CN101475819B - Two-tower type pressure reducing coke tar distillation process and apparatus therefor - Google Patents
Two-tower type pressure reducing coke tar distillation process and apparatus therefor Download PDFInfo
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- CN101475819B CN101475819B CN2008102295844A CN200810229584A CN101475819B CN 101475819 B CN101475819 B CN 101475819B CN 2008102295844 A CN2008102295844 A CN 2008102295844A CN 200810229584 A CN200810229584 A CN 200810229584A CN 101475819 B CN101475819 B CN 101475819B
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Abstract
The invention relates to a two-tower type process for distilling vacuum tar and a device thereof. The process comprises the following steps: removing the moisture and light oil distillate of raw tar in a pre-dehydration tower and a dehydration tower at normal pressure; performing decompressing operations in a No.1 distillation tower to obtain carbolic oil, naphthalene oil and light washing oil distillate; and performing decompressing operations in a No.2 distillation tower to obtain heavy washing oil, first anthracene oil, second anthracene oil and mid-temperature pitch. The heat for the pre-dehydration tower and the dehydration tower is supplied by heat conducting oil; the heat for the No.1 distillation tower is supplied by heating the mixed oil on the bottom of the tower circularly in a No.1 tubular heating furnace; and the heat for the No.2 distillation tower is supplied by heating the mixed oil on the bottom of the No.1 distillation tower in a No.2 tubular heating furnace and then performing flash distillation on the mixed oil on the bottom of the No.2 tower. The main devices comprise the dehydration tower, the No.1 distillation tower, the No.2 distillation tower, a dehydration tower reboiler, the No.1 tubular heating furnace, the No.2 tubular heating furnace, a heat exchanger for each distillate, a cooler, a steam generator and the like. The process has the advantages of short technological flow, less device investment, and less energy consumption, thus the process is applicable to large scale coal tar processing engineering.
Description
Technical field
The present invention relates to metallurgical coking industry coal tar processing technical field, is a kind of tar distillation to be separated technology and the device thereof obtain various fractions and mid-temperature pitch, is specially adapted to the new construction that extensive coal tar is processed.
Background technology
Contain up to ten thousand kinds of materials in the coal tar, identified material has kind more than 500, kind surplus the ability product processed has 200.Because tar processing is made up of roughing out, precision work, this whole process of acquisition high value added product, roughing out is the requisite basis of following process, and the roughing out effect can directly influence quality, yield and the energy consumption of follow-up deep processed product.
At present, domestic and international existing coal tar distillation technology can be divided into underpressure distillation, atmospheric and vacuum distillation and air distillation three major types with regard to the working pressure of distillation tower.
One, reduced pressure distillation process flow process
Still-process is made up of dehydration and fraction distillation.Tar removes moisture and light oil fraction under the normal pressure in dehydration tower, anhydrous tar gets into the fraction tower and carries out underpressure distillation about tube furnace internal heating to 330 ℃ then, separates obtaining carbolic oil, naphtalene oil, washing oil, carbolineum fraction and viscid bitumen.
This technology fraction tower is under reduced pressure operated, and has reduced distillation temperature, has reduced the coking of tube furnace; And decompression operation can improve operating environment, helps environment protection.But because anhydrous tar need separate into a plurality of fractions in single tower, between each fraction cutting meticulous inadequately, cause high value added product to run off easily.If the viscid bitumen direct marketing of producing is because its softening temperature is low, need characteristics market such as liquid transportation limited, if further processing mid-temperature pitch then need increase facility investment and running cost.
In addition, because the separation of a plurality of fractions is in same tower, to accomplish, distillation institute heat requirement is provided by a tube furnace, limit by tube furnace device structure designing institute, and single covering device processing power is lower, is generally year to handle anhydrous tar 13～150,000 ton.
Two, atmospheric and vacuum distillation technical process
Still-process is made up of normal pressure dehydration, normal pressure fore-running and vacuum fractionation.
The raw material crude tar oil removes water and light oil fraction under the normal pressure in dehydration tower, the anhydrous tar at the bottom of the dehydration tower gets into primary tower after the tube furnace heating, in tower, carry out initial gross separation under the normal pressure.Obtain mid-temperature pitch at the bottom of the tower, the tower side line cuts the anthracene oil fraction, and overhead oil vapour gets into quench tower.Condensed mixing oil is sent into the vacuum fractionation system after adding alkali in quench tower.Fractionator overhead extraction carbolic oil fraction, the side line of tower cut carbolic oil, naphtalene oil, washing oil and a carbolineum fraction respectively, extraction anthracene oil fraction at the bottom of the tower, separation column distillation institute heat requirement by tower at the bottom of anthracene oil advance tube furnace circulation heating and provide.
The pressure of this technical process properly distributed distillation tower reaches energy and the reasonable best of breed of fractionation component; Fraction is cut apart thinner, reduces the heating that repeats of following process fraction.But complex process, equipment is various, and initial cost is big.Main fraction twice heating in fore-running and vacuum fractionation process in the tar, the gas consumption amount is big.
Three, air distillation technical process
Air distillation technology is that tar at first removes water and light oil fraction in dehydration tower; Dehydrated tar gets into about tube furnace internal heating to 405 ℃, gets into asphalt tower, extraction mid-temperature pitch at the bottom of the pitch Tata; Overhead oil vapour gets into the fraction tower, in the fraction tower, it is cut into various cuts then.Cut both cuts can be by narrow fraction, also can be by two mixing, three mixing cuts and carry out.In order to reduce service temperature, feed the superheated open steam at the bottom of asphalt tower, the fraction Tata.
This technical process is short, and initial cost is low, controls easyly, but compare the coal gas consumption with atmospheric and vacuum distillation higher with underpressure distillation.Distillation institute heat requirement is to be provided by a tube furnace equally, and single covering device processing power is 200,000 tons of year processing anhydrous tars to the maximum.And become phenolic wastewater after the oily water separation of the open steam that feeds process, increased the water pollution.
More than three kinds of tar distillation technologies characteristics are separately respectively arranged, technology one is technology of domestic comparative maturity with technology three, but processing power is limited to the production equipment of year handling 200,000 tons of anhydrous tars.Technology two is external patented technologies, and the domestic precedent that introduction was once arranged is because complex process; Equipment is various, adds the introduction of patented technology and major equipment, and engineering is once invested very big; And the complicacy of technology determined the complicacy of operation, and the execute-in-place difficulty is bigger.
In sum, it is simple that the design of at present domestic and international metallurgical coking industry urgent need has technical process, and easy handling is invested tar distillation novel process low, that environment protecting good, less energy consumption also can be applicable to extensive coal tar processing.
Summary of the invention
The purpose of this invention is to provide a kind ofly be applicable to that the processing of extensive coal tar, technical process are simple to operate, low equipment investment, minimizing environmental pollution, two-tower type pressure reducing tar distillation technology and device thereof that energy expenditure is low.
For realizing above-mentioned purpose, the present invention realizes through following technical proposals:
Two-tower type pressure reducing tar distillation technology; Comprise that raw tar is removing moisture and light oil fraction in dehydration tower, the dehydration tower in advance; Dehydrated tar is at 1# distillation tower cat head extraction carbolic oil fraction, and side line cuts naphtalene oil and fine laundering oil fraction, and mixing oil weighs the washing oil fraction in the extraction of 2# distillation tower cat head at the bottom of the tower after the heating of 2# tubular oven; Side line cuts a carbolineum, anthracene oil fraction; Extraction mid-temperature pitch at the bottom of the tower, raw tar is under condition of normal pressure, to remove moisture and light oil fraction in preparatory dehydration tower, dehydration tower, the heat of dehydration tower, dehydration tower is provided by thermal oil in advance; Dehydrated tar is that fractionation by distillation obtains various fractions and mid-temperature pitch under reduced pressure in 1#, 2# distillation tower; The heat of 1# distillation tower by tower at the bottom of mixing oil provide in 1# tubular oven internal recycle heating, the heat of 2# distillation tower by 1# distillation Tata at the bottom of mixing oil provide at 2# tubular oven internal heating.
1# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa; 115～140 ℃ of tower top temperatures, 165～190 ℃ of naphtalene oil fraction extraction plate temperatures, 180～220 ℃ of fine laundering oil fraction extraction plate temperatures; 240～270 ℃ of column bottom temperatures; 260～290 ℃ of 1# tubular oven turning oil temperature outs, cat head carbolic oil reflux ratio is 0.7～0.85t/t, reflux ratio is the ratio of cat head carbolic oil and anhydrous tar.
2# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa; 190～210 ℃ of tower top temperatures, 260～280 ℃ of carbolineum fraction extraction plate temperatures, 320～340 ℃ of anthracene oil fraction extraction plate temperatures; 350～370 ℃ of column bottom temperatures; 350～385 ℃ of 2# tubular oven mixing oil temperature outs, the heavy washing oil reflux ratio of cat head is 0.15～0.25t/t, reflux ratio is the ratio of cat head carbolic oil and anhydrous tar.
The device of two-tower type pressure reducing tar distillation process using; Comprise two distillation towers, by the heat supply respectively of two tube furnaces, dehydration tower, dehydration tower, 1# distillation tower, 2# distillation tower connect through pipeline successively in advance; The 1# distillation tower connects the 1# tubular oven, and the 2# distillation tower connects the 2# tubular oven; Be provided with the dehydration tower reboiler at the bottom of the dehydration tower; 1# distillation tower side line is provided with interchanger, water cooler, cut extraction pump; 2# distillation tower side line is provided with vapour generator, and cut extraction pump, water cooler connect successively, and the 2# distillation tower also is connected with the interchanger of heating raw tar.
1# distillation tower, 2# distillation tower are valve tray column, adopt the novel float valve in wide aperture, and material is a stainless steel, and the 1# distillation tower has 15～50 blocks of theoretical trays, and the 2# distillation tower has 8～30 blocks of column plates.
1# tubular oven and 2# tubular oven are vertical coil pipe cylindrical furnace, and upper of furnace body is energy-conservation section with flue gas heat exchange, and the bottom is a radiation section, and furnace tube material is a stainless steel.
Compare with existing tar distillation technology, two-tower type pressure reducing tar distillation technology of the present invention has the following advantages:
1) compare with domestic normal pressure flow process, decompression flow process, cutting in two distillation towers of fraction accomplished respectively, by the heat supply respectively of two tube furnaces, solved the technical barrier of handling extensive tar with single covering device;
2) compare with external normal decompression flow process, flow process is short, low equipment investment, control easy, easy handling, constant product quality, equipment operation, maintenance cost are lower;
3) dehydration of tar carries out under normal pressure, and distillation is under reduced pressure carried out, and temperature, pressure regime distribute rationally, and underpressure distillation has reduced service temperature, and the gas consumption amount is low;
4) adopt the heat-supplying mode of oil circulation heating at the bottom of dehydration tower, the 1# distillation Tata, be convenient to operation and regulate;
5) still-process need not feed open steam, does not produce phenolic wastewater;
6) fraction is cut apart carefullyyer, reduces the heating that repeats of following process fraction, reduces total energy consumption;
7) UTILIZATION OF VESIDUAL HEAT IN is abundant, can reclaimed fully and utilizes through heat exchange like the heat of pitch and each fraction;
8) because distillation is under negative pressure, to operate, can improve operating environment, help environment protection;
9) fraction that be prone to crystallization, is prone to solidify cools off minimizing equipment, line clogging with warm water;
10) dehydration of tar substitutes steam heating with heat-conducting oil heating, practices thrift steam, reduces the water of condensation discharge capacity.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is done further explain.
As shown in Figure 1, raw tar advances tar preheater 9 after at first getting into tar/heavy washing oil interchanger 18 and the heat exchange of heavy washing oil fraction, by heat-conducting oil heating to 125～135 ℃, gets into preparatory dehydration tower 1 at this then.
The dehydration column overhead temperature is about 110～125 ℃ in advance; Light oil fraction that cat head is overflowed and water are cooled to 50～60 ℃ through 1# light oil air cooler 7 earlier; Be cooled to 40～45 ℃ through 1# light oil water cooler 10 again; Flow into 1# light oil separator 26, isolated light oil is as the dehydration tower usefulness that refluxes, and flows into ammonia vessel after dividing dried up further separating oil.Tar at the bottom of the dehydration Tata is from flowing into dehydration tower 2 in advance.
The dehydration column overhead temperature is 100～115 ℃; Distilled light oil fraction and water are cooled to 50～60 ℃ through 2# light oil air cooler 8 earlier; Be cooled to 40～45 ℃ through 2# light oil water cooler 11 again, flow into 2# light oil separator 27, isolate light oil at this; Part light oil send the dehydration cat head as backflow by dehydration tower reflux pump 29, and all the other send the oil depot device as product by light oil extraction pump 40; Flow into ammonia vessel after dividing dried up further separating oil, regularly by ammoniacal liquor transferpump gas delivery cleaning shop, isolated oil flows into the emptying groove.Dehydrated tar by the dehydration Tata at the bottom of extractor pump 31 extract out, send into the bottom of 1# distillation tower.
As thermal source, extract out with dehydration tower recycle pump 30 by dehydration tower bed coke oil with thermal oil for dehydration tower, is heated to 200～220 ℃ through 12 circulations of dehydration tower reboiler, returns at the bottom of the dehydration tower to provide dehydration to distill institute's heat requirement.
1# distillation tower 3 is a decompression operation, and tower top pressure is about absolute pressure 10～30kPa, and tower top temperature is 110～140 ℃, and from the condensation in carbolic oil reduction appts. 13 of cat head distilled carbolic oil vapour, a part is as refluxing from flowing back to cat head; Another part after carbolic oil water cooler 14 is cooled to 50～60 ℃, flows into the carbolic oil groove, regularly with being pumped to the subsequent production device as the intermediates extraction.
Cut naphtalene oil fraction, fine laundering oil fraction respectively from 1# distillation tower 3 side lines.About 165～190 ℃ of naphtalene oil fraction tower exit temperature is introduced into soft water/naphtalene oil interchanger 15 to the soft water heating, extracts out with naphtalene oil extraction pump 32 again, is cooled to 85～95 ℃ through naphtalene oil water cooler 16 usefulness warm water, send the naphtalene oil groove to store, regularly with being pumped to the subsequent production device.About 180～220 ℃ of fine laundering oil fraction tower exit temperature is cooled to 65～75 ℃ through fine laundering oil cooler 17 usefulness warm water, extracts out with fine laundering oil extraction pump 33 and send the fine laundering groove to store, regularly with being pumped to the oil depot device.
1# distillation tower column bottom temperature is about 240～270 ℃, and a mixing oil part is extracted out with recycle pump at the bottom of the 1# tower 34 at the bottom of the tower, is heated to 260～290 ℃ through 1# tubular oven 5, gets back to then at the bottom of the tower, and distillation institute heat requirement is provided; Another part is extracted out by 1# column bottoms pump extractor pump 35, sends into 2# tubular oven 6.
1# distillation tower cat head non-condensable gases gets into vacuum system after vacuum cooler-condenser 24 condensations.
The mixing oil that is come by the 1# base product gets into the bottom of 2# distillation tower 4 2# tubular oven internal heating to 350～385 ℃.The 2# distillation tower is a decompression operation, and tower top pressure is about absolute pressure 10～30kPa, and tower top temperature is 190～210 ℃; From the heavy washing oil vapour of cat head distilled after tar/heavy washing oil interchanger 18 and raw tar heat exchange; In heavy washing oil water cooler 19, be cooled to 85～95 ℃, flow into heavy washing oil backflash 28 again, with heavy washing oil reflux pump 36 the heavy washing oil of a part is sent to 2# distillation tower cat head as backflow at this with warm water; Another part to heavy washing oil groove is stored, and regularly uses pumping oil depot device.
Cut a carbolineum fraction and anthracene oil fraction respectively from 2# distillation tower side line.About 260～280 ℃ of one carbolineum fraction tower exit temperature; Temperature is about 170～190 ℃ after vapour generator 20 heat exchange; Be cooled to 85～95 ℃ with a carbolineum extraction pump 37 through a carbolineum water cooler 21 usefulness warm water then, deliver to a carbolineum groove and store, regularly use pumping oil depot device.About 320～340 ℃ of anthracene oil fraction tower exit temperature; Temperature is about 170～190 ℃ after vapour generator 20 heat exchange; Be cooled to 85～95 ℃ with anthracene oil extraction pump 38 through anthracene oil water cooler 22 usefulness warm water then, deliver to the anthracene oil groove and store, regularly use pumping oil depot device.
2# distillation tower column bottom temperature is about 350～370 ℃, and extractor pump 39 was extracted out after sending pitch/heat-condutive oil heat exchanger 23 and thermal oil heat exchange at the bottom of mid-temperature pitch distilled Tata by 2#, delivered to the subsequent production device.
The vacuum exhaust of 2# distillation tower is extracted out by heavy washing oil water cooler, through the laggard vacuum system of vacuum cooler-condenser 25 condensations,
Described 1# distillation tower and 2# distillation tower are valve tray column, and the 1# distillation tower has 15～50 blocks of theoretical trays, and the 2# distillation tower has 8～30 blocks of theoretical trays, adopt the novel float valve in wide aperture, and material is a stainless steel.
Described 1# tubular oven and 2# tubular oven are vertical coil pipe cylindrical furnace, and furnace tube material is a stainless steel.
Described interchanger, water cooler are shell-and-tube, according to different choice stationary tubesheet, U type pipe or the floating head type of fluid properties.The interchanger material is selected carbon steel or stainless steel for use according to the corrosion situation of medium.
Claims (6)
1. two-tower type pressure reducing tar distillation technology; It is characterized in that comprise that raw tar is removing moisture and light oil fraction in dehydration tower, the dehydration tower in advance, dehydrated tar is at 1# distillation tower cat head extraction carbolic oil fraction; Side line cuts naphtalene oil and fine laundering oil fraction; At the heavy washing oil fraction of 2# distillation tower cat head extraction, side line cuts a carbolineum, anthracene oil fraction to mixing oil, extraction mid-temperature pitch at the bottom of the tower after the heating of 2# tubular oven at the bottom of the tower; Raw tar is under condition of normal pressure, to remove moisture and light oil fraction in preparatory dehydration tower, dehydration tower, and the heat of dehydration tower, dehydration tower is provided by thermal oil in advance; Dehydrated tar is that fractionation by distillation obtains various fractions and mid-temperature pitch under reduced pressure in 1#, 2# distillation tower; The heat of 1# distillation tower by tower at the bottom of mixing oil provide in 1# tubular oven internal recycle heating, the heat of 2# distillation tower by 1# distillation Tata at the bottom of mixing oil provide at 2# tubular oven internal heating.
2. two-tower type pressure reducing tar distillation technology according to claim 1 is characterized in that 1# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa; 115～140 ℃ of tower top temperatures; 165～190 ℃ of naphtalene oil fraction extraction plate temperatures, 180～220 ℃ of fine laundering oil fraction extraction plate temperatures, 240～270 ℃ of column bottom temperatures; 260～290 ℃ of 1# tubular oven turning oil temperature outs, cat head carbolic oil reflux ratio is 0.7～0.85t/t.
3. two-tower type pressure reducing tar distillation technology according to claim 1; It is characterized in that 2# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa, 190～210 ℃ of tower top temperatures, 260～280 ℃ of carbolineum fraction extraction plate temperatures; 320～340 ℃ of anthracene oil fraction extraction plate temperatures; 350～370 ℃ of column bottom temperatures, 350～385 ℃ of 2# tubular oven mixing oil temperature outs, the heavy washing oil reflux ratio of cat head 0.15～0.25t/t.
4. the device of two-tower type pressure reducing tar distillation process using according to claim 1; It is characterized in that; Comprise two distillation towers, by the heat supply respectively of two tubular ovens, dehydration tower, dehydration tower, 1# distillation tower, 2# distillation tower connect through pipeline successively in advance; The 1# distillation tower connects the 1# tubular oven, and the 2# distillation tower connects the 2# tubular oven; Be provided with the dehydration tower reboiler at the bottom of the dehydration tower; 1# distillation tower side line is provided with interchanger, water cooler, cut extraction pump; 2# distillation tower side line is provided with vapour generator, and cut extraction pump, water cooler connect successively, and the 2# distillation tower also is connected with the interchanger of heating raw tar.
5. the device of two-tower type pressure reducing tar distillation process using according to claim 4; It is characterized in that 1# tubular oven and 2# tubular oven are vertical coil pipe cylindrical furnace, upper of furnace body is energy-conservation section with flue gas heat exchange; The bottom is a radiation section, and furnace tube material is a stainless steel.
6. the device of two-tower type pressure reducing tar distillation process using according to claim 4 is characterized in that, cut interchanger, water cooler are shell-and-tube, according to the different choice stationary tubesheet of fluid properties, U-shaped pipe or floating head type; The interchanger material is selected carbon steel or stainless steel for use according to the corrosion situation of medium.
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