CN103773419A - System and method for on-line fractionation and dust removal of tar - Google Patents
System and method for on-line fractionation and dust removal of tar Download PDFInfo
- Publication number
- CN103773419A CN103773419A CN201410031174.4A CN201410031174A CN103773419A CN 103773419 A CN103773419 A CN 103773419A CN 201410031174 A CN201410031174 A CN 201410031174A CN 103773419 A CN103773419 A CN 103773419A
- Authority
- CN
- China
- Prior art keywords
- pump
- packing tower
- tar
- valve
- interchanger
- 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.)
- Granted
Links
Landscapes
- Industrial Gases (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a system and method for on-line fractionation and dust removal of tar. The system comprises a spray tower, a first heat exchanger, a first filled tower, a second heat exchanger, a second filled tower, a third heat exchanger, a fourth heat exchanger, an electric tar precipitator, an oil-water separator, a first pump, a second pump, a third pump, a fourth pump, a first valve, a second valve, a third valve, a fourth valve and a heat filter. According to the invention, a liquid heat filtration mode is adopted, and the dust removal efficiency is up to 99.9% or above; and compared with a gas filtration mode, the filtration cost and the volume required by the filter are reduced, utilization of waste heat of high-temperature coal gas is realized in the process, fractionation of tar is realized in a cooling process, and a tar utilization process of direct tar condensation and then distillation is not used any more. The complexity of the system is reduced, the energy consumption of the system is reduced, and separation of phenol oil and water is realized on line in the cooling process while only a small amount of phenol waste water is produced. Compared with the traditional large-amount ammonium spray condensation process, the invention has obvious advantages.
Description
Technical field
The present invention relates to tar fractionation dedusting field, relate in particular to the online fractionation dust-removal system of a kind of tar and method.
Background technology
Gas purification and tar are recycled in the system of the various gas production by-product of technique widespread use tar, typically comprise coking furnace coal gas, low-temperature pyrolysis coal gas system.
The general coal-tar middle oil content 50-200g/Nm of coal gas
3, fly ash content reaches 5-20g/Nm
3.Therefore general purification process comprises the master operation contents such as cooling, washing, parsing, aftertreatment.It is in high temperature raw gas, directly to spray the cyclic ammonia water of 70-75 ℃ to be connect and be down to 80-82 ℃ that the technique of tar is reclaimed in gas purification ash disposal, then makes coal gas enter in primary cooler, is indirectly directly cooled to 25-35 ℃ with water coolant.Then the condensation ammoniacal liquor and the tar that spray cycle ammoniacal liquor and condensed tar and primary cooler condensation are got off are sent into mechanizeding ammonia clarifying groove, are divided into ammoniacal liquor, tar and coke tar refuse three parts.Tar is delivered to tar workshop through tar medial launder; The part Quench coal gas that circulates, unnecessary ammoniacal liquor is called remained ammonia.Remained ammonia is high-concentration phenolic wastewater, after set, first through oil removing and solvent dephenolize, goes ammonia still process afterwards.
The utilization of coal tar realizes cut cutting by reheating distillation.And coal tar must carry out the de-slag of dewatering and desalting deliming (dehydration can reduce distillation hear rate, and desalination has alleviated the corrosion of equipment pipe, and the de-slag of deliming is all favourable to the utilization of tar distillation procedure and pitch) before distillation.
Directly be cooled to 25～35 ℃ to Sprayer Circulation ammoniacal liquor in coal gas of high temperature, in coal gas, waste heat could not utilize; After cyclic ammonia water spray, still need a large amount of water quench; For heavy tar can be flowed with ammoniacal liquor, the ammoniacal liquor of spray is greatly excessive, produces a large amount of phenolic wastewater.For making waste water circulation ammonia nitrogen up to standard, need to adopt ammonia distillation process.In order to utilize coal tar, need after dewatering and desalting, then coal tar is distilled to cutting cut again by diamond heating to 350 degree Celsius.
Summary of the invention
The object of the invention is the deficiencies in the prior art, the online fractionation dust-removal system of a kind of tar and method are provided.
The online fractionation dust-removal system of tar comprises spray column, First Heat Exchanger, the first packing tower, the second interchanger, the second packing tower, the 3rd interchanger, the 4th interchanger, electrical tar precipitator, water-and-oil separator, the first pump, the second pump, the 3rd pump, the 4th pump, the first valve, the second valve, the 3rd valve, the 4th valve, heat filter; The top of spray column is connected with the first packing tower, and the bottom of spray column is connected with the first pump, the first valve respectively, and the first pump is connected with First Heat Exchanger, and First Heat Exchanger is connected with the top of spray column, and the first valve is connected with heat filter; The top of the second packing tower is connected with the 4th interchanger, and the bottom of the second packing tower is connected with the 3rd pump, the 3rd valve respectively, and the 3rd pump is connected with the 3rd interchanger, and the 3rd interchanger is connected with the top of the second packing tower; The 4th interchanger is connected with electrical tar precipitator, water-and-oil separator respectively, and electrical tar precipitator, water-and-oil separator are connected with the 4th pump respectively, and the 4th pump is connected with the 4th valve.
Described heat filter adopts Y-piece road strainer.
The fractionation method for dust removal of the online fractionation dust-removal system of tar is: the hot flue gas of raw material enters spray column, spray column bottom output tar heavy oil, part tar heavy oil returns to spray column as spray liquid by the first pump, First Heat Exchanger, another part tar heavy oil is discharged by the first valve, heat filter, realize the fractionation dedusting of tar heavy oil, spray column top output gas enters the first packing tower; The first packing tower bottom output last running, part last running is returned to the first packing tower as absorption liquid by the second pump, the second interchanger, another part last running goes out by second valve door row, realizes the fractionation of last running, and the first packing tower top output gas enters the second packing tower; The second packing tower bottom output lighting end, part lighting end is returned to the second packing tower as absorption liquid by the 3rd pump, the 3rd interchanger, another part lighting end is discharged by the 3rd valve, realizes the fractionation of lighting end, and the second packing tower top output gas enters the 4th interchanger; The gas of the second packing tower top output produces vapor phase stream thigh and liquid phase stream thigh in the 4th interchanger after heat exchange, vapor phase stream thigh enters electrical tar precipitator trapping light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator separates and obtains light oil and water; The light oil that electrical tar precipitator, water-and-oil separator obtain is discharged through the 4th pump and the 4th valve; Realize the fractionation of light oil.
The hot flue-gas temperature of described raw material is not less than 400 ℃.
Described spray column adopts atomizing spray, the top exit gas temperature of spray column is 250 ℃, the temperature of spray column outlet at bottom tar heavy oil is 280 ℃, and the air speed of spray column is 1-2m/s, return spray column as the tar heavy oil amount of spray liquid be the hot flue gas quality of raw material 2-4 doubly.
The first described packing tower top exit gas temperature is 150 ℃, and the temperature of bottom heavy distillate is 200 ℃, return the first packing tower as the double distilled component of absorption liquid be spray column top output gaseous mass 2-4 doubly.
The second described packing tower top exit gas temperature is 70 ℃, and the temperature of bottom benzoline is 100 ℃, return the second packing tower as the lighting end amount of absorption liquid be the first packing tower top output gaseous mass 2-4 doubly.
The 4th described heat exchanger outlet temperature is 25 ℃.
The beneficial effect that the present invention has is: the mode that adopts heat of liquid to filter, efficiency of dust collection reaches more than 99.9%.Compared with traditional gas cleaning at high temperature mode, greatly reduce required filtration area, the cost and the required volume of strainer that filter are reduced, in process, realize the utilization of coal gas of high temperature waste heat, in process of cooling, realize the fractionation of tar, do not utilized technique at the tar that is aided with again distillation that uses direct condensed tar.Reduce the complicacy of system and reduced the energy consumption of system, in process of cooling canbe used on line separating of carbolic oil and water (in coal a small amount of moisture with in conjunction with water) only produce a small amount of phenolic wastewater simultaneously, there is obvious advantage compared with spraying in a large number ammonia condensing technique with tradition.The present invention can be used for coke oven and kinds of processes low-temperature pyrolysis producer gas purifies and the online fractionation of tar is recycled.
Accompanying drawing explanation
Fig. 1 is the online fractionation dust-removal system of tar process flow sheet;
In figure: spray column 1, First Heat Exchanger 2, the first packing tower 3, the second interchanger 4, the second packing tower 5, the 3rd interchanger 6, the 4th interchanger 7, electrical tar precipitator 8, water-and-oil separator 9, the first pump 10, the second pump 11, the 3rd pump 12, the 4th pump 13, the first valve 14, the second valve 15, the 3rd valve 16, the 4th valve 17, heat filter 18.
Embodiment
As shown in Figure 1, the online fractionation dust-removal system of tar comprises spray column 1, First Heat Exchanger 2, the first packing tower 3, the second interchanger 4, the second packing tower 5, the 3rd interchanger 6, the 4th interchanger 7, electrical tar precipitator 8, water-and-oil separator 9, the first pump 10, the second pump 11, the 3rd pump 12, the 4th pump 13, the first valve 14, the second valve 15, the 3rd valve 16, the 4th valve 17, heat filter 18; The top of spray column 1 is connected with the first packing tower 3, the bottom of spray column 1 is connected with the first pump 10, the first valve 14 respectively, the first pump 10 is connected with First Heat Exchanger 2, and First Heat Exchanger 2 is connected with the top of spray column 1, and the first valve 14 is connected with heat filter 18; The top of the second packing tower 5 is connected with the 4th interchanger 7, and the bottom of the second packing tower 5 is connected with the 3rd pump 12, the 3rd valve 16 respectively, and the 3rd pump 12 is connected with the 3rd interchanger 6, and the 3rd interchanger 6 is connected with the top of the second packing tower 5; The 4th interchanger 7 is connected with electrical tar precipitator 8, water-and-oil separator 9 respectively, and electrical tar precipitator 8, water-and-oil separator 9 are connected with the 4th pump 13 respectively, and the 4th pump 13 is connected with the 4th valve 17.
Described heat filter 18 adopts Y-piece road strainer.
The fractionation method for dust removal of the online fractionation dust-removal system of tar is: the hot flue gas of raw material enters spray column 1, spray column 1 bottom output tar heavy oil, part tar heavy oil returns to spray column 1 as spray liquid by the first pump 10, First Heat Exchanger 2, another part tar heavy oil is discharged by the first valve 14, heat filter 18, realize the fractionation dedusting of tar heavy oil, spray column 1 top output gas enters the first packing tower 3; The first packing tower 3 bottom output last running, part last running is returned to the first packing tower 3 as absorption liquid by the second pump 11, the second interchanger 4, another part last running is discharged by the second valve 15, realizes the fractionation of last running, and the first packing tower 3 top output gases enter the second packing tower 5; The second packing tower 5 bottom output lighting ends, part lighting end is returned to the second packing tower 5 as absorption liquid by the 3rd pump 12, the 3rd interchanger 6, another part lighting end is discharged by the 3rd valve 16, realizes the fractionation of lighting end, and the second packing tower 5 top output gases enter the 4th interchanger 7; The gas of the second packing tower 5 top outputs produces vapor phase stream thigh and liquid phase stream thigh in the 4th interchanger 7 after heat exchange, vapor phase stream thigh enters electrical tar precipitator 8 and traps light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator 9 separates and obtains light oil and water; The light oil that electrical tar precipitator 8, water-and-oil separator 9 obtain is discharged through the 4th pump 13 and the 4th valve 17; Realize the fractionation of light oil.
The hot flue-gas temperature of described raw material is not less than 400 ℃.
Described spray column 1 adopts atomizing spray, the top exit gas temperature of spray column 1 is 250 ℃, the temperature of spray column 1 outlet at bottom tar heavy oil is 280 ℃, and the air speed of spray column 1 is 1-2m/s, return spray column 1 as the tar heavy oil amount of spray liquid be the hot flue gas quality of raw material 2-4 doubly.
The first described packing tower 3 top exit gas temperatures are 150 ℃, and the temperature of bottom heavy distillate is 200 ℃, return the first packing tower 3 as the double distilled component of absorption liquid be spray column 1 top output gaseous mass 2-4 doubly.
The second described packing tower 5 top exit gas temperatures are 70 ℃, and the temperature of bottom benzoline is 100 ℃, return the second packing tower 5 as the lighting end amount of absorption liquid be the first packing tower 3 top output gaseous masses 2-4 doubly.
The 4th described interchanger 7 temperature outs are 25 ℃.
Hot flue gas of the present invention is that the dry distillation of coal or fluidized bed pyrolysis produce flue gas, is characterized as hot tarry matters in smoke content and reaches 50-200g/Nm
3, fly ash content reaches 5-20g/Nm
3.First high temperature oil-containing collects heavy tar components through Quench spray column containing grey hot flue gas, choosing at the bottom of tower liquid, to be 280 ℃ be the Pintsch process in order to reduce it, and directly enter vacuum distillation equipment and carry out underpressure distillation and obtain VGO component and asphalt component, VGO component can hydrocracking be prepared petrol and diesel oil, heat filtering equipment also can be set simultaneously at the bottom of tower, realize removing of thin ash.Coal gas is isolated last running tar component in the first packing tower, can be used for hydrogenation of tar.Coal gas is isolated benzoline component in the second packing tower, carbolic oil is carried out to preliminary separating with water simultaneously, reduces the discharge of phenolic wastewater.Light oil is collected in water-and-oil separator and electric fishing light oil device.Electric fishing light oil device coal gas out can carry out further purifying treatment and utilize (for example de-benzene, desulfurization etc.).
Claims (8)
1. the online fractionation dust-removal system of tar, is characterized in that comprising spray column (1), First Heat Exchanger (2), the first packing tower (3), the second interchanger (4), the second packing tower (5), the 3rd interchanger (6), the 4th interchanger (7), electrical tar precipitator (8), water-and-oil separator (9), the first pump (10), the second pump (11), the 3rd pump (12), the 4th pump (13), the first valve (14), the second valve (15), the 3rd valve (16), the 4th valve (17), heat filter (18); The top of spray column (1) is connected with the first packing tower (3), the bottom of spray column (1) is connected with the first pump (10), the first valve (14) respectively, the first pump (10) is connected with First Heat Exchanger (2), First Heat Exchanger (2) is connected with the top of spray column (1), and the first valve (14) is connected with heat filter (18); The top of the second packing tower (5) is connected with the 4th interchanger (7), the bottom of the second packing tower (5) is connected with the 3rd pump (12), the 3rd valve (16) respectively, the 3rd pump (12) is connected with the 3rd interchanger (6), and the 3rd interchanger (6) is connected with the top of the second packing tower (5); The 4th interchanger (7) is connected with electrical tar precipitator (8), water-and-oil separator (9) respectively, and electrical tar precipitator (8), water-and-oil separator (9) are connected with the 4th pump (13) respectively, and the 4th pump (13) is connected with the 4th valve (17).
2. the online fractionation dust-removal system of tar according to claim 1, is characterized in that described heat filter (18) adopts Y-piece road strainer.
3. the fractionation method for dust removal of the online fractionation dust-removal system of tar according to claim 1, it is characterized in that: the hot flue gas of raw material enters spray column (1), spray column (1) bottom output tar heavy oil, part tar heavy oil returns to spray column (1) as spray liquid by the first pump (10), First Heat Exchanger (2), another part tar heavy oil is discharged by the first valve (14), heat filter (18), realize the fractionation dedusting of tar heavy oil, spray column (1) top output gas enters the first packing tower (3); The output last running of the first packing tower (3) bottom, part last running is returned to the first packing tower (3) as absorption liquid by the second pump (11), the second interchanger (4), another part last running is discharged by the second valve (15), realize the fractionation of last running, the first packing tower (3) top output gas enters the second packing tower (5); The output lighting end of the second packing tower (5) bottom, part lighting end is returned to the second packing tower (5) as absorption liquid by the 3rd pump (12), the 3rd interchanger (6), another part lighting end is discharged by the 3rd valve (16), realize the fractionation of lighting end, the second packing tower (5) top output gas enters the 4th interchanger (7); The gas of the second packing tower (5) top output produces vapor phase stream thigh and liquid phase stream thigh after heat exchange in the 4th interchanger (7), vapor phase stream thigh enters electrical tar precipitator (8) trapping light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator (9) separates and obtains light oil and water; The light oil that electrical tar precipitator (8), water-and-oil separator (9) obtain is discharged through the 4th pump (13) and the 4th valve (17); Realize the fractionation of light oil.
4. method according to claim 3, is characterized in that the described hot flue-gas temperature of raw material is not less than 400 ℃.
5. method according to claim 3, it is characterized in that described spray column (1) adopts atomizing spray, the top exit gas temperature of spray column (1) is 250 ℃, the temperature of spray column (1) outlet at bottom tar heavy oil is 280 ℃, the air speed of spray column (1) is 1-2m/s, return spray column (1) as the tar heavy oil amount of spray liquid be the hot flue gas quality of raw material 2-4 doubly.
6. method according to claim 3, it is characterized in that described the first packing tower (3) top exit gas temperature is 150 ℃, the temperature of bottom heavy distillate is 200 ℃, return the first packing tower (3) as the double distilled component of absorption liquid be spray column (1) top output gaseous mass 2-4 doubly.
7. method according to claim 3, it is characterized in that described the second packing tower (5) top exit gas temperature is 70 ℃, the temperature of bottom benzoline is 100 ℃, return the second packing tower (5) as the lighting end amount of absorption liquid be the first packing tower (3) top output gaseous mass 2-4 doubly.
8. method according to claim 3, is characterized in that the 4th described interchanger (7) temperature out is 25 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410031174.4A CN103773419B (en) | 2014-01-23 | 2014-01-23 | System and method for on-line fractionation and dust removal of tar |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410031174.4A CN103773419B (en) | 2014-01-23 | 2014-01-23 | System and method for on-line fractionation and dust removal of tar |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103773419A true CN103773419A (en) | 2014-05-07 |
| CN103773419B CN103773419B (en) | 2015-04-29 |
Family
ID=50566187
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410031174.4A Active CN103773419B (en) | 2014-01-23 | 2014-01-23 | System and method for on-line fractionation and dust removal of tar |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103773419B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104479725A (en) * | 2014-10-27 | 2015-04-01 | 陕西航星能源科技有限公司 | Device for deep recovering light oil from dry distillation gas |
| CN111718765A (en) * | 2020-06-28 | 2020-09-29 | 河南恒天久大实业有限公司 | Device and absorption method for fuel oil in plastic pyrolysis gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201949808U (en) * | 2011-01-12 | 2011-08-31 | 江苏新世纪江南环保有限公司 | Flue gas desulfurization device for realizing online oil and dust separation |
| CN102259943A (en) * | 2011-07-21 | 2011-11-30 | 天津市昊永化工科技有限公司 | Energy-saving method for recycling wastewater containing phenol and ammonia |
| CN103215089A (en) * | 2013-04-09 | 2013-07-24 | 陕西煤业化工技术研究院有限责任公司 | Device and method for cold-state separation of gas and solid in pulverized coal pyrolysis |
| CN203754649U (en) * | 2014-01-23 | 2014-08-06 | 浙江大学 | Online tar oil fractionation and dedusting system |
-
2014
- 2014-01-23 CN CN201410031174.4A patent/CN103773419B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201949808U (en) * | 2011-01-12 | 2011-08-31 | 江苏新世纪江南环保有限公司 | Flue gas desulfurization device for realizing online oil and dust separation |
| CN102259943A (en) * | 2011-07-21 | 2011-11-30 | 天津市昊永化工科技有限公司 | Energy-saving method for recycling wastewater containing phenol and ammonia |
| CN103215089A (en) * | 2013-04-09 | 2013-07-24 | 陕西煤业化工技术研究院有限责任公司 | Device and method for cold-state separation of gas and solid in pulverized coal pyrolysis |
| CN203754649U (en) * | 2014-01-23 | 2014-08-06 | 浙江大学 | Online tar oil fractionation and dedusting system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104479725A (en) * | 2014-10-27 | 2015-04-01 | 陕西航星能源科技有限公司 | Device for deep recovering light oil from dry distillation gas |
| CN111718765A (en) * | 2020-06-28 | 2020-09-29 | 河南恒天久大实业有限公司 | Device and absorption method for fuel oil in plastic pyrolysis gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103773419B (en) | 2015-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101619223B (en) | Oil-washing energy-saving device of condensing recovery system by oil shale carbonization method and operation process thereof | |
| CN103013583B (en) | Process for dust removing, cooling and tar oil recovering of pyrolysis coal gas | |
| CN102585918B (en) | Technology and system for deep removal of tar in biomass gas by coupling adsorption | |
| CN106731444A (en) | A kind of coking plant low pressure loss gas recovery and treatment method and device | |
| CN104449880B (en) | A kind of raw gas purifying method and device | |
| CN104388128B (en) | System and method for dedusting of pyrolysis raw gas and tar recycling employing oil-cooling | |
| CN103965971B (en) | Double-tower type coal tar recovering system and recovery method | |
| CN103589462A (en) | Technological method for purifying coal oven gas and recovering chemical products | |
| SA95150447B1 (en) | Method for re-refining used oils | |
| CN108096999B (en) | Reboiler method negative pressure crude benzene distillation process | |
| CN103409175A (en) | Purifying and tar recovery system for high temperature gas containing ash and tar and method thereof | |
| CN105036507A (en) | Pyrolysis oil-gas-water synchronous condensing and oil-water separation recovery system and method | |
| CN203754648U (en) | Online tar oil fractionation and dedusting system | |
| CN109576001B (en) | Organic hazardous waste pyrolysis gas purifying system | |
| CN103773419B (en) | System and method for on-line fractionation and dust removal of tar | |
| CN109021999B (en) | Device for recovering pyrolysis gas, method and application thereof | |
| CN110330988A (en) | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology | |
| CN203754649U (en) | Online tar oil fractionation and dedusting system | |
| CN103773420B (en) | The online fractionation dust pelletizing system of tar and method | |
| CN203411517U (en) | Ash and tar-containing high-temperature coal gas purification and tar recovery system | |
| CN108728175A (en) | Organic dangerous waste pyrolysis gas purification system | |
| CN206279155U (en) | A kind of system of utilization low-order coal | |
| CN102994171B (en) | Gas turbine generating coke oven gas comprehensive purification system and purification method thereof | |
| WO2012079499A1 (en) | Method and device for enclosed recycling of oil-water-sludge in oil shale dry distillation system | |
| CN209519364U (en) | A kind of embrane method Reclaimed Base Oil purifying refining system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |