CN110484289A - A kind of tar negative pressure dewatering system and method - Google Patents
A kind of tar negative pressure dewatering system and method Download PDFInfo
- Publication number
- CN110484289A CN110484289A CN201910901988.1A CN201910901988A CN110484289A CN 110484289 A CN110484289 A CN 110484289A CN 201910901988 A CN201910901988 A CN 201910901988A CN 110484289 A CN110484289 A CN 110484289A
- Authority
- CN
- China
- Prior art keywords
- tar
- entrance
- oil
- anhydrous
- connect
- 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
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/02—Removal of water
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of tar negative pressure dewatering system and methods.The tar negative pressure dewatering system increases vacuum pump set, vacuum buffer tank, oil-washing tank, vacuum cooler on the basis of existing tar normal pressure dewatering system, air-distillation is changed to vacuum distillation, so that operation temperature reduces, ammonia salt is reduced to the extent of corrosion of equipment, saves steam consumption.
Description
Technical field
The present invention relates to dehydration of tar technologies, and in particular to a kind of tar negative pressure dewatering system and method.
Background technique
Common dehydration of tar method has following several: the first is set in tar tank using settled process pre-dehydration is heated
Have steam heater, tar temperature made to be maintained at 80~90 DEG C, stood 36h or more, can make the moisture in tar take off to 2~
3%, but water content cannot be down to 1% or less；Second of utilization batch still thermal dehydration, it is high, seriously polluted etc. scarce that there are energy consumptions
Point；The third is dehydrated using dehydrating tower normal pressure, and the mutual heat exchange between tar and product has the characteristics that consumption reduction, is suitable for big
The tar production enterprise of scale, can make dehydration of tar to 0.5% or less.
Be dehydrated detailed process using dehydrating tower normal pressure: raw tar is delivered to tar preheater, In by pumping from tar tank
It exchanges heat in tar preheater with a part of anhydrous tar from dehydrating tower bottom；Raw tar after preheating with come from dehydrating tower bottom
Another part anhydrous tar enter tar heating device jointly, after being heated to 190~220 DEG C enter dehydrating tower in the middle part of, dehydrating tower
Bottom temp is controlled at 190~220 DEG C or so；Raw tar removes moisture in dehydrating tower, and moisture content is down to 0.8% or less
Anhydrous tar be delivered to tar preheater or tar heating device, it is cold that the anhydrous tar of tar preheater is delivered to anhydrous tar again
But device is cooled to 80~90 DEG C, is finally delivered to anhydrous tar slot.The oil gas at tower dehydration top is cold by light oil condensate cooler
But enter oil water separator afterwards, separate water with edible vegetable oil, water enters phenol sink, and light oil enters light oil backflash；Light oil backflash
In a part of light oil be delivered to dehydrating tower overhead reflux, extra light oil enters light oil slot.Be dehydrated column bottom temperature 190~
220 DEG C or so, a large amount of steam can be expended, while the ammonia salt in tar is decomposed, the hydrogen chloride of generation can be increased to equipment
Corrosion.
Summary of the invention
In order to reduce dehydration of tar operation temperature, reduce equipment extent of corrosion, the present invention provides a kind of tar negative pressure dehydration
System and method.
A kind of tar negative pressure dewatering system provided by the invention, including it is tar preheater, tar heating device, dehydrating tower, light
Oil cooler, oil water separator, light oil backflash, vacuum buffer tank and vacuum pump set, the tar outlet and coke of tar preheater
The entrance of oil heater connects, and the outlet of tar heating device and the entrance in the middle part of dehydrating tower connect；It is dehydrated a nothing of tower bottom
Water tar outlet is connect with the anhydrous tar entrance of tar preheater, is dehydrated the outlet of another anhydrous tar and the tar of tower bottom
The entrance of heater connects；Outlet at the top of dehydrating tower is connect with the gas phase entrance of light oil cooler, the liquid of light oil cooler
Outlet is connect with the entrance of oil water separator, and the light oil outlet of oil water separator is connect with the entrance of light oil backflash, and light oil returns
The outlet of chute and the entrance at the top of dehydrating tower connect；The gaseous phase outlet of light oil cooler and the gas phase entrance of vacuum buffer tank connect
It connects, the gaseous phase outlet of vacuum buffer tank is connect with vacuum pump set, the liquid outlet of vacuum buffer tank and the entrance of light oil backflash
Connection.The system is provided with vacuum buffer tank and vacuum pump set, vacuum pump set can intake-gas so that vacuum buffer tank, light
Negative pressure state is maintained in oil cooler, dehydrating tower.Operation temperature reduces when tar is dehydrated under subnormal ambient in dehydrating tower, ammonia salt
More difficult decomposition.
Further, further include oil-washing tank and vacuum cooler, oil-washing tank is connect with vacuum cooler, vacuum cooler with
Vacuum pump set connection, vacuum pump set are connect with oil-washing tank, are formed into a loop.After washing oil in oil-washing tank is cooled down by vacuum cooler
Into vacuum pump set, after vacuum pump set use, oil-washing tank is entered back into, is formed into a loop.Washing oil is in vacuum pump set and vacuum cooled
It is circulated in device, wherein vacuum cooler cools down washing oil, so that the temperature of washing oil maintains 30~50 DEG C.
It further, further include anhydrous tar cooler, the entrance of anhydrous tar cooler is anhydrous with tar preheater
Tar outlet connection.
Further, vacuum buffer tank, light oil cooler position be above 8~10 meters of oil water separator.
A kind of tar negative pressure dewatering provided by the invention, comprising the following steps:
Negative pressure is generated using vacuum pump set intake-gas, so that maintaining negative pressure state in dehydrating tower；
It is being preheated to tar between 100~120 DEG C in tar preheater；
Tar after making preheating is being heated between 120~130 DEG C in tar heating device；
It is dehydrated the tar for being heated to 120~130 DEG C in dehydrating tower, becoming anhydrous tar after dehydration of tar, (moisture contains
Amount is 120~130 DEG C less than the temperature of dehydration tower bottom 0.8%), is kept；
A part of anhydrous tar is set to be delivered to the heat source in tar preheater as pre- thermal tar；
Another part anhydrous tar is set to be delivered to tar heating device.
Further, the anhydrous tar that is delivered in tar preheater and the anhydrous tar that is delivered in tar heating device
Ratio is 1:6~1:3.
Further, the gas pressure range in dehydrating tower is -30KP~-50KP.
Beneficial effects of the present invention: being transformed former normal pressure dehydrating tower dewatering process, adds after light oil cooler true
Empty unit extracts on-condensible gas, and air-distillation is changed to vacuum distillation, and dehydrating tower forms negative pressure state, so that operation temperature drops
It is low；Heat is not only reduced, steam consumption is saved；And the boiling point of ammonium hydroxide is reduced, reduce corruption of the ammonia salt to equipment
Degree of corrosion；It is obviously improved dehydrating effect simultaneously.
Detailed description of the invention
Fig. 1 is the schematic diagram of tar negative pressure dewatering system of the invention.
Appended drawing reference is explained: 1- light oil cooler, 2- dehydrating tower, 3- tar heating device, 4- tar preheater, the anhydrous coke of 5-
Oil cooler, 6- tar delivery pump, 7- anhydrous tar drawing pump, 8- anhydrous tar circulating pump, 9- light oil reflux pump, 10- light oil
Backflash, 11- oil water separator, 12- vacuum cooler, 13- vacuum pump set, 14- oil-washing tank, 15- vacuum buffer tank.
Specific embodiment
The present invention will be further described with reference to the accompanying drawings and examples.
As shown in Figure 1, a kind of tar negative pressure dewatering system of the invention, including it is tar preheater 4, tar heating device 3, de-
Water tower 2, anhydrous tar cooler 5, light oil cooler 1, oil water separator 11, light oil backflash 10, vacuum buffer tank 15, vacuum
Unit 13, oil-washing tank 14 and vacuum cooler 12.
Wherein, tar preheater 4 is heat exchange equipment, is equipped with tar entrance, tar outlet, anhydrous tar entrance, anhydrous coke
The tar entrance of oil export, tar preheater 4 is connect with tar delivery pump 6 by pipeline.Raw tar is defeated by tar delivery pump 6
It send to tar preheater 4, absorb heat in tar preheater 4 and realizes preheating.
