank by light oil condensate cooler,
The light oil outlet of light oil water-oil separating trench bottom connects the reflux light oil entrance on fraction tower top, light oil by light oil reflux line
Light oil pump and light oil extraction mouth are set on return pipe；Incoagulable gas outlet connection external vacuum system at the top of light oil oil-water separation tank
System, light oil water-oil separating trench bottom set separation water out；Fraction tower side sets tri-mixed fractions extraction mouth and carbolineum extraction mouth, and three is mixed
Fraction extraction mouth connection tri-mixed fractions send pipeline outside, and tri-mixed fractions, which are sent outside, sets mixed fraction cooler and mixed fraction is adopted on pipeline
It pumps out；Carbolineum extraction mouth connection carbolineum sends pipeline outside, carbolineum send outside set on pipeline tar-carbolineum heat exchanger, carbolineum extraction pump and
Carbolineum cooler；Fraction tower tower bottom sets mid temperature pitch extraction mouth, and mid temperature pitch extraction mouth connection mid temperature pitch sends pipeline, medium temperature outside
Pitch, which is sent outside, sets fraction tower column bottoms pump on pipeline.
2. a kind of tar according to claim 1 is evaporated under reduced pressure the system for adopting tri-mixed fractions, which is characterized in that the fraction
Tower is valve tower, and tower body material is stainless steel, inside sets 50~57 blocks of column plates, and the position of upper the 15th~24 block of plate of number is tri-mixed fractions
Produce Board position.
3. a kind of tar according to claim 1 is evaporated under reduced pressure the system for adopting tri-mixed fractions, which is characterized in that the tubular type
Furnace is vertical coil cylindrical furnace, and furnace tube material is stainless steel, and burner selects low nitrogen oxygen burner.
4. a kind of tar according to claim 1 is evaporated under reduced pressure the system for adopting tri-mixed fractions, which is characterized in that the coke
Oil-carbolineum heat exchanger, light oil cooler, mixed fraction cooler, carbolineum cooler use shell-and-tube heat exchanger, fixed tube sheet type
Heat exchanger, U-shaped pipe heat exchanger or movable tube sheets heat exchanger, the material of heat exchanger are carbon steel or stainless steel.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821955431.3U CN209307296U (en) | 2018-11-26 | 2018-11-26 | A kind of system that tri-mixed fractions are adopted in tar vacuum distillation |
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| CN201821955431.3U CN209307296U (en) | 2018-11-26 | 2018-11-26 | A kind of system that tri-mixed fractions are adopted in tar vacuum distillation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355083A (en) * | 2018-11-26 | 2019-02-19 | 中冶焦耐(大连)工程技术有限公司 | The technique and system of tri-mixed fractions are adopted in a kind of tar vacuum distillation |
-
2018
- 2018-11-26 CN CN201821955431.3U patent/CN209307296U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355083A (en) * | 2018-11-26 | 2019-02-19 | 中冶焦耐(大连)工程技术有限公司 | The technique and system of tri-mixed fractions are adopted in a kind of tar vacuum distillation |
| CN109355083B (en) * | 2018-11-26 | 2024-05-14 | 中冶焦耐(大连)工程技术有限公司 | Process and system for extracting three-mixed fraction by reduced pressure distillation of tar |
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