CN203653487U - High dust content coal tar separating and upgrading device - Google Patents
High dust content coal tar separating and upgrading device Download PDFInfo
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- CN203653487U CN203653487U CN201320784154.5U CN201320784154U CN203653487U CN 203653487 U CN203653487 U CN 203653487U CN 201320784154 U CN201320784154 U CN 201320784154U CN 203653487 U CN203653487 U CN 203653487U
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Abstract
The utility model relates to a high dust content coal tar separating and upgrading device, in order to solve the problems of the existing high dust content coal tar which difficultly removes dust and results in affect on product quality. The technical scheme comprises a filter, a feed tank, a preheater and a rectifying tower which are sequentially connected, and is characterized in that an overhead outlet of the rectifying tower is connected to a tower condenser and a tower reflux tank through the preheater; an outlet of the tower reflux tank is respectively connected to a reflux inlet of the rectifying tower, a tar mixing tank and a tar storage tank; an outlet of the tar mixing tank is connected to the filter. The separating and upgrading device disclosed by the utility model is simple in system, good in coal tar dust removal effect, energy-saving and cost-reducing, free from wastewater discharge, environmental friendly, and low in equipment investment and running cost.
Description
Technical field
The utility model relates to a kind of tar upgrading system, and a kind of high dustiness coal tar separates upgrading system specifically.
Background technology
The at present mainly byproduct taking bituminous coal and brown coal as raw material production semicoke of China's coal tar, the turnout of the annual semicoke of China is 3,000 ten thousand tons of left and right, the production of coal tar is to refine on the basis producing at semicoke, according to the output of annual semicoke, coal tar annual output is 3,000,000 tons of left and right, 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: the one, and coal tar distillation isolation technique, utilize each constitutive property in coal tar to have difference, but the component that character is close is more, separate various cuts with distillation technique, the wish extraction components products such as anthracene, phenol, naphthalene are concentrated in corresponding cut, more further adopt physics or chemical process to separate; The 2nd, coal tar is carried out to catalytic hydroprocessing, produce fuel oil.
Brown improving quality of coal by pyrolysis process, comprises gaseous heat-carrier and solid thermal carriers technique, and the dust content in the coal tar obtaining is larger, and maximum can reach more than 30%.Brown improving quality of coal by pyrolysis process output tar dust content has greatly following reason to cause: the one, and the poor stability of brown coal, separates out coal cinder is broken because of water and coal gas when heating, and raw gas can be taken a large amount of coal dusts or semi-coke powder out of; The 2nd, to mix with pyrolysis of coal raw gas as the useless flue gas of thermal barrier, the gentle speed of destructive distillation outlet tolerance increases, and carrying coal dust or Dust Capacity increases; The 3rd, coal is in pyrolysis upgrading process, and coal has become dry loose porous structure, and the bulk density of coal generally only has 450-600Kg/Nm3, and the powder phenomenon-tion of pyrolysis upgrading process coal is also more serious, and coal dust is because density reduces to reduce and very easily taken out of by gas with granularity.General brown improving quality of coal by pyrolysis process dusty gas is processed and is adopted 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 that is less than 5 μ m does not have removal effect substantially, thereby the dust content in the coal tar that causes obtaining in the oily process of receipts is larger, is difficult to the dust content in tar to be controlled at below 3%.
Dust in the coal tar that brown improving quality of coal by pyrolysis process obtains has following feature: in (1) coal tar, density and granularity are all less, and density only has 450-600Kg/Nm3, and more than 80% granularity of dust is below 20 μ m; (2) in coal tar, heavy component is high, and viscosity is large.
Because the coal tar obtaining in brown improving quality of coal by pyrolysis process has These characteristics, thereby be difficult to the dust of coal tar to remove by general filtering separation means, and in coal tar process for upgrading, the dust content in coal tar exceedes 0.5%wt and will bring the problems such as hydrotreatment difficulty, the quality that reduces the tar light oil obtaining, affects economic return; And by water wash tar exist water loss large, pollute greatly, need oily water separation to increase the problem of technology difficulty.
Summary of the invention
The purpose of this utility model is in order to solve the problems of the technologies described above, and provides that a kind of system is simple, coal tar good dedusting effect, energy-saving and cost-reducing, non-wastewater discharge, the high dustiness coal tar that environmentally friendly, facility investment is low with running cost separates upgrading system.
The high dustiness coal tar of the utility model separates 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 rectifying tower reflux inlet, 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.
The preferred sintering metal formula of described strainer strainer.
Adopt the technique of said system to comprise that high dustiness coal tar is filtered dust successively, then send into charging stock tank charging, after preheater is preheated to more than 200-250 DEG C, send into again rectifying tower rectifying and obtain light component and heavy component, after coal tar after described light component is distillated by rectifying tower tower top after described preheater preheating dedusting, send into again tower condenser condenses and become the liquid tar light oil that forms, 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 send into strainer together with again and filter dust, remaining part send tar light oil storage tank.
Describedly send into the tar light oil of tar mixing tank and the mixing quality ratio of high dustiness coal tar is 0.1-1.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 reduced viscosity of high dustiness coal tar 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 is sent into rectifying tower successively after #1 preheater and the preheating of #2 preheater again; After the coal tar of the light component being distillated by described rectifying tower tower top after #1 preheater preheating dedusting, send into tower condenser; 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 170 DEG C of following heavy asphaltic oils that form, described heavy asphaltic oil send cooling forming in heavy asphaltic oil storage tank.
Described high dustiness coal tar refers to that dustiness is the coal tar that is greater than 3%wt.
The lightweight coal tar that the utility model employing rectifying tower distillates is as being diluent media, with high dustiness coal tar mixed diluting, by the control to temperature and addition, make to mix the reduced viscosity of rear tar, to meet the requirement of filtering separation, thereby the dustiness that makes to enter the coal tar before rectifying tower is down to below 0.01%wt, greatly improve the quality of finished product.And utilize self-produced tar light oil part reuse, can realize continuous operation, avoided washing with water 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.
On the other hand, the energy heat of the heavy asphaltic oil of drawing through reboiler at the bottom of utilizing preheater to tower top tar light oil and tower fully reclaims, and for the preheating of coal tar before rectifying, can further ensure the effect of rectifying.Carry out the further byproduct steam of heavy pitch prill oil after preheating, the heavy pitch prill cooling down oil is curable to facilitate its storage, transport and to utilize.
In the utility model, tar light oil and the mixed temperature of high dustiness coal tar are preferably controlled at 50-70 DEG C, this is to determine according to the coal dust characteristic in burnt oil properties and tar, it is larger that excess Temperature adds thermal tar energy loss, temperature is crossed low tar viscosity and is difficult to more greatly pass through strainer, by further research comparison, preferably control described tar light oil and the mixed reduced viscosity of high dustiness coal tar below 5cP, under this viscosity, can better meet the requirement of filtration, improve efficiency and the effect of filtering.
Beneficial effect:
1, the utility model utilizes lightweight coal tar to dilute 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 the high dustiness coal tar of solvent cut, do not consume fresh water, do not produce waste water yet, do not cause environmental pollution, dust in tar separates step by step with heavy component, can obtain the lightweight coal-tar products of high-quality, this technique water saving, energy-conservation, reduce the aspects such as facility investment and running cost, raising product quality and have outstanding advantage, be specially adapted to high dustiness coal tar oil separating and upgrading.
3, the utility model system flow takes into full account energy-conservation setting, first utilize out rectifying tower oil gas to carry out preheating to entering rectifying tower tar, the hard pitch oil that recycles out reboiler carries out preheating to feed coal tar, and byproduct steam, energy recovery rate is high, system is simple, easy and simple to handle, facility investment and running cost are low.
4, in the utility model system, tar light oil internal circulating load determines according to the physical property of high dustiness coal tar, and dilution generally can be controlled in 0.1-1 with the mass ratio of tar light oil and high dustiness coal tar, when normal running without outsourcing light oil.
Brief description of the drawings
Fig. 1 is the utility model process flow sheet 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, the utility model system is further expalined to explanation:
Technological process embodiment:
High dustiness coal tar (dustiness is greater than 3%) and tar light oil from tower backflash 4 mix tar mixing tank 10 is interior, described in control, send into the tar light oil of tar mixing tank 10 and the mixing quality ratio of high dustiness coal tar is 0.1-1, mixed temperature is 50-70 DEG C, and mixed reduced viscosity is below 5cP.Mixed high dustiness coal tar is delivered to strainer 12 through discharging pump 11 pressurizations and is filtered, make the dustiness in coal tar be less than 0.01%wt, coal tar after dedusting is through #1 preheater 9 and be preheated to 160-180 DEG C from the tar light oil indirect heat exchange of rectifying tower tower top, and then through #2 preheater 7 and heavy asphaltic oil indirect heat exchange from reboiler 2, further be preheated to after 200-250 DEG C, 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 the 9 preheating dedustings of #1 preheater and be cooled to 180 DEG C after send into again tower condenser 3 and be further condensed into the liquid tar light oil that forms, tar light oil is sent into into tower backflash 4 and is collected, the tar light oil going out after tower backflash 4 is divided into three parts, a part passes back into rectifying tower 1 for the cooling that refluxes through rectifying tower reflux inlet, another part after tar light oil pump 5 pressurization, deliver to as solvent tar mixing tank 10 mixed with high dustiness coal tar after after send into strainer 12 together with again and filter dust, remaining part is delivered to tar light oil storage tank 16 through 5 pressurizations of tar light oil pump.
Heavy component at the bottom of described rectifying tower 1 tower is after after tower bottom reboiler 2 heat supplies, after the further preheating dedusting of #2 preheater 7, coal tar is also lowered the temperature again, send into the steam of vapour generator 8 by-products again and be cooled to 170 DEG C of following heavy asphaltic oils that form, described heavy asphaltic oil send cooling forming in heavy asphaltic oil storage tank 15.
The dustiness of the tar light oil finally obtaining is less than 0.01%wt, the dustiness of heavy asphaltic oil is 0.1%wt, year is processed the system of 200,000 tons of raw materials, every year can 3-4 ten thousand tons of low-pressure steam of by-product through the utility model technique, cross and filter out more than 99.9% coal dust in tar, except ensureing, reliable and stable tar light oil and heavy bitumen oil quality, to also have considerable additional economic benefit.
Claims (3)
1. one kind high dustiness coal tar separates 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 rectifying tower reflux inlet, tar mixing tank and tar storage tank respectively, and described tar mixing tank outlet is connected with strainer.
2. high dustiness coal tar as claimed in claim 1 separates 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.
3. high dustiness coal tar as claimed in claim 1 or 2 separates upgrading system, it is characterized in that, described strainer is sintering metal formula strainer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320784154.5U CN203653487U (en) | 2013-11-29 | 2013-11-29 | High dust content coal tar separating and upgrading device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320784154.5U CN203653487U (en) | 2013-11-29 | 2013-11-29 | High dust content coal tar separating and upgrading device |
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| CN203653487U true CN203653487U (en) | 2014-06-18 |
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| CN201320784154.5U Withdrawn - After Issue CN203653487U (en) | 2013-11-29 | 2013-11-29 | High dust content coal tar separating and upgrading device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103666513A (en) * | 2013-11-29 | 2014-03-26 | 中国五环工程有限公司 | High-dust-content coal tar separation and upgrading purification process and system |
| CN105419835A (en) * | 2015-11-30 | 2016-03-23 | 华电重工股份有限公司 | Processing method of coal low-temperature pyrolysis volatile component |
-
2013
- 2013-11-29 CN CN201320784154.5U patent/CN203653487U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103666513A (en) * | 2013-11-29 | 2014-03-26 | 中国五环工程有限公司 | High-dust-content coal tar separation and upgrading purification process and system |
| CN103666513B (en) * | 2013-11-29 | 2015-02-04 | 中国五环工程有限公司 | High-dust-content coal tar separation and upgrading purification process and system |
| CN105419835A (en) * | 2015-11-30 | 2016-03-23 | 华电重工股份有限公司 | Processing method of coal low-temperature pyrolysis volatile component |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140618 Effective date of abandoning: 20150204 |
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| RGAV | Abandon patent right to avoid regrant |