CN103666513B - High-dust-content coal tar separation and upgrading purification process and system - Google Patents
High-dust-content coal tar separation and upgrading purification process and system Download PDFInfo
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- CN103666513B CN103666513B CN201310638614.8A CN201310638614A CN103666513B CN 103666513 B CN103666513 B CN 103666513B CN 201310638614 A CN201310638614 A CN 201310638614A CN 103666513 B CN103666513 B CN 103666513B
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Abstract
The invention relates to a high-dust-content coal tar separation and upgrading purification process and a system, and solves the problem that dust of conventional high-dust-content coal tar is difficult to remove, and thus the product quality is affected. The process includes the steps: successively, the high-dust-content coal tar successively passes through a filter to filter dust, then is sent into a feed tank for feeding, next is preheated to 200-250 DEG C or more by preheaters, and finally is sent into a rectifying tower for rectifying to obtain a light component and a heavy component; the light component distilled out of the tower top of the rectifying tower is preheated and dedusted by the first preheater, and then is sent to a tower condenser to be congealed into a liquid to form light tar; the light tar goes out of a tower reflux tank and is divided into three parts, one part flows back to the rectifying tower, another part is sent to a tar mixing tank and is mixed with the high-dust-content coal tar and then together with the coal tar is sent into the filter for filtering the dust, and the remaining part is sent to a light tar storage tank. The process is simple, has the advantages of good coal tar dedusting effect, no waste water discharge and low equipment investment and operation costs, saves energy, reduces consumption, and is friendly to the environment.
Description
Technical field
The present invention relates to a kind of tar process for upgrading and system, a kind of high dustiness coal tar is separated process for upgrading and system specifically.
Background technology
Current China coal tar is mainly with the byproduct that bituminous coal and brown coal are raw material production semicoke, the turnout of the annual semicoke of China is at about 3,000 ten thousand tons, the production of coal tar is refined on the basis that semicoke is produced, according to the output of annual semicoke, coal tar annual output is at about 3,000,000 tons, so large coal tar output, its course of processing is diversified, due to various factors, domestic coal tar processing industrial development is also in the very elementary stage, small scale, state of the art is low, product is few, environment-protective water adjustment is the Actuality Characteristic of China's coal tar processing industry.Domestic modal coal tar processing has following two kinds: one to be coal tar distillation isolation technique, namely each constitutive property in coal tar is utilized to have difference, but the component that character is close is more, various cut is separated with distillation technique, make anthracene, phenol, naphthalene etc. be concentrated in corresponding cut for extraction components product, then adopt physics or chemical process to be separated further; Two is carry out catalytic hydroprocessing to coal tar, produces fuel oil.
Brown coal pyrolysis grading process, comprises gaseous heat-carrier and solid thermal carriers technique, and the dust content in the coal tar obtained is comparatively large, maximumly reaches more than 30%.Brown coal pyrolysis grading process output tar dust content has greatly following reason to cause: one is the poor stability of brown coal, and because water and coal gas are separated out and made coal cinder break during heating, raw gas can take a large amount of coal dusts or semi-coke powder out of; Two is mix with pyrolysis of coal raw gas as the useless flue gas of thermal barrier, and the gentle speed of destructive distillation outlet tolerance increases, and carries coal dust or Dust Capacity increases; Three be coal at pyrolysis grading process, coal becomes dry loose porous structure, and the bulk density of coal generally only has 450-600Kg/Nm
3, the powder phenomenon-tion of pyrolysis grading process coal is also relatively more serious, and coal dust reduces due to density and granularity reduction is very easily taken out of by gas.General brown coal pyrolysis grading process dusty gas process adopts tornado dust collector dedusting, the efficiency of dust collection of tornado dust collector is not high, efficiency of dust collection is generally 80-90%, and the particle being less than 5 μm does not have removal effect substantially, thus cause the dust content in the coal tar obtained in the oily process of receipts comparatively large, be difficult to the dust content in tar to control below 3%.
Dust in the coal tar that brown coal pyrolysis grading process obtains has following feature: (1) coal tar Midst density and granularity all less, density only has 450-600Kg/Nm
3, the granularity of dust of more than 80% is below 20 μm; (2) in coal tar, heavy component is high, and viscosity is large.
Because the coal tar obtained in brown coal pyrolysis grading process has These characteristics, thus be difficult to the dust of coal tar to remove by general filtering separation means, and the dust content in coal tar process for upgrading in coal tar will bring the problems such as hydrotreatment difficulty more than 0.5%wt, reduce the quality of the tar light oil obtained, affect economic return; And by water wash tar exist water loss large, pollute large, need oily water separation to increase the problem of technology difficulty.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, providing that a kind of technique is simple, coal tar good dedusting effect, energy-saving and cost-reducing, non-wastewater discharge, environmentally friendly, that facility investment is low with running cost high dustiness coal tar is separated process for upgrading.
The present invention also provides a kind of system for above-mentioned technique, has that system is simple, facility investment and a low advantage of running cost.
Technical scheme comprises high dustiness coal tar and is filtered dust successively, then charging stock tank charging is sent into, after preheater preheats is extremely to more than 200-250 DEG C, send into rectifying tower rectifying again and obtain light component and heavy component, sending into tower condenser condenses after coal tar after described light component is distillated by rectifying tower tower top after described preheater preheats dedusting again becomes liquid state to form tar light oil, tar light oil is divided into three parts after going out tower backflash, a part passes back into rectifying tower, another part deliver to tar mixing tank and high dustiness coal tar mixed after after again together with send into metre filter dust, remaining part send tar light oil storage tank.
The tar light oil of described feeding tar mixing tank is 0.1-1 with the mixing quality ratio of high dustiness coal tar.Described strainer is sintering metal formula strainer.
Control described tar light oil and the mixed temperature of high dustiness coal tar is 50-70 DEG C.
Control described tar light oil and the mixed viscosity of high dustiness coal tar is reduced to below 5cP.
Described strainer is sintering metal formula strainer, and the coal dust content in the coal tar after dedusting is less than 0.01%wt.
Described preheater comprises #1 preheater and #2 preheater, and after the dedusting of being drawn by described charging stock tank, coal tar sends into rectifying tower more successively after #1 preheater and #2 preheater preheats; Tower condenser is sent into after the coal tar of the light component distillated by described rectifying tower tower top after the dedusting of #1 preheater preheats; Heavy component at the bottom of described rectifying tower be after tower bottom reboiler heat supply again after the further preheating dedusting of #2 preheater after coal tar, send into vapour generator byproduct steam again and be cooled to less than 170 DEG C and form heavy asphaltic oil, described heavy asphaltic oil send cooling forming in heavy asphaltic oil storage tank.
High dustiness coal tar of the present invention is separated upgrading system, comprise the strainer, charging stock tank, preheater and the rectifying tower that connect successively, described rectifying tower tower top outlet is connected with tower condenser, tower backflash through preheater, the outlet of described tower backflash is connected with rectifier column reflux entrance, tar mixing tank and tar storage tank respectively, and described tar mixing tank outlet is connected with strainer.
Described preheater comprises #1 preheater and #2 preheater, and described tar mixing tank is connected with #1 preheater, #2 preheater and rectifying tower successively, and the tower top outlet of described rectifying tower is connected with tower condenser through #1 preheater; The tower bottom outlet of described rectifying tower is connected with heavy asphaltic oil storage tank through reboiler, #2 preheater, vapour generator.
Described strainer preferred sintering metal formula strainer.
Described high dustiness coal tar refers to that dustiness is the coal tar being greater than 3%wt.
The light tar that the present invention adopts rectifying tower to distillate is as being diluent media, with high dustiness coal tar mixed diluting, by the control to temperature and addition, after making mixing, the viscosity of tar reduces, to meet the requirement of filtering separation, thus make the dustiness of the coal tar before entering rectifying tower be down to below 0.01%wt, substantially increase the quality of finished product.And utilize self-produced tar light oil part reuse, can continuous operation be realized, avoid and wash that the facility investment that dedusting brings is high, oily water separation is difficult, a large amount of waste water produces, the problems such as contaminate environment with water.
On the other hand, utilize preheater fully to reclaim the energy heat of heavy asphaltic oil of drawing through reboiler at the bottom of overhead light tar and tower, and for the preheating of coal tar before rectifying, the effect of rectifying can be ensured further.Carry out all right byproduct steam further of the oil of the heavy pitch prill after preheating, the heavy pitch prill cooled down oil is curable to facilitate its storage, transport and utilization.
In the present invention, tar light oil and the mixed temperature of high dustiness coal tar preferably control at 50-70 DEG C, this determines according to the coal dust characteristic in burnt oil properties and tar, temperature is too high, and to add thermal tar energy loss larger, temperature is crossed low tar viscosity and is difficult to more greatly pass through strainer, compare by further studying, preferably control described tar light oil and the mixed viscosity of high dustiness coal tar is reduced to below 5cP, the requirement of filtration can be better met under this viscosity, improve the efficiency and effect of filtering.
Beneficial effect:
1, technology utilization light tar of the present invention dilutes high dustiness coal tar, reduces its viscosity, meets the requirement of filtering separation, and the coal dust content in the tar after filtration treatment is less than 0.01%wt.
2, tar separation process is using tar light oil as solvent cut high dustiness coal tar, do not consume fresh water, also waste water is not produced, do not cause environmental pollution, dust in tar is separated step by step with heavy component, the light tar product of high-quality can be obtained, this technique water saving, energy-conservation, reduce in facility investment and running cost, raising product quality etc. and have outstanding advantage, be specially adapted to high dustiness coal tar oil separating and upgrading.
3, present invention process flow process takes into full account energy-conservation setting, first utilizes out rectifying tower oil gas to carry out preheating to entering rectifying tower tar, and the hard pitch oil recycling out reboiler carries out preheating to feed coal tar, and byproduct steam, energy recovery rate is high.
4, present invention process flow process tar light oil internal circulating load determines according to the physical property of high dustiness coal tar, and the mass ratio of dilution tar light oil and high dustiness coal tar generally can be controlled in 0.1-1, without the need to outsourcing light oil during normal running.
Accompanying drawing explanation
Fig. 1 is present invention process schema and system diagram.
Wherein, 1-rectifying tower, 2-reboiler, 3-tower condenser, 4-tower backflash, 5-tar light oil pump, 6-column bottoms pump, 7-#2 preheater, 8-vapour generator, 9-#1 preheater, 10-tar mixing tank, 11-discharging pump, 12-tar filter, 13-charging stock tank, 14-fresh feed pump, 15-heavy bitumen oil tank, 16-tar light oil storage tank.
Embodiment
Below in conjunction with accompanying drawing, explanation is further expalined to present system:
Tar mixing tank 10 and discharging pump 11, strainer 12(are sintering metal formula strainer), the shell side of charging stock tank 13, fresh feed pump 14, #1 preheater 9, the shell side of #2 preheater 7 and rectifying tower 1 be connected successively, described rectifying tower 1 tower top outlet is connected with tower condenser 3, tower backflash 4 successively through the tube side of #1 preheater 9, and the outlet of described tower backflash 4 is connected with rectifier column reflux entrance, tar mixing tank 10 and tar storage tank 16 respectively.The tower bottom outlet of described rectifying tower 1 is connected with heavy asphaltic oil storage tank 15 through the tube side of reboiler 2, column bottoms pump 6, #2 preheater 7, vapour generator 8.
Process embodiments:
High dustiness coal tar (dustiness is greater than 3%) mixes in tar mixing tank 10 with the tar light oil from tower backflash 4, controlling the tar light oil of described feeding tar mixing tank 10 with the mixing quality ratio of high dustiness coal tar is 0.1-1, mixed temperature is 50-70 DEG C, and mixed viscosity is reduced to below 5cP.Mixed high dustiness coal tar is delivered to strainer 12 through discharging pump 11 pressurization and is filtered, the dustiness in coal tar is made to be less than 0.01%wt, coal tar after dedusting is preheated to 160-180 DEG C through #1 preheater 9 and the tar light oil indirect heat exchange from rectifying tower tower top, and then through #2 preheater 7 and the heavy asphaltic oil indirect heat exchange from reboiler 2, after being preheated to 200-250 DEG C further, send into rectifying tower 1 rectifying and obtain light component and heavy component, coal tar after described light component is distillated by rectifying tower 1 tower top after #1 preheater 9 preheating dedusting is also sent into tower condenser 3 again and is condensed into further and liquid forms tar light oil after being cooled to 180 DEG C, tar light oil is sent into and is collected into tower backflash 4, the tar light oil gone out after tower backflash 4 is divided into three parts, a part enters rectifying tower 1 for the cooling that refluxes through rectifier column reflux inlet return, another part to deliver to as solvent after tar light oil pump 5 pressurizes tar mixing tank 10 mixed with high dustiness coal tar after after again together with send into strainer 12 filter dust, remaining part delivers to tar light oil storage tank 16 through tar light oil pump 5 pressurization.
Heavy component at the bottom of described rectifying tower 1 tower is coal tar being cooled to after #2 preheater 7 further preheating dedusting again after tower bottom reboiler 2 heat supply.。。After, then send into vapour generator 8 by-product pressure and be.。。Steam and be cooled to less than 170 DEG C and form heavy asphaltic oil, described heavy asphaltic oil send cooling forming in heavy asphaltic oil storage tank 15.
The dustiness of the tar light oil finally obtained is less than 0.01%wt, the dustiness of heavy asphaltic oil is 0.1%wt, the system of year process 200,000 tons of raw materials, every year can by-product 3-4 ten thousand tons of low-pressure steam through present invention process, in removed by filtration tar more than 99.9% coal dust, except the reliable and stable tar light oil of guarantee and heavy bitumen oil quality, also has considerable additional economic benefit.
Claims (9)
1. one kind high dustiness coal tar is separated process for upgrading, high dustiness coal tar is filtered dust successively, then charging stock tank charging is sent into, after preheater preheats is extremely to 200-250 DEG C, send into rectifying tower rectifying again and obtain light component and heavy component, it is characterized in that, sending into tower condenser condenses after coal tar after described light component is distillated by rectifying tower tower top after described preheater preheats dedusting again becomes liquid state to form tar light oil, tar light oil is divided into three parts after going out tower backflash, a part passes back into rectifying tower, another part deliver to tar mixing tank and high dustiness coal tar mixed after after again together with send into metre filter dust, remaining part send tar light oil storage tank.
2. high dustiness coal tar as claimed in claim 1 is separated process for upgrading, and it is characterized in that, the tar light oil of described feeding tar mixing tank is 0.1-1 with the mixing quality ratio of high dustiness coal tar, and described strainer is sintering metal formula strainer.
3. high dustiness coal tar as claimed in claim 1 is separated process for upgrading, it is characterized in that, controls described tar light oil and the mixed temperature of high dustiness coal tar is 50-70 DEG C.
4. high dustiness coal tar as claimed in claim 1 is separated process for upgrading, it is characterized in that, controls described tar light oil and the mixed viscosity of high dustiness coal tar is reduced to below 5cP.
5. the high dustiness coal tar as described in any one of claim 1-4 is separated process for upgrading, and it is characterized in that, described strainer is sintering metal formula strainer, and the coal dust content in the coal tar after dedusting is less than 0.01%wt.
6. high dustiness coal tar as claimed in claim 1 is separated process for upgrading, it is characterized in that, described preheater comprises #1 preheater and #2 preheater, and after the dedusting of being drawn by described charging stock tank, coal tar sends into rectifying tower more successively after #1 preheater and #2 preheater preheats; Tower condenser is sent into after the coal tar of the light component distillated by described rectifying tower tower top after the dedusting of #1 preheater preheats; Heavy component at the bottom of described rectifying tower be after tower bottom reboiler heat supply again after the further preheating dedusting of #2 preheater after coal tar, send into vapour generator byproduct steam again and be cooled to less than 170 DEG C and form heavy asphaltic oil, described heavy asphaltic oil send cooling forming in heavy asphaltic oil storage tank.
7. one kind high dustiness coal tar is separated upgrading system, comprise the strainer, charging stock tank, preheater and the rectifying tower that connect successively, it is characterized in that, described rectifying tower tower top outlet is connected with tower condenser, tower backflash through preheater, the outlet of described tower backflash is connected with rectifier column reflux entrance, tar mixing tank and tar storage tank respectively, and described tar mixing tank outlet is connected with strainer.
8. high dustiness coal tar as claimed in claim 7 is separated upgrading system, it is characterized in that, described preheater comprises #1 preheater and #2 preheater, described tar mixing tank is connected with #1 preheater, #2 preheater and rectifying tower successively, and the tower top outlet of described rectifying tower is connected with tower condenser through #1 preheater; The tower bottom outlet of described rectifying tower is connected with heavy asphaltic oil storage tank through reboiler, #2 preheater, vapour generator.
9. high dustiness coal tar as claimed in claim 7 or 8 is separated upgrading system, and it is characterized in that, described strainer is sintering metal formula strainer.
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| CN105602614B (en) * | 2014-11-23 | 2017-12-15 | 胜帮科技股份有限公司 | Dust-laden crosses gasification oil gas condensation separation method |
| CN106994278B (en) * | 2017-04-06 | 2019-03-01 | 西安交通大学 | Experimental method and device for the purification of pulverized coal pyrolysis high temperature dust tar step |
| CN108342212B (en) * | 2018-01-23 | 2019-04-12 | 陕西煤业化工集团神木天元化工有限公司 | Handle the method and system of slag inclusion coal tar |
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