Tar heating device 3 is heating equipment, entrance and exit is equipped with, for heating tar.The entrance of tar heating device 3 with
The tar outlet of tar preheater 4 is connected by pipeline, so that tar is flowed into tar heating device 3 and is heated.
Dehydrating tower 2 is used to remove the moisture in tar, and middle part is equipped with entrance, and top is equipped with entrance and exit, and bottom is equipped with
Two anhydrous tar outlets.The entrance at 2 middle part of dehydrating tower is connect with the outlet of tar heating device 3 by pipeline, and tar is entered
Dehydrating tower 2 is dehydrated.The anhydrous tar outlet of 2 bottom of dehydrating tower is connect with the entrance of tar heating device 3 by pipeline, they
Between pipeline be equipped with anhydrous tar circulating pump 8, recycle a part of anhydrous tar.Another of 2 bottom of dehydrating tower is anhydrous
Tar outlet is connect with the anhydrous tar entrance of tar preheater 4, and the pipeline between them is equipped with anhydrous tar drawing pump 7,
A part of anhydrous tar is set to flow into tar preheater 4 as heat source.
Anhydrous tar cooler 5 is equipped with entrance and exit for cooling down anhydrous tar.The entrance of anhydrous tar cooler 5
It exports with the anhydrous tar of tar preheater 4 and is connect by pipeline, the outlet of anhydrous tar cooler 5 can be stored up with anhydrous tar
Slot is connected by pipeline.
Light oil cooler 1 goes out for the cooling gas come out from dehydrating tower 2 equipped with gas phase entrance, gaseous phase outlet and liquid phase
Mouthful.The gas phase entrance of light oil cooler 1 is connect with the outlet at 2 top of dehydrating tower by pipeline, and the gas in dehydrating tower 2 is flowed into
It is cooled down in light oil cooler 1, a part of liquid is precipitated after gas cooling (main component is light oil and water).
Oil water separator 11 is equipped with entrance, water out and light oil outlet for separating light oil and water.Oil water separator 11
Entrance is connect with the liquid-phase outlet of light oil cooler 1 by pipeline, and the liquid being precipitated in light oil cooler 1 is made to flow into water-oil separating
Device 11 is separated.The water out of oil water separator 11 can be connect with phenol sink by pipeline.
Light oil backflash 10 is equipped with entrance and exit for collecting light oil.The entrance of light oil backflash 10 and water-oil separating
The light oil outlet of device 11 is connected by pipeline.The outlet of light oil backflash 10 is connect with the entrance at 2 top of dehydrating tower by pipeline,
Pipeline between them is equipped with light oil reflux pump 9, is back to a part of light oil in dehydrating tower 2.
Vacuum buffer tank 15 is for gas-liquid separation and keeps negative regulation, goes out equipped with gas phase entrance, gaseous phase outlet and liquid phase
Mouthful.The gas phase entrance of vacuum buffer tank 15 is connect with the gaseous phase outlet of light oil cooler 1 by pipeline, the liquid of vacuum buffer tank 15
Mutually outlet is connect with the entrance of light oil backflash 10 by pipeline.
Vacuum pump set 13 generates negative pressure for intake-gas, goes out equipped with gas phase entrance, gaseous phase outlet, liquid phase entrance and liquid phase
Mouthful.The gas phase entrance of vacuum pump set 13 is connect with the gaseous phase outlet of vacuum buffer tank 15 by pipeline, the gas phase of vacuum pump set 13
Outlet can be connect with emission-control equipment by pipeline.
Oil-washing tank 14 is connected for storing washing oil, the outlet of oil-washing tank 14 and the liquid phase entrance of vacuum pump set 13 by pipeline
It connects, washing oil is allow to flow into vacuum pump set 13.Vacuum cooler 12 is equipped with entrance and exit for cooling down to washing oil.Very
The entrance of empty cooler 12 is connect with the liquid-phase outlet of vacuum pump set 13 by pipeline, the outlet of vacuum cooler 12 and oil-washing tank
14 are connected by pipeline, forming circuit.Temperature can rise washing oil slightly during the work time, and vacuum cooler 12 can make washing oil
Temperature maintain 30~50 DEG C, to ensure that entire washing oil circulatory system heat is stablized.
According to above-mentioned tar negative pressure dewatering system, the dehydration of tar negative pressure may be implemented, the specific steps are as follows:
Start vacuum pump set 13,13 intake-gas of vacuum pump set generates negative pressure, so that vacuum buffer tank 15, light oil cooler
1, negative pressure state is maintained in dehydrating tower 2；
Raw tar through tar delivery pump 6 directly from raw tar slot pumping be delivered to tar preheater 4 preheat, with come from nothing
The anhydrous tar of water tar drawing pump 7 exchanges heat；
Tar after preheating adds into tar with anhydrous tar circulating pump 8 from the anhydrous tar that dehydration tower bottom is extracted out jointly
Hot device 3, is heated to 120~130 DEG C；
Tar after heating enters 2 middle part of dehydrating tower, and column bottom temperature is controlled at 120~130 DEG C or so；
2 top oil gas of dehydrating tower gas phase after light oil condensate cooler 1 is cooling enters vacuum buffer tank 15, and liquid phase enters
Oil water separator 11；Dehydration is conveyed by anhydrous tar drawing pump 7 to 0.8% anhydrous tar a part below and is preheated through tar
Device 4, tar cooler 5 are cooled to 80~90 DEG C, into anhydrous tar pan tank；Another part is defeated by anhydrous tar circulating pump 8
It send to tar heating device 3 and participates in recycling；
For the isolated water of oil water separator 11 from phenol sink is flow to, isolated light oil flowing full enters backflash 10；
A part in backflash 10 is sent through light oil reflux pump 9 to 2 overhead reflux of dehydrating tower, and extra light oil is by reflux
10 flowing full of slot enters light oil pan tank；
The gas phase of vacuum buffer tank 15 enters vacuum pump set 13, and vacuum pump lack of gas send emission-control equipment；
Vacuum pump set 13 makees medium using the washing oil in oil-washing tank 14, with vacuum cooler 12 keep circulating washing oil 30~
Between 50 DEG C.
It follows that the present invention increases vacuum pump set 13 on the basis of existing tar normal pressure dewatering system, vacuum is delayed
Tank 15, oil-washing tank 14, vacuum cooler 12 are rushed, air-distillation is changed to vacuum distillation, so that operation temperature reduces, reduces ammonia
Salt saves steam consumption to the extent of corrosion of equipment.
Claims (7)
1. a kind of tar negative pressure dewatering system, it is characterised in that: cold including tar preheater, tar heating device, dehydrating tower, light oil
But device, oil water separator, light oil backflash, vacuum buffer tank and vacuum pump set, tar outlet and the tar of tar preheater add
The entrance of hot device connects, and the outlet of tar heating device and the entrance in the middle part of dehydrating tower connect；It is dehydrated an anhydrous coke of tower bottom
Oil export is connect with the anhydrous tar entrance of tar preheater, is dehydrated the outlet of another anhydrous tar and the tar heating of tower bottom
The entrance of device connects；Outlet at the top of dehydrating tower is connect with the gas phase entrance of light oil cooler, the liquid outlet of light oil cooler
It is connect with the entrance of oil water separator, the light oil outlet of oil water separator is connect with the entrance of light oil backflash, light oil backflash
Outlet and dehydrating tower at the top of entrance connect；The gaseous phase outlet of light oil cooler and the gas phase entrance of vacuum buffer tank connect,
The gaseous phase outlet of vacuum buffer tank is connect with vacuum pump set, and the liquid outlet of vacuum buffer tank and the entrance of light oil backflash connect
It connects.
2. tar negative pressure dewatering system according to claim 1, it is characterised in that: further include oil-washing tank and vacuum cooled
Device, oil-washing tank are connect with vacuum cooler, and vacuum cooler is connect with vacuum pump set, and vacuum pump set is connect with oil-washing tank, are formed
Circuit.
3. tar negative pressure dewatering system according to claim 1 or 2, it is characterised in that: it further include anhydrous tar cooler,
The entrance of anhydrous tar cooler and the anhydrous tar of tar preheater are exported and are connected.
4. tar negative pressure dewatering system according to claim 3, it is characterised in that: vacuum buffer tank, light oil cooler
Position is above 8~10 meters of oil water separator.
5. a kind of tar negative pressure dewatering, comprising the following steps:
Negative pressure is generated using vacuum pump set intake-gas, so that maintaining negative pressure state in dehydrating tower；
Tar is set to be preheated to 100~110 DEG C in tar preheater；
Tar after making preheating is heated to 120~130 DEG C in tar heating device；
It is dehydrated the tar for being heated to 120~130 DEG C in dehydrating tower, becomes anhydrous tar after dehydration of tar, keep dehydrating tower
The temperature of bottom is 120~130 DEG C；
A part of anhydrous tar is set to be delivered to the heat source in tar preheater as pre- thermal tar；
Another part anhydrous tar is set to be delivered to tar heating device.
6. according to the method described in claim 5, it is characterized by: the anhydrous tar being delivered in tar preheater be delivered to
The ratio of anhydrous tar in tar heating device is between 1:6~1:3.
7. method according to claim 5 or 6, it is characterised in that: gas pressure range in dehydrating tower be -30KP~-
50KP。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910901988.1A CN110484289A (en) | 2019-09-24 | 2019-09-24 | A kind of tar negative pressure dewatering system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910901988.1A CN110484289A (en) | 2019-09-24 | 2019-09-24 | A kind of tar negative pressure dewatering system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110484289A true CN110484289A (en) | 2019-11-22 |
Family
ID=68559129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910901988.1A Pending CN110484289A (en) | 2019-09-24 | 2019-09-24 | A kind of tar negative pressure dewatering system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110484289A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114058402A (en) * | 2021-11-22 | 2022-02-18 | 北京中科诚毅科技发展有限公司 | Dehydration feeding buffer tank, raw oil dehydration process adopting buffer tank and application |
-
2019
- 2019-09-24 CN CN201910901988.1A patent/CN110484289A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114058402A (en) * | 2021-11-22 | 2022-02-18 | 北京中科诚毅科技发展有限公司 | Dehydration feeding buffer tank, raw oil dehydration process adopting buffer tank and application |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102791846B (en) | For the device and method of energy recovery | |
| CN108138053A (en) | The delayed coking unit of combined heat and power | |
| CN102391064B (en) | Process for recovering and refining extracting agent in production procedure of hexanolactam | |
| CN104383704B (en) | A kind of step heating system to the preheating of gas fractionator inlet feed | |
| CN110484289A (en) | A kind of tar negative pressure dewatering system and method | |
| CN102311771B (en) | Crude oil processing method | |
| CN108151547B (en) | Equipment and method for recycling waste heat of raw coke oven gas for benzene removal and ammonia distillation | |
| CN106746118A (en) | A kind of system and method for utilization heat recovery from sewage alcohol ketone | |
| CN108444304A (en) | A kind of waste heat of coke oven crude gas recycling system | |
| CN102443407B (en) | Crude oil deep drawing process method | |
| CN110776947A (en) | Catalytic reforming energy-saving system, energy-saving method and catalytic reforming reaction system | |
| CN102443406B (en) | Crude oil distillation method | |
| CN210595933U (en) | Novel coal tar pitch preparation system | |
| CN210656809U (en) | Tar negative pressure dewatering system | |
| CN212315980U (en) | Trifluorotrichloroethane deacidification device | |
| CN102583395A (en) | Heat pump rectification method for refining trichlorosilane | |
| CN102443408B (en) | Pressure reduction distillation process method | |
| CN205398513U (en) | Heat recovery system in TFE production process | |
| CN205556518U (en) | Economizer of refined system of acetonitrile | |
| CN105462601A (en) | Coal tar distillation and asphalt modification integrated process system | |
| CN206545923U (en) | Waste heat comprehensive utilization system in a kind of process of producing polyformaldehyde | |
| CN106085513B (en) | Coke oven gas liquid film cooling process and device | |
| CN114225652B (en) | Petroleum absorption stabilizing process without supplementary absorbent and petroleum refining equipment | |
| CN104629818B (en) | Vacuum carbonate desulphurization rich solution economic benefits and social benefits desorption technique and system | |
| CN103865565B (en) | A kind of crude oil vacuum distillation method eliminating decompression process bottleneck |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |