CN103773419B - 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
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- CN103773419B CN103773419B CN201410031174.4A CN201410031174A CN103773419B CN 103773419 B CN103773419 B CN 103773419B CN 201410031174 A CN201410031174 A CN 201410031174A CN 103773419 B CN103773419 B CN 103773419B
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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 dust removal field, particularly relate 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 technique widespread use various gas production by-product tar, typically comprise coking furnace coal gas, low-temperature pyrolysis coal gas system.
The coal-tar middle oil content 50-200g/Nm of general 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 that the cyclic ammonia water directly spraying 70-75 DEG C in high temperature raw gas is connect and is down to 80-82 DEG C 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 DEG C with water coolant.Then condensation ammoniacal liquor spray cycle ammoniacal liquor and condensed tar and primary cooler condensation got off and tar send into mechanizeding ammonia clarifying groove, are divided into ammoniacal liquor, tar and coke tar refuse three part.Tar delivers to tar workshop through tar medial launder; Component loops Quench coal gas, unnecessary ammoniacal liquor is called remained ammonia.Remained ammonia is high-concentration phenolic wastewater, first through oil removing and solvent dephenolize after set, goes ammonia still process afterwards.
The utilization of coal tar then realizes cut cutting by reheating distillation.And coal tar must carry out dewatering and desalting deliming before it is distilled and takes off slag (dehydration can reduce distillation hear rate, and desalination alleviates the corrosion of equipment pipe, and deliming to take off the utilization of slag to tar distillation procedure and pitch be all favourable).
Be cooled to 25 ~ 35 DEG C directly to Sprayer Circulation ammoniacal liquor in coal gas of high temperature, in coal gas, waste heat could not utilize; A large amount of water quench is still needed after cyclic ammonia water spray; In order to make heavy tar can flow 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, ammonia distillation process need be adopted.In order to utilize coal tar, after needing dewatering and desalting, then coal tar is carried out distillation cutting cut by diamond heating again to 350 degrees 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; 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: raw material heat smoke enters spray column, output tar heavy oil bottom spray column, part tar heavy oil returns 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; Output last running bottom first packing tower, part last running returns the first packing tower as absorption liquid by the second pump, the second interchanger, another part last running is discharged by the second valve, and realize the fractionation of last running, the first packing tower top output gas enters the second packing tower; Output lighting end bottom second packing tower, part lighting end returns the second packing tower as absorption liquid by the 3rd pump, the 3rd interchanger, another part lighting end is discharged by the 3rd valve, and realize the fractionation of lighting end, the second packing tower top output gas enters the 4th interchanger; The gas of the second packing tower top output produces vapor phase stream stock and liquid phase stream stock after heat exchange in the 4th interchanger, and vapor phase stream stock enters electrical tar precipitator trapping light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator is separated 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.
Described raw material heat smoke temperature is not less than 400 DEG C.
Described spray column adopts atomizing spray, the top exit gas temperature of spray column is 250 DEG C, the temperature of spray column outlet at bottom tar heavy oil is 280 DEG C, 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 2-4 of raw material heat smoke quality doubly.
The first described packing tower top exit gas temperature is 150 DEG C, and the temperature of bottom heavy distillate is 200 DEG C, return the first packing tower as the double distilled component of absorption liquid be the 2-4 of spray column top output gaseous mass doubly.
The second described packing tower top exit gas temperature is 70 DEG C, and the temperature of bottom benzoline is 100 DEG C, return the second packing tower as the lighting end amount of absorption liquid be the 2-4 of the first packing tower top output gaseous mass doubly.
The 4th described heat exchanger outlet temperature is 25 DEG C.
The beneficial effect that the present invention has is: adopt the mode that heat of liquid is filtered, efficiency of dust collection reaches more than 99.9%.Compared with traditional gas cleaning at high temperature mode, greatly reduce required filtration area, decrease the cost of filtration and the volume needed for strainer, the utilization of coal gas of high temperature waste heat is achieved in process, in process of cooling, achieve the fractionation of tar, do not use the tar being aided with distillation again of direct condensed tar to utilize technique.Reduce the complicacy of system and decrease the energy consumption of system, in process of cooling, canbe used on line carbolic oil only produces a small amount of phenolic wastewater with being separated of water (in coal a small amount of moisture and Bound moisture) simultaneously, has obvious advantage compared with spraying ammonia condensing technique in a large number with tradition.The online fractionation that the present invention can be used for coke oven and the purification of kinds of processes low-temperature pyrolysis producer gas and tar is recycled.
Accompanying drawing explanation
Fig. 1 is tar online fractionation dust-removal system process flow sheet;
In figure: spray column 1, First Heat Exchanger 2, first packing tower 3, second interchanger 4, second packing tower 5, the 3rd interchanger 6, the 4th interchanger 7, electrical tar precipitator 8, water-and-oil separator 9, first pump 10, second pump 11, the 3rd pump 12, the 4th pump 13, first valve 14, 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, first packing tower 3, second interchanger 4, second packing tower 5, the 3rd interchanger 6, the 4th interchanger 7, electrical tar precipitator 8, water-and-oil separator 9, first pump 10, second pump 11, the 3rd pump 12, the 4th pump 13, first valve 14, 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, first valve 14 respectively, 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; 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: raw material heat smoke enters spray column 1, output tar heavy oil bottom spray column 1, part tar heavy oil returns 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; Output last running bottom first packing tower 3, part last running returns the first packing tower 3 as absorption liquid by the second pump 11, 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 gas enters the second packing tower 5; Output lighting end bottom second packing tower 5, part lighting end returns 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 gas enters the 4th interchanger 7; The gas of the second packing tower 5 top output produces vapor phase stream stock and liquid phase stream stock after heat exchange in the 4th interchanger 7, and vapor phase stream stock enters electrical tar precipitator 8 and traps light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator 9 is separated 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.
Described raw material heat smoke temperature is not less than 400 DEG C.
Described spray column 1 adopts atomizing spray, the top exit gas temperature of spray column 1 is 250 DEG C, the temperature of spray column 1 outlet at bottom tar heavy oil is 280 DEG C, 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 2-4 of raw material heat smoke quality doubly.
The first described packing tower 3 top exit gas temperature is 150 DEG C, and the temperature of bottom heavy distillate is 200 DEG C, return the first packing tower 3 as the double distilled component of absorption liquid be the 2-4 of spray column 1 top output gaseous mass doubly.
The second described packing tower 5 top exit gas temperature is 70 DEG C, and the temperature of bottom benzoline is 100 DEG C, return the second packing tower 5 as the lighting end amount of absorption liquid be the 2-4 of the first packing tower 3 top output gaseous mass doubly.
The 4th described interchanger 7 temperature out is 25 DEG C.
Heat smoke of the present invention is that the dry distillation of coal or fluidized bed pyrolysis produce flue gas, is characterized as heat smoke tar 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 heat smoke, to choose liquid at the bottom of tower be 280 DEG C is 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 hydrocracking can prepare petrol and diesel oil, also can heat filtering equipment be set at the bottom of tower simultaneously, realizes removing of thin ash.Coal gas isolates last running tar component in the first packing tower, can be used for hydrogenation of tar.Coal gas isolates benzoline component in the second packing tower, carries out preliminary being separated to carbolic oil 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 (such as 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, 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, 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); 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: raw material heat smoke enters spray column (1), spray column (1) bottom output tar heavy oil, part tar heavy oil returns 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 first packing tower (3) bottom, part last running returns 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 second packing tower (5) bottom, part lighting end returns 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 stock and liquid phase stream stock after heat exchange in the 4th interchanger (7), vapor phase stream stock enters electrical tar precipitator (8) trapping light oil combustion gas, and liquid phase stream stock-traders' know-how water-and-oil separator (9) is separated 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 described raw material heat smoke temperature is not less than 400 DEG C.
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 DEG C, the temperature of spray column (1) outlet at bottom tar heavy oil is 280 DEG C, 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 2-4 of raw material heat smoke quality doubly.
6. method according to claim 3, it is characterized in that described the first packing tower (3) top exit gas temperature is 150 DEG C, the temperature of bottom heavy distillate is 200 DEG C, return the first packing tower (3) as the double distilled component of absorption liquid be the 2-4 of spray column (1) top output gaseous mass doubly.
7. method according to claim 3, it is characterized in that described the second packing tower (5) top exit gas temperature is 70 DEG C, the temperature of bottom benzoline is 100 DEG C, return the second packing tower (5) as the lighting end amount of absorption liquid be the 2-4 of the first packing tower (3) top output gaseous mass doubly.
8. method according to claim 3, is characterized in that the 4th described interchanger (7) temperature out is 25 DEG C.
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| CN201410031174.4A CN103773419B (en) | 2014-01-23 | 2014-01-23 | System and method for on-line fractionation and dust removal of tar |
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| CN201410031174.4A CN103773419B (en) | 2014-01-23 | 2014-01-23 | System and method for on-line fractionation and dust removal of tar |
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| CN103773419B true CN103773419B (en) | 2015-04-29 |
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| CN104479725B (en) * | 2014-10-27 | 2016-03-02 | 陕西航星能源科技有限公司 | A kind of dry distillation gas lightweight oil degree of depth retrieving arrangement |
| CN111718765B (en) * | 2020-06-28 | 2022-04-08 | 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 |
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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 |
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