CN210656809U - Tar negative pressure dewatering system - Google Patents
Tar negative pressure dewatering system Download PDFInfo
- Publication number
- CN210656809U CN210656809U CN201921587424.7U CN201921587424U CN210656809U CN 210656809 U CN210656809 U CN 210656809U CN 201921587424 U CN201921587424 U CN 201921587424U CN 210656809 U CN210656809 U CN 210656809U
- Authority
- CN
- China
- Prior art keywords
- tar
- outlet
- inlet
- cooler
- light oil
- 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.)
- Active
Links
Images
Abstract
The utility model provides a tar negative pressure dewatering system. This tar negative pressure dewatering system has increased vacuum unit, vacuum buffer tank, wash tank, vacuum cooler on current tar ordinary pressure dewatering system's basis, changes the ordinary pressure distillation into the negative pressure distillation for operating temperature reduces, has reduced the degree of corrosion of ammonia salt to equipment, has saved the steam consumption.
Description
Technical Field
The utility model relates to a tar dehydration technique, concretely relates to tar negative pressure dewatering system.
Background
The following methods are common for dehydrating tar: the first method adopts a heating standing method for pre-dehydration, a steam heater is arranged in a tar storage tank to keep the temperature of tar at 80-90 ℃, and the water content in the tar can be dehydrated to 2-3% but can not be reduced to below 1% after standing for more than 36 hours; the second method utilizes an intermittent kettle to heat and dehydrate, and has the defects of high energy consumption, serious pollution and the like; and the third method utilizes the dehydration tower to dehydrate under normal pressure, and the mutual heat exchange between the tar and the product is realized, so that the method has the characteristic of consumption reduction, is suitable for large-scale tar processing enterprises, and can dehydrate the tar to below 0.5 percent.
The specific process of normal pressure dehydration by using a dehydration tower comprises the following steps: conveying the raw material tar from a tar storage tank to a tar preheater by a pump, and exchanging heat with a part of anhydrous tar from the bottom of the dehydration tower in the tar preheater; the preheated raw material tar and the other part of anhydrous tar from the bottom of the dehydration tower enter a tar heater together, are heated to 190-220 ℃ and then enter the middle part of the dehydration tower, and the temperature of the bottom of the dehydration tower is controlled to be about 190-220 ℃; and (3) dehydrating the raw material tar in a dehydration tower, conveying the anhydrous tar with the moisture content reduced to be less than 0.8% to a tar preheater or a tar heater, conveying the anhydrous tar of the tar preheater to an anhydrous tar cooler, cooling to 80-90 ℃, and finally conveying to an anhydrous tar tank. Cooling the oil gas at the top of the tower dehydration by a light oil condensing cooler, then feeding the oil gas into an oil-water separator to separate water from clean oil, feeding the water into a phenol water tank, and feeding the light oil into a light oil reflux tank; and conveying a part of light oil in the light oil reflux tank to the top of the dehydration tower for reflux, and introducing redundant light oil into a light oil tank. The temperature at the bottom of the dehydration tower is about 190-220 ℃, a large amount of steam can be consumed, meanwhile, ammonia salt in tar is decomposed, and the generated hydrogen chloride can increase the corrosion to equipment.
Disclosure of Invention
In order to reduce the tar dehydration operation temperature and reduce the corrosion degree of equipment, the utility model provides a tar negative pressure dehydration system.
The utility model provides a tar negative pressure dehydration system, which comprises a tar preheater, a tar heater, a dehydration tower, a light oil cooler, an oil-water separator, a light oil reflux tank, a vacuum buffer tank and a vacuum unit, wherein the tar outlet of the tar preheater is connected with the inlet of the tar heater, and the outlet of the tar heater is connected with the inlet in the middle of the dehydration tower; one anhydrous tar outlet at the bottom of the dehydration tower is connected with an anhydrous tar inlet of the tar preheater, and the other anhydrous tar outlet at the bottom of the dehydration tower is connected with an inlet of the tar heater; the outlet of the top of the dehydration tower is connected with the gas phase inlet of the light oil cooler, the liquid outlet of the light oil cooler is connected with the inlet of the oil-water separator, the light oil outlet of the oil-water separator is connected with the inlet of the light oil reflux tank, and the outlet of the light oil reflux tank is connected with the inlet of the top of the dehydration tower; the gas phase outlet of the light oil cooler is connected with the gas phase inlet of the vacuum buffer tank, the gas phase outlet of the vacuum buffer tank is connected with the vacuum unit, and the liquid outlet of the vacuum buffer tank is connected with the inlet of the light oil reflux tank. The system is provided with a vacuum buffer tank and a vacuum unit, and the vacuum unit can suck gas, so that a negative pressure state is maintained in the vacuum buffer tank, the light oil cooler and the dehydration tower. The operation temperature of tar is reduced when dehydration is carried out in the dehydration tower under the negative pressure environment, and the ammonia salt is not easy to decompose.
Furthermore, the device also comprises a wash oil tank and a vacuum cooler, wherein the wash oil tank is connected with the vacuum cooler, the vacuum cooler is connected with a vacuum unit, and the vacuum unit is connected with the wash oil tank to form a loop. The washing oil in the washing oil tank is cooled by a vacuum cooler and then enters a vacuum unit, and then enters the washing oil tank after being used by the vacuum unit to form a loop. The washing oil circularly flows in the vacuum unit and the vacuum cooler, wherein the vacuum cooler cools the washing oil, so that the temperature of the washing oil is maintained at 30-50 ℃.
Furthermore, the system also comprises an anhydrous tar cooler, and the inlet of the anhydrous tar cooler is connected with the anhydrous tar outlet of the tar preheater.
Furthermore, the positions of the vacuum buffer tank and the light oil cooler are 8-10 meters higher than the oil-water separator.
The method for dehydrating by using the tar negative pressure dehydration system comprises the following steps:
utilizing a vacuum unit to suck gas to generate negative pressure so as to maintain the negative pressure state in the dehydration tower, wherein the gas pressure range in the dehydration tower is-30 KP to-50 KP;
preheating tar in a tar preheater to 100-120 ℃;
heating the preheated tar in a tar heater to 120-130 ℃;
dehydrating tar heated to 120-130 ℃ in a dehydrating tower to obtain anhydrous tar (the water content is less than 0.8%), and keeping the temperature at the bottom of the dehydrating tower at 120-130 ℃;
conveying a part of the anhydrous tar to a tar preheater to be used as a heat source for preheating the tar;
and conveying the other part of the anhydrous tar to a tar heater, wherein the ratio of the anhydrous tar conveyed to the tar preheater to the anhydrous tar conveyed to the tar heater is 1: 6-1: 3.
The utility model has the advantages that: the original dehydration process of the atmospheric dehydration tower is modified, a vacuum unit is additionally arranged behind a light oil cooler to extract non-condensable gas, atmospheric distillation is changed into negative pressure distillation, and the dehydration tower is in a negative pressure state, so that the operation temperature is reduced; not only reducing heat, saving steam consumption; the boiling point of the ammonia water is reduced, and the corrosion degree of the ammonia salt to equipment is reduced; and meanwhile, the dehydration effect is obviously improved.
Drawings
FIG. 1 is a schematic view of the tar negative pressure dewatering system of the present invention.
The reference signs explain: 1-light oil cooler, 2-dehydration tower, 3-tar heater, 4-tar preheater, 5-anhydrous tar cooler, 6-tar delivery pump, 7-anhydrous tar extraction pump, 8-anhydrous tar circulating pump, 9-light oil reflux pump, 10-light oil reflux tank, 11-oil-water separator, 12-vacuum cooler, 13-vacuum unit, 14-wash tank and 15-vacuum buffer tank.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
As shown in fig. 1, the tar negative pressure dewatering system of the present invention includes a tar preheater 4, a tar heater 3, a dewatering tower 2, an anhydrous tar cooler 5, a light oil cooler 1, an oil-water separator 11, a light oil reflux tank 10, a vacuum buffer tank 15, a vacuum unit 13, a wash oil tank 14, and a vacuum cooler 12.
Wherein, the tar preheater 4 is a heat exchange device and is provided with a tar inlet, a tar outlet, an anhydrous tar inlet and an anhydrous tar outlet, and the tar inlet of the tar preheater 4 is connected with the tar delivery pump 6 through a pipeline. The raw material tar is conveyed into the tar preheater 4 by the tar conveying pump 6, and the heat is absorbed in the tar preheater 4 to realize preheating.
The tar heater 3 is a heating device provided with an inlet and an outlet for heating tar. The inlet of the tar heater 3 is connected with the tar outlet of the tar preheater 4 through a pipeline, so that the tar flows into the tar heater 3 for heating.
The dehydration tower 2 is used for removing moisture in tar, the middle part is provided with an inlet, the top is provided with an inlet and an outlet, and the bottom is provided with two anhydrous tar outlets. The inlet at the middle part of the dehydration tower 2 is connected with the outlet of the tar heater 3 through a pipeline, so that tar enters the dehydration tower 2 for dehydration. An anhydrous tar outlet at the bottom of the dehydration tower 2 is connected with an inlet of the tar heater 3 through a pipeline, and an anhydrous tar circulating pump 8 is arranged on the pipeline between the anhydrous tar outlet and the tar heater to circulate part of the anhydrous tar. The other anhydrous tar outlet at the bottom of the dehydration tower 2 is connected with the anhydrous tar inlet of the tar preheater 4, and an anhydrous tar extraction pump 7 is arranged on a pipeline between the anhydrous tar outlet and the tar preheater 4, so that part of the anhydrous tar flows into the tar preheater 4 to be used as a heat source.
The anhydrous tar cooler 5 is used for cooling the anhydrous tar and is provided with an inlet and an outlet. The inlet of the anhydrous tar cooler 5 is connected with the anhydrous tar outlet of the tar preheater 4 through a pipeline, and the outlet of the anhydrous tar cooler 5 can be connected with the anhydrous tar storage tank through a pipeline.
The light oil cooler 1 is used for cooling the gas coming out of the dehydration tower 2 and is provided with a gas phase inlet, a gas phase outlet and a liquid phase outlet. The gas phase inlet of the light oil cooler 1 is connected with the outlet at the top of the dehydration tower 2 through a pipeline, so that the gas in the dehydration tower 2 flows into the light oil cooler 1 for cooling, and a part of liquid (mainly comprising light oil and water) is separated out after the gas is cooled.
The oil-water separator 11 is used for separating light oil and water, and is provided with an inlet, a water outlet and a light oil outlet. An inlet of the oil-water separator 11 is connected to a liquid phase outlet of the light oil cooler 1 via a pipe, and the liquid precipitated in the light oil cooler 1 is separated by flowing into the oil-water separator 11. The water outlet of the oil-water separator 11 can be connected with the phenol water tank through a pipeline.
The light oil reflux tank 10 is used for collecting light oil, and is provided with an inlet and an outlet. An inlet of the light oil reflux tank 10 is connected to a light oil outlet of the oil-water separator 11 through a pipe. The outlet of the light oil reflux tank 10 is connected to the inlet at the top of the dehydration tower 2 through a pipe, and a light oil reflux pump 9 is provided on the pipe between them to reflux a part of the light oil to the dehydration tower 2.
The vacuum buffer tank 15 is used for gas-liquid separation and stable negative pressure maintaining, and is provided with a gas phase inlet, a gas phase outlet and a liquid phase outlet. A gas phase inlet of the vacuum buffer tank 15 is connected to a gas phase outlet of the light oil cooler 1 through a pipe, and a liquid phase outlet of the vacuum buffer tank 15 is connected to an inlet of the light oil reflux tank 10 through a pipe.
The vacuum unit 13 is used for sucking gas to generate negative pressure and is provided with a gas phase inlet, a gas phase outlet, a liquid phase inlet and a liquid phase outlet. The gas phase inlet of the vacuum unit 13 is connected with the gas phase outlet of the vacuum buffer tank 15 through a pipeline, and the gas phase outlet of the vacuum unit 13 can be connected with an exhaust gas treatment device through a pipeline.
The wash oil tank 14 is used for storing wash oil, and an outlet of the wash oil tank 14 is connected with a liquid phase inlet of the vacuum unit 13 through a pipeline, so that the wash oil can flow into the vacuum unit 13. The vacuum cooler 12 is used for cooling the wash oil and is provided with an inlet and an outlet. The inlet of the vacuum cooler 12 is connected to the liquid phase outlet of the vacuum unit 13 through a pipe, and the outlet of the vacuum cooler 12 is connected to the oil washing tank 14 through a pipe to form a loop. The temperature of the washing oil rises slightly in the working process, and the vacuum cooler 12 can maintain the temperature of the washing oil at 30-50 ℃, so that the heat stability of the whole washing oil circulating system is guaranteed.
According to the tar negative pressure dehydration system, tar negative pressure dehydration can be realized, and the method comprises the following specific steps:
starting the vacuum unit 13, and the vacuum unit 13 sucks gas to generate negative pressure so as to maintain the negative pressure state in the vacuum buffer tank 15, the light oil cooler 1 and the dehydration tower 2;
the raw material tar is directly pumped and conveyed from a raw material tar tank to a tar preheater 4 through a tar conveying pump 6 for preheating, and exchanges heat with the anhydrous tar from an anhydrous tar pumping pump 7;
the preheated tar and the anhydrous tar pumped out from the bottom of the dehydration tower by the anhydrous tar circulating pump 8 enter the tar heater 3 together, and are heated to 120-130 ℃;
the heated tar enters the middle part of a dehydration tower 2, and the temperature of the tower bottom is controlled to be about 120-130 ℃;
the oil gas at the top of the dehydration tower 2 is cooled by the light oil condensing cooler 1, the gas phase enters the vacuum buffer tank 15, and the liquid phase enters the oil-water separator 11; conveying a part of anhydrous tar with the dehydration content of less than 0.8% by an anhydrous tar extraction pump 7, cooling the part of the anhydrous tar to 80-90 ℃ by a tar preheater 4 and a tar cooler 5, and feeding the part of the anhydrous tar into an anhydrous tar finished product tank; the other part is conveyed to the tar heater 3 by an anhydrous tar circulating pump 8 to participate in circulation;
the water separated by the oil-water separator 11 automatically flows to the phenol water tank, and the separated light oil fully flows into the reflux tank 10;
a part of the inside of the reflux tank 10 is sent to the top of the dehydration tower 2 through a light oil reflux pump 9 for reflux, and the redundant light oil flows into a light oil finished product tank through the reflux tank 10;
the gas phase of the vacuum buffer tank 15 enters a vacuum unit 13, and the exhaust gas of the vacuum pump is sent to a waste gas treatment device;
the vacuum unit 13 adopts wash oil in a wash oil tank 14 as a medium, and a vacuum cooler 12 is used for keeping the circulating wash oil at 30-50 ℃.
Therefore, the utility model discloses increased vacuum unit 13, vacuum buffer tank 15, wash tank 14, vacuum cooler 12 on current tar ordinary pressure dewatering system's basis, changed the atmospheric distillation into the negative pressure distillation for operating temperature reduces, has reduced the degree of corrosion of ammonia salt to equipment, has saved the steam consumption.
Claims (4)
1. A tar negative pressure dewatering system is characterized in that: the device comprises a tar preheater, a tar heater, a dehydration tower, a light oil cooler, an oil-water separator, a light oil reflux tank, a vacuum buffer tank and a vacuum unit, wherein a tar outlet of the tar preheater is connected with an inlet of the tar heater, and an outlet of the tar heater is connected with an inlet in the middle of the dehydration tower; one anhydrous tar outlet at the bottom of the dehydration tower is connected with an anhydrous tar inlet of the tar preheater, and the other anhydrous tar outlet at the bottom of the dehydration tower is connected with an inlet of the tar heater; the outlet of the top of the dehydration tower is connected with the gas phase inlet of the light oil cooler, the liquid outlet of the light oil cooler is connected with the inlet of the oil-water separator, the light oil outlet of the oil-water separator is connected with the inlet of the light oil reflux tank, and the outlet of the light oil reflux tank is connected with the inlet of the top of the dehydration tower; the gas phase outlet of the light oil cooler is connected with the gas phase inlet of the vacuum buffer tank, the gas phase outlet of the vacuum buffer tank is connected with the vacuum unit, and the liquid outlet of the vacuum buffer tank is connected with the inlet of the light oil reflux tank.
2. The negative tar dewatering system of claim 1, further comprising: the washing oil tank is connected with the vacuum cooler, the vacuum cooler is connected with the vacuum unit, and the vacuum unit is connected with the washing oil tank to form a loop.
3. The tar negative pressure dewatering system according to claim 1 or 2, characterized in that: the device also comprises an anhydrous tar cooler, wherein the inlet of the anhydrous tar cooler is connected with the anhydrous tar outlet of the tar preheater.
4. The negative tar dewatering system of claim 3, further comprising: the positions of the vacuum buffer tank and the light oil cooler are 8-10 meters higher than the oil-water separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921587424.7U CN210656809U (en) | 2019-09-24 | 2019-09-24 | Tar negative pressure dewatering system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921587424.7U CN210656809U (en) | 2019-09-24 | 2019-09-24 | Tar negative pressure dewatering system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210656809U true CN210656809U (en) | 2020-06-02 |
Family
ID=70839673
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921587424.7U Active CN210656809U (en) | 2019-09-24 | 2019-09-24 | Tar negative pressure dewatering system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210656809U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
-
2019
- 2019-09-24 CN CN201921587424.7U patent/CN210656809U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
| CN114292659B (en) * | 2022-01-25 | 2023-09-01 | 枣庄杰富意振兴化工有限公司 | Deep processing method of coal tar |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103265089A (en) | High temperature high efficiency multi-effect seawater distillation desalination apparatus and method | |
| CN104926675A (en) | Recovery process of low concentration dimethylacetamide | |
| CN210656809U (en) | Tar negative pressure dewatering system | |
| CN204224499U (en) | A kind of film produces the device that in waste liquid, N,N-DIMETHYLACETAMIDE reclaims | |
| CN201660611U (en) | Semi-coke gas purification tar recovery device | |
| CN113813623A (en) | MVR concentration and rectification system and recovery method of DMAC waste liquid | |
| CN204874161U (en) | Device of ammonia nitrogen in filtration liquid is got rid of to negative pressure ammonia still process method | |
| CN204891253U (en) | Evaporative concentration system of emulsion | |
| CN102583861B (en) | Method for preheating inflow water of membrane method seawater softening device | |
| CN104844414A (en) | Equipment and process for recovering glyphosate solvent during production with glycine method | |
| CN108251144B (en) | Process and system for realizing final dehydration of tar by recycling waste heat of heat pump unit | |
| CN206108988U (en) | Utilize water treatment facilities of power plant's waste heat | |
| CN108654127A (en) | A kind of steam condensate recovery system | |
| CN104477955B (en) | Live steam condensed water cooling in a kind of alumina producing and heat recovery method | |
| CN204417451U (en) | The full-automatic regeneration treatment system of energy-saving waste lubricating oil | |
| CN203770068U (en) | Vacuum-pumping system of water ring | |
| CN103342733A (en) | Extraction method for protein in juice | |
| CN210506153U (en) | Waste heat recovery and utilization system of PTA refining unit mother liquor | |
| CN102839056A (en) | Stepped recovery and purification method and device of biodiesel methanol | |
| CN203429098U (en) | Alcohol recycling device in pectin production | |
| CN202164247U (en) | Device for recycling triethylene glycol | |
| CN214361177U (en) | Energy-saving consumption-reducing device for improving dehydration quality of carbon black raw oil | |
| CN102492555B (en) | Method and device for high-efficiency energy-saving desolvation of fossilized animal/plant wax-containing solution | |
| CN206626848U (en) | One kind utilizes second-kind absorption-type heat pump recovery waste heat system | |
| CN105669380A (en) | Ethylene glycol recovery device of polyester wastewater recovery system and ethylene glycol recovery method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |