CN203462016U - Raw coke oven gas dust removal device - Google Patents

Raw coke oven gas dust removal device Download PDF

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Publication number
CN203462016U
CN203462016U CN201320570485.9U CN201320570485U CN203462016U CN 203462016 U CN203462016 U CN 203462016U CN 201320570485 U CN201320570485 U CN 201320570485U CN 203462016 U CN203462016 U CN 203462016U
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China
Prior art keywords
gas
pipeline
dust removal
blowback
coke oven
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Expired - Fee Related
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CN201320570485.9U
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Chinese (zh)
Inventor
杨占彪
王树宽
于广彦
万宝良
柴宗成
贺志宝
史宏伟
郭生飞
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SHENMUFUYOU ENERGY TECHNOLOGY Co Ltd
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SHENMUFUYOU ENERGY TECHNOLOGY Co Ltd
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Abstract

The utility model relates to a raw coke oven gas dust removal device. The raw coke oven gas dust removal device comprises at least one dust removal unit, wherein the dust removal unit comprises a filter which is respectively communicated with a raw coke oven gas pipeline, a coal gas cooler and a replaced gas pipeline, the coal gas cooler is communicated with a bag-type dust collector which is communicated with an oil-free gas pipeline and a circulating fan, the circulating fan is communicated with a coal gas heater, a purified gas discharging port at the bottom of the filter is communicated with a purified gas discharging pipeline, a blowback gas inlet and a blowback gas pipeline, and the blowback gas pipeline is communicated with a gas change pipeline and the coal gas heater. The raw coke oven gas dust removal device is simple in structure, stable in operation, low in energy consumption and high in filtration efficiency and is not provided with a circulating soot blowing regeneration system; by adopting the raw coke oven gas dust removal device, bed materials do not need to circulate, so that filter materials are prevented from being crushed and wearing equipment in a filtering process; the multiple raw coke oven gas dust removal devices can be connected in parallel and combined for filtration.

Description

A kind of raw gas cleaning apparatus
Technical field
The utility model belongs to technical field of coal chemical industry oil-containing gas high-temperature dust removal, is specifically related to the cleaning apparatus of the raw gas that produces in pulverized coal pyrolysis preparing coal tar process.
Background technology
In recent years, low-temperature pyrolysis of coal preparing coal tar has been had widely to research both at home and abroad, but a large amount of containing coke powder raw gas owing to containing in the raw gas that the process of producing produces, dedusting does not have breakthrough progress, is seriously restricting the development of this industry.
For a kind of raw gas dedusting, have three kinds of methods at present, first method is to adopt knockdown cyclonic separator, and separation efficiency is low, cannot the following coal dust of separated 5 μ m, and producing a large amount of greasy filth also cannot separation; Second method is electric precipitation, and because the raw gas temperature containing tar is lower than tar condensation point meeting condensation, electric precipitation need at high temperature move, the high temperature corrosion of wire electrode cannot solve, and electric precipitation is due to bulky, tar overstand, second pyrolysis seriously can cause the yield of tar to decline; The third method is that pottery, powder metal pipe automatic back blow filter, and under high temperature, raw gas constantly raises pressure reduction at tube-surface carbon distribution, and blowback cannot make filter cake come off, and causes the device can not long-term operation.
Utility model content
The purpose of this utility model is to overcome the existing deficiency of raw gas cleaning apparatus, a kind of granular-bed filter dedusting that utilizes fixed bed filtering and fluidized-bed blowback coupling is provided, at high temperature effectively make solid dust and gas-oil separation in raw gas, the raw gas cleaning apparatus stable, efficiency of dust collection is high.
Solving the problems of the technologies described above adopted technical scheme is:
Raw gas cleaning apparatus is comprised of at least one dust removing units, dust removing units comprises strainer, the top of strainer is communicated with raw coke oven gas pipeline outlet by raw gas control valve, by blowback air air outlet valve, be connected with the air intake of gas cooler, by displacement gas control valve and displacement gas pipeline communication, the air outlet of gas cooler is connected with the inlet mouth of sack cleaner by pipeline, the outlet pipe of sack cleaner with without oil gas body device for cleaning pipeline, cross the first T-shaped valve and be connected with the entrance of recirculation blower, the outlet of recirculation blower is connected with the inlet mouth of gas heater by pipeline, the bottom purified gas relief outlet of strainer is communicated with purified gas discharge tube by purified gas control valve, blowback air inlet mouth is by blowback air air intake control valve and blowback air pipeline communication, blowback air pipeline is connected with the air outlet of gas heater by the second T-shaped valve with air refreshing tube,
The structure of above-mentioned strainer is: in tank body, be disposed with collection chamber from top to bottom, filter bed, support bed and lower collection chamber.
Above-mentioned filtration bed is comprised of filtering layer and the current stabilization layer that is arranged on filtering layer bottom.
Above-mentioned filtering layer is up big and down small by interlayer particle diameter, bulk density is up-small and down-big fine perlite or pitchstone, hollow glass bead, hollow alumina ball, super light ceramisite, float stone, float in pearl, obsidian, closed-cell foam metal any one or two kinds form; its particle size distribution range is 1.5~6mm; filtering layer thickness is 200~400mm, and bulk density is 60~800kg/m 3.
Above-mentioned current stabilization layer is that any one or two kinds in large little inert ceramic balls or quartz sand, peridotites, yellow sand, pebbles, Metal Ball under large little, bulk density under interlayer particle diameter form, its particle size distribution range is 0.5~9mm, current stabilization layer thickness is 300~600mm, and bulk density is 1100~4000kg/m 3.
Above-mentioned support bed is comprised of flase floor and the Johnson Net that is arranged on flase floor top.
The grid of above-mentioned flase floor is spaced apart 20~80mm, and the grating of Johnson Net is spaced apart 3~7mm.
Above-mentioned dust removing units can be connected in parallel 8~16 by pipeline.
The raw gas cleaning apparatus that the utility model provides is to have utilized fixed bed filtering and fluidized-bed blowback coupling, rebuilding, after raw gas filters, first with oil-free coal gas or nitrogen or steam, first replace, then blowback, gas cooling after blowback is by sack cleaner dedusting, and heating enters systemic circulation utilization, and whole apparatus structure is simple, stable, energy consumption is low, filtration efficiency is high, grey regeneration system rapidly is not blown in circulation, bed material has been avoided filtrate broken and wearing and tearing to equipment in filtration procedure without circulation, and strainer of the present utility model adopts the resistant to elevated temperatures flase floor to add Johnson Net to support, and current stabilization layer adopts porcelain ball or quartz sand (sea sand), peridotites, pebbles, yellow sand, Metal Ball is one or both combinations wherein, and granularity and bulk density adopt lower large little distribution, and filtering layer adopts fine perlite or pitchstone, hollow glass bead, hollow alumina ball, super light ceramisite, float stone, float pearl, obsidian, one or both combinations in closed-cell foam metal, granularity is up big and down small, the up-small and down-big layout of bulk density, makes whole filtration bed become gradient filtration, when not reducing filtration efficiency, has increased the dustiness of unit volume gas, avoids occurring surface knot layer, the phenomenon that pressure reduction raises suddenly, dust removing units of the present utility model can adopt many cover parallel combinations to filter in addition, and wherein a blowback, realizes non-stop run, greatly improves except dust quantity and efficiency of dust collection.
Accompanying drawing explanation
Fig. 1 is the dust removing units workflow diagram of embodiment 1.
Fig. 2 is the structural representation of the strainer 4 in Fig. 1.
Embodiment
Now in conjunction with the accompanying drawings and embodiments the technical solution of the utility model is further described, but the utility model is not only confined to following embodiment.
Embodiment 1
The dust-laden raw gas that the treatment temp of take is 4~10KPa as 350~600 ℃, pressure is example, the cleaning apparatus of the present embodiment by one independently dust removing units form, referring to Fig. 1, this dust removing units comprises displacement, blowback gas tank 1, raw coke oven gas pipeline 2, raw gas control valve 3, strainer 4, displacement gas control valve 5, blowback air air outlet valve 6, gas cooler 7, sack cleaner 8, without the T-shaped valve 10 of oily gas control valve 9, first, recirculation blower 11, the T-shaped valve 13 of well heater 12, second, blowback air intake valve 14 and purified gas control valve 15, connects and composes.
The top of the strainer 4 of the present embodiment is processed with air inlet port and production well, a threeway is installed on air inlet port, a mouth of this threeway by raw coke oven gas pipeline 2 pass into raw gas, another mouthful of linker substitution feed channel passes into substitution gas, raw gas control valve 3 is installed on raw coke oven gas pipeline 2, the break-make of controlling raw gas is provided with displacement gas control valve 5 on displacement gas pipeline, controls the break-make of displacement gas, when passing into raw gas, close displacement gas control valve 5; When passing into displacement gas, close raw gas control valve 3.The production well at strainer 4 tops is communicated with gas cooler 7 by blowback air gas exhaust duct, blowback air air outlet valve 6 is installed on blowback air gas exhaust duct, for the interior blowback air of controlled filter device 4, discharge, the air outlet of gas cooler 7 is communicated with the inlet mouth of sack cleaner 8 by pipeline, after blowback air is cooling, carry out dedusting, and then recycle, the outlet pipe of sack cleaner 8 with without oily gas pipeline, be connected in two vertical duct of the first T-shaped valve 10, another pipeline of the first T-shaped valve 10 is communicated with the entrance of recirculation blower 11 by pipeline, the outlet of recirculation blower 11 is communicated with the inlet mouth of well heater 12 by pipeline, that by well heater 12, recirculation blower 11 is carried carries out heat temperature raising processing without oil gas body, on without oily gas pipeline, be provided with without oily gas control valve 9, control supplements without oil gas body, the present embodiment without oil gas body, be coal gas or nitrogen or steam, this is without oily gas pipeline and displacement, blowback gas tank 1 is communicated with, utilize after the clean coal gas heat temperature raising containing oil content and grit and pass in strainer 4 and replace or blowback.In strainer 4 bottoms, be processed with purified gas relief outlet and blowback air inlet mouth, purified gas relief outlet is communicated with purified gas discharge tube by purified gas control valve 15, blowback air inlet mouth is by blowback air intake valve 14 and blowback air pipeline communication, and blowback air pipeline is communicated with the outlet side of gas heater 12 by the second T-shaped valve 13 with the other end of displacement gas pipeline.
Referring to Fig. 2, above-mentioned strainer 4 is that upper collection chamber 4-2, filtering layer 4-3, current stabilization layer 4-4, Johnson Net 4-5, flase floor 4-6 and the lower collection chamber 4-7 of setting form from top to bottom by tank body 4-1 and in tank body 4-1.
Above-mentioned filtering layer 4-3 is combined with the current stabilization layer 4-4 of the coaxial setting in filtering layer 4-3 bottom and is formed the filtration bed of strainer 4, with filtering layer 4-3 and two groups of bed combined filterings of current stabilization layer 4-4.The filtering layer 4-3 of the present embodiment adopts fine perlite as filtrate, filtrate thickness is 300mm, fine perlite becomes the Gradient distribution of uniform gradient series according to the up big and down small order of interlayer particle diameter, particle diameter is 6mm~1.5mm from top to bottom, difference is 0.5, bulk density becomes the Gradient distribution of uniform gradient series according to up-small and down-big order, bulk density is respectively 60~800kg/m from top to bottom 3, difference is 80.Current stabilization layer 4-4 adopts inert ceramic balls as major ingredient, its thickness is 400mm, it becomes Gradient distribution according to up-small and down-big order, and to be respectively 0.5~9mm be 0.5 to be uniform gradient series according to difference to particle diameter from top to bottom, and bulk density is distributed as 1100~4000kg/m from top to bottom 3, according to difference, be 170 to be uniform gradient series and to distribute.
The coaxial flase floor 4-6 arranging in above-mentioned Johnson Net 4-5 and Johnson Net 4-5 bottom constitutes the support bed of the present embodiment, and Johnson Net 4-5 adopts resistant to elevated temperatures sieve-board type Johnson Net 4-5, and its grating is spaced apart 5mm.Flase floor 4-6 adopts high temperature material, and its grid is spaced apart 50mm.
By the method that said apparatus carries out dedusting to raw gas, by following steps, formed:
(1) open raw gas control valve 3 and purified gas control valve 15, close displacement gas control valve 5 and blowback air air outlet valve 6, blowback air air intake control valve 14, raw gas in raw coke oven gas pipeline 2 is delivered in the upper collection chamber 4-2 of strainer 4 by raw gas control valve 3, through filtering layer 4-3, current stabilization layer 4-4, filter again, the raw gas purifying moves in lower collection chamber 4-7, by purified gas discharge line, discharges;
(2) in filtration procedure, the grit in raw gas is intercepted in filtrate, when the pressure reduction between filtering layer 4-3 and current stabilization layer 4-4 reaches 7KPa, close raw gas control valve 3, stop carrying raw gas in strainer 4, open without oily gas control valve 9 and displacement gas control valve 5, will be by replacing, being delivered to and carrying out heat temperature raising in well heater 12 through recirculation blower 11 without oil gas in blowback gas tank 1, after temperature increase to 480 ℃, by displacement gas pipeline, be delivered in strainer 4, raw gas in oil-free coal gas and strainer 4 is replaced, raw gas drains in lower collection chamber 4-7 through filtering bed, from purified gas discharge tube, discharge completely, complete the displacement gas stage.
(3) raw gas displacement completely, close purified gas control valve 15 and displacement gas control valve 5, successively open blowback air air outlet valve 6 and blowback air intake valve 14, oil-free coal gas blows to gas heater 12 through recirculation blower 11, after being warming up to 480 ℃, from strainer 4 bottoms, enter in strainer 4, from lower collection chamber 4-7, make progress through current stabilization layer 4-4, filtering layer 4-3 is in upper collection chamber 4-2, the grit depositing in filtering layer 4-3 is carried out to blowback, purge gas is discharged from upper collection chamber 4-2, after cooling by gas cooler 7, in sack cleaner 8, carry out dust removal process, oil-free coal gas recycle after dedusting, mix with the coal gas without carrying in oily gas pipeline, through recirculation blower 11, be delivered in gas heater 12, as current stabilization layer 4-4, pressure reduction between filtering layer 4-3 stops blowback while being returned to original state, close blowback air intake valve 14 and blowback air air outlet valve 6, complete the blowback stage.
(4) repeat above-mentioned step (1)~(3), complete raw gas dedusting.
Embodiment 2
In the present embodiment, filtering layer 4-3 adopts fine perlite as filtrate, and filtrate thickness is 400mm, and fine perlite is that particle diameter is respectively 6~1.5mm from top to bottom according to the up big and down small distribution of interlayer particle, and bulk density is distributed as 60~800kg/m 3.Current stabilization layer 4-4 adopts peridotites to arrange, thickness is 600mm, and peridotites is that particle diameter is respectively 1~8mm from top to bottom according to up-small and down-big order Gradient distribution, and bulk density is 1480~2800kg/m 3.Johnson Net 4-5 adopts resistant to elevated temperatures sieve-board type Johnson Net 4-5, and its grating is spaced apart 3mm.Flase floor 4-6 adopts high temperature material, and its grid is spaced apart 20mm.Other parts and annexation thereof are identical with embodiment 1.
Embodiment 3
In the present embodiment, filtering layer 4-3 adopts float stone as filtrate, and filtrate thickness is 200mm, and float stone is that particle diameter is respectively 3~1.5mm from top to bottom according to the up big and down small distribution of interlayer particle, and bulk density is distributed as 210~360kg/m 3.Current stabilization layer 4-4 adopts Metal Ball to arrange, thickness is 300mm, and Metal Ball is to distribute according to lower large little order, and particle diameter is respectively 1~8mm from top to bottom, and bulk density is 2600~4000kg/m 3.Johnson Net 4-5 adopts resistant to elevated temperatures sieve-board type Johnson Net 4-5, and its grating is spaced apart 7mm.Flase floor 4-6 adopts high temperature material, and its grid is spaced apart 80mm.Other parts and annexation thereof are identical with embodiment 1.
Embodiment 4
In the present embodiment, it is filtrate that filtering layer 4-3 adopts hollow alumina, and filtrate thickness is 400mm, and hollow alumina is that particle diameter is respectively 3~1.5mm from top to bottom according to the up big and down small distribution of particle, and bulk density is respectively 300~600kg/m 3.Current stabilization layer 4-4 adopts porcelain ball to arrange, thickness is 300mm, and porcelain ball is to distribute according to up-small and down-big order, and particle diameter is respectively 9~0.5mm from top to bottom, and bulk density is 1500~2100kg/m 3, Johnson Net 4-5 adopts resistant to elevated temperatures sieve-board type Johnson Net 4-5, and its grating is spaced apart 5mm.Flase floor 4-6 adopts high temperature material, and its grid is spaced apart 60mm.Other parts and annexation thereof are identical with embodiment 1.
Embodiment 5
In the present embodiment, filtering layer 4-3 adopts closed-cell foam metal as filtrate, and filtrate thickness is 300mm, and closed-cell foam metal is that particle diameter is respectively 3~1.5mm from top to bottom according to the up big and down small distribution of particle, and bulk density is respectively 310~800kg/m 3.Current stabilization layer 4-4 adopts pebbles, and thickness is 500mm, and pebbles is to distribute according to up-small and down-big order, and particle diameter is respectively 1~9mm from top to bottom, and bulk density is 1700~2300kg/m 3, Johnson Net 4-5 adopts resistant to elevated temperatures sieve-board type Johnson Net 4-5, and its grating is spaced apart 4mm.Flase floor 4-6 adopts high temperature material, and its grid is spaced apart 70mm.Other parts and annexation thereof are identical with embodiment 1.
Embodiment 6
In the raw gas cleaning apparatus of above-described embodiment 1~5; the filtrate of filtering layer 4-3 can or float pearl or obsidian or closed-cell foam metal are replaced with pitchstone or hollow glass bead or hollow alumina ball or super light ceramisite or float stone; the filtrate of current stabilization layer 4-4 can be replaced by quartz sand (sea sand) or peridotites or yellow sand or pebbles or Metal Ball, and the laying of filtrate and miscellaneous part and annexation thereof are identical with corresponding embodiment.
Embodiment 7
In the raw gas cleaning apparatus of above-described embodiment 1~5; the filtrate of filtering layer 4-3 can be replaced with pitchstone, hollow glass bead, hollow alumina ball, super light ceramisite, float stone or any two kinds of combinations of floating in pearl, obsidian and closed-cell foam metal; the filtrate of current stabilization layer 4-4 can be replaced with any two kinds of combinations in quartz sand (sea sand), peridotites, yellow sand or pebbles and Metal Ball, and the laying of filtrate and miscellaneous part and annexation thereof are identical with corresponding embodiment.
Embodiment 8
The filtration unit of the present embodiment is to be connected in parallel and to be formed by pipeline by 8 dust removing units, the structure of each dust removing units is identical with any one in above-described embodiment 1~10, realizes wherein 7 dust removing units and filters, 1 dust removing units blowback, cycle operation successively, increases work efficiency.
Embodiment 9
The filtration unit of the present embodiment is to be connected in parallel and to be formed by pipeline by 16 dust removing units, the structure of each dust removing units is identical with any one in above-described embodiment 1~10, realizes wherein 15 dust removing units and filters, 1 dust removing units blowback, cycle operation successively, increases work efficiency.

Claims (7)

1. a raw gas cleaning apparatus, it is characterized in that: by least one dust removing units, formed, described dust removing units comprises strainer (4), the top of strainer (4) is communicated with raw coke oven gas pipeline (2) outlet by raw gas control valve (3), by blowback air air outlet valve (6), be connected with the air intake of gas cooler (7), by displacement gas control valve (5) and displacement gas pipeline communication, the air outlet of gas cooler (7) is connected with the inlet mouth of sack cleaner (8) by pipeline, the outlet pipe of sack cleaner (8) and cross the first T-shaped valve (10) without oil gas body device for cleaning pipeline and be connected with the entrance of recirculation blower (11), the outlet of recirculation blower (11) is connected with the inlet mouth of gas heater (12) by pipeline, the bottom purified gas relief outlet of strainer (4) is communicated with purified gas discharge tube by purified gas control valve (15), blowback air inlet mouth is by blowback air air intake control valve (14) and blowback air pipeline communication, blowback air pipeline and air refreshing tube are connected with the air outlet of gas heater (12) by the second T-shaped valve (13),
The structure of above-mentioned strainer (4) is: in tank body (4-1), be disposed with upper collection chamber (4-2) from top to bottom, filter bed, support bed and lower collection chamber (4-7).
2. raw gas cleaning apparatus according to claim 1, is characterized in that: described filtration bed is comprised of filtering layer (4-3) and the current stabilization layer (4-4) that is arranged on filtering layer (4-3) bottom.
3. raw gas cleaning apparatus according to claim 2; it is characterized in that: any one or two kinds that described filtering layer (4-3) is up big and down small by interlayer particle diameter, bulk density is up-small and down-big fine perlite or pitchstone, hollow glass bead, hollow alumina ball, super light ceramisite, float stone, float in pearl, obsidian, closed-cell foam metal form; its particle size distribution range is 1.5~6mm; filtering layer (4-3) thickness is 200~400mm, and bulk density is 60~800kg/m 3.
4. raw gas cleaning apparatus according to claim 2, it is characterized in that: described current stabilization layer (4-4) is that any one or two kinds in large little inert ceramic balls or quartz sand, peridotites, yellow sand, pebbles, Metal Ball under large little, bulk density under interlayer particle diameter form, its particle size distribution range is 0.5~9mm, current stabilization layer (4-4) thickness is 300~600mm, and bulk density is 1100~4000kg/m 3.
5. raw gas cleaning apparatus according to claim 1, is characterized in that: described support bed is comprised of flase floor (4-6) and the Johnson Net (4-5) that is arranged on flase floor (4-6) top.
6. raw gas cleaning apparatus according to claim 5, is characterized in that: the grid of described flase floor (4-6) is spaced apart 20~80mm, and the grating of Johnson Net (4-5) is spaced apart 3~7mm.
7. raw gas cleaning apparatus according to claim 1, is characterized in that: described dust removing units is 8~16 that by pipeline, are connected in parallel.
CN201320570485.9U 2013-09-13 2013-09-13 Raw coke oven gas dust removal device Expired - Fee Related CN203462016U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103468323A (en) * 2013-09-13 2013-12-25 神木富油能源科技有限公司 Raw coke oven gas dedusting device and raw coke oven gas dedusting method

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103468323A (en) * 2013-09-13 2013-12-25 神木富油能源科技有限公司 Raw coke oven gas dedusting device and raw coke oven gas dedusting method
CN103468323B (en) * 2013-09-13 2015-01-14 神木富油能源科技有限公司 Raw coke oven gas dedusting device and raw coke oven gas dedusting method

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