CN202829975U - Coke oven coal gas refining and purification assembly line with dry and wet combination method - Google Patents
Coke oven coal gas refining and purification assembly line with dry and wet combination method Download PDFInfo
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- CN202829975U CN202829975U CN201220467298.3U CN201220467298U CN202829975U CN 202829975 U CN202829975 U CN 202829975U CN 201220467298 U CN201220467298 U CN 201220467298U CN 202829975 U CN202829975 U CN 202829975U
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Abstract
The utility model relates to a coke oven coal gas refining and purification assembly line with a dry and wet combination method. The dry method segment comprises a naphthalene scrubber (1) and an electrical tar precipitator (3). An oil groove (1b) is arranged in the lower portion of the naphthalene scrubber (1) and a nozzle (1a) is arranged in the upper portion of the naphthalene scrubber (1). An oil pump (7) is arranged between the oil groove (1b) and the nozzle (1a). The electrical tar precipitator (3) is connected with an exit of the naphthalene scrubber (1). The dry method segment comprises an oil and naphthalene removing device and a desulfurizer. The oil and naphthalene removing device is connected with the exit of the electrical tar precipitator (3). A solid absorption agent is filled in the oil and naphthalene removing device. The desulfurizer is connected with an exit of the oil and naphthalene removing device. A solid desulfurizing agent is filled in the desulfurizer. The coke oven coal gas refining and purification assembly line with the dry and wet combination method can ensure purification effect, facilitate implement, reduce burden of the dry method segment, reduce burden in regeneration and replacement of the absorption agent packing and reduce operation expenses and cost without affecting efficiency.
Description
Technical field
The utility model relates to the refining streamline that purifies of a kind of coke-oven gas, relates in particular to a kind of coke-oven gas and does the refining streamline that purifies of wet combined techniques.
Background technology
Coke-oven gas is the manufacture gas that coking by coke oven is produced.Because the not equal factor of the operation of coking coal, process of coking and coal-gas recovering equipment, impurities also is not quite similar in the coke-oven gas.Coke-oven gas is industry, the very important gas raw materials of civil area such as metallurgy, power, chemical industry is synthetic.The purpose of gas purification process is to remove detrimental impurity in the coke-oven gas, mainly contains hydrogen sulfide, prussiate, benzene, naphthalene etc., to satisfy the user demand of different user.
General coke-oven plant all is provided with coal-gas recovering technique, in order to the impurity removal in the coke-oven gas, recycles.Raw gas that coke oven is produced through condensation air blast, tar removing, except naphthalene, desulfurization, wash ammonia, wash benzene after, foreign matter content in the coke-oven gas generally can reach: tar content≤50mg/m3, hydrogen sulfide content≤200mg/m3, naphthalene content≤400mg/m3, benzene content≤4000mg/m3, the coal gas of this kind quality is used for the production of general metallurgical works and uses and can satisfy the demands, but following user's requirement meeting is higher:
1, cold rolling, the vacuum circulation degassing refining furnace of metallurgical works etc. owing to use the difference of technique, can propose requirements at the higher level to gas quality;
2, coke-oven gas requires: tar content≤10mg/m3, hydrogen sulfide content≤20mg/m3, naphthalene content≤50-100mg/m3 as domestic gas;
3, as the synthetic raw material of chemical industry, hydrogen sulfide content≤1～2mg/m3.
The technique of coke-oven coal qi exhaustion naphthalene, desulfurization is divided dry type, wet method.
Dry process is the impurity that adopts in the dry adsorption agent absorption coal gas that main component is comprised of gac, ferric oxide and various catalyzer.
The wet technique of taking off naphthalene is to adopt coal tar wash oil or diesel oil to carry out reverse the contact with coal gas, utilizes naphthalene difference of solubleness in absorption agent to absorb.
The wet process of desulfurization has according to the processing method difference to absorb and two types of oxidation style.All be to adopt the ammoniacal liquor that removes in the coke-oven gas to make alkali source such as First Phase of Baosteel Project jet, the five rich pool coking of Ningbo iron and steel, oxidation absorbs the hydrogen sulfide in the coal gas under catalyst action.Produce sulphur cream behind the desulfurizer regeneration.The monoethanolamine method that adopts such as the Baosteel second phase again, the vacuum potassium carbonate method that plum mountain chemical industry adopts all belongs to absorption process, has absorbed the rich solution of sulphur impurity, and the sour gas that produces after the regeneration is used for sulfuric acid processed, and the absorption liquid after the regeneration recycles.Above method belongs to the wet process of desulfurization.
Two kinds of purification process are compared as follows table:
Coke-oven gas after the rough purification of metallurgical works production is as raw material, often need to make with extra care and purify to satisfy more high-quality customer need, existing refining purification is according to the actual use of coke-oven gas, the wet purification method of passing through that has purifies, the dry purification method of passing through that has purifies, from the purification efficiency aspect, wet processing has limitation.Wet method is taken off naphthalene technique and is subjected to service temperature, takes off naphtalene oil product quality and affect, and best can reach≤50～100mg/m
3Wet desulphurization, best accomplishing≤15mg/m
3And dry process, it is very high that the effect of imurity-removal can reach.But removal effect is higher, and the consumption of sorbent material is larger, and running cost is higher, and especially dry method is taken off naphthalene, and the regeneration power consumption of sorbent material is larger.
For civilian, the coke-oven gas of the purposes such as industrial chemicals, all adopt the dry purification method of good purification to purify, the consumption of sorbent material and decontamination effect improving are closely bound up in the dry process, changing the sorbent material filler is heavy work, Gu treatment of wastes produced also must be by the processed in units with professional qualification, processing costs is very high.Although wet purification method working cost is lower, do not reach the effect of purification.
Summary of the invention
The technical problem that the utility model actual needs solves is: coke-oven gas pure dry type method of purification sorbent material consumption is large, and changing the sorbent material filler is heavy work, Gu treatment of wastes produced also must be by the processed in units with professional qualification, processing costs is very high.Although wet purification method working cost is lower, does not reach and purify the effect that requires.Consider, the burden of taking off the naphthalene sorbent material for reducing dry method is taken off with wet method crude first, wet processing is placed on before the dry process key point: avoid the absorption liquids such as washing oil, diesel oil of wet method section to bring dry type absorption tower into air-flow.
Wet desulphurization efficient is not high, reach same texts, and than dry desulfurization, wet desulphurization is taken up an area greatly, investment is high, subsystem is more, energy consumption is larger, and the especially processing of desulfurization waste liquor is a larger difficult problem to non-coking enterprise.General factory can not process the desulfurization waste liquor device, need set up storage and transportation apparatus and send processing outside.In addition, because system complex, running maintenance is also more numerous.Thus, sulfur removal technology only keeps dry process.Concrete technical scheme is as follows:
The utility model provides a kind of coke-oven gas to do the refining streamline that purifies of wet combined techniques, comprise wet method section and dry method section, described wet method section comprises following equipment: wash naphthalene tower 1, described naphthalene tower 1 bottom of washing is provided with oil groove 1b, top is provided with shower nozzle 1a, is provided with oil pump 7 between described oil groove 1b and the shower nozzle 1a; Also be provided with interchanger 2 between described oil pump 7 and the shower nozzle 1a, described interchanger 2 pipelines are connected with low-pressure steam; Electrical tar precipitator 3, described electrical tar precipitator is connected with the outlet of washing naphthalene tower 1; Described dry method section comprises following equipment: the naphthalene device is taken off in oil removing, and described oil removing is taken off the naphthalene device and is connected with the outlet of electrical tar precipitator 3, and filling solid adsorbent in the naphthalene device is taken off in described oil removing; Desulfurizer, described desulfurizer is connected with the outlet that the naphthalene device is taken off in described oil removing, filling solid desulfurating agent in the described desulfurizer.
Preferably, to take off the naphthalene device be that naphthalene device 5 is taken off in two oil removings that are connected in parallel in described oil removing.
Preferably, described desulfurizer is the thionizer 6 that three parallel/series connect.
The difference of the utility model and prior art mainly is: adopted the streamline of doing wet combination that coke-oven gas is made with extra care purification, replaced original pure dry cleaning, economy improves greatly.
The beneficial effects of the utility model are:
1) adopt the gas purification process of doing wet combination, decontamination effect improving is better than wet type, can reach tar content≤5mg/m3, hydrogen sulfide content≤5mg/m3, naphthalene content≤20mg/m3.
2) adopt the gas purification process of doing wet combination, both guaranteed decontamination effect improving, be beneficial to again enforcement.Take off naphthalene section elder generation wet method, dry method again, given full play to the effect of wet processing, alleviated the burden of dry method section, thereby reduced the burden of the regeneration of sorbent material filler, replacement.
3) reduce working cost, reduce cost.
4) utilize electrical tar precipitator and oil removing to take off the naphthalene device washing oil of washing in the naphthalene tower is carried out filtering, so that do not produce new impurity because of the technique of wet method section self.
5) dried, the wet method of taking off naphthalene and desulfurization is optimized combination, so that whole refining purification process is not loaded down with trivial details, assembly line equipment is simple in structure, reduces cost and has taken into account simultaneously efficient.
Description of drawings
Fig. 1 is that the utility model coke-oven gas is done the refining synoptic diagram that purifies assembly line equipment of wet combined techniques.
Wherein, 1, wash the naphthalene tower, 2, interchanger, 3, electrical tar precipitator, 4, electric heater, 5, oil removing takes off the naphthalene device, 6, thionizer, 7, oil pump.
Embodiment
Below in conjunction with embodiment the utility model is further specified.
For away from the coke-oven plant, need the user of refining coke-oven gas again, in conjunction with the relative merits of dry-wet purification technique use that a kind of technique is simple, reduced investment, occupation of land less, the deep refining gas purification process safeguarded of handled easily.
The utility model coke-oven gas is done the refining streamline that purifies of wet combined techniques and is comprised wet method section and dry method section, described wet method section may further comprise the steps: the coke-oven gas after the rough purification enters oil wash naphthalene tower 1, circulating washing oil flows into the oil groove 1b of oil wash naphthalene tower 1, flow out again oil groove 1b by the top of the described oil wash naphthalene tower 1 of oil pump 7 arrival, spray downwards through shower nozzle 1a again, coal gas in the oil wash naphthalene tower is carried out spray washing, also be provided with interchanger 2 between described oil pump 7 and the shower nozzle 1a, low-pressure steam heats circulating washing oil at described interchanger 2 places, makes the oil temperature of circulating washing oil be higher than 3～5 ℃ of gas temperatures; Coke-oven gas flows out oil wash naphthalene tower 1, enters electrical tar precipitator 3, captures most of remaining washing oil mist, tar fog; Described dry method section may further comprise the steps: coke-oven gas flows out electrical tar precipitator 3, enter oil removing and take off the naphthalene device, filling solid adsorbent in the naphthalene device is taken off in described oil removing, oil removing is taken off the naphthalene device after use for some time, low-pressure steam is formed superheated vapour through behind the electric heater 4, the naphthalene device is taken off in oil removing purges, with oil removing take off in the naphthalene device the impurity desorption out, thereby make the regeneration of described solid adsorbent; Coke-oven gas flows out and flows into desulfurizer after the naphthalene device is taken off in oil removing, and filling solid desulfurating agent in the described desulfurizer, coke-oven gas form the refining coal gas that purifies after flowing out described desulfurizer.Described solid adsorbent comprises gac, alchlor.Described superheated vapour is that temperature is 350 ℃ steam.Described solid desulfurating agent comprises Fe
2O
3.H
2O.It is that naphthalene device 5 is taken off in two oil removings that are connected in parallel that the naphthalene device is taken off in described oil removing.Described desulfurizer is the thionizer 6 that three parallel/series connect.
Below concrete scavenging process is elaborated:
At first, wet method section part, the coke-oven gas through rough purification from the coke-oven plant is introduced into material filling type oil wash naphthalene tower 1, with circulating washing oil spray washing coal gas.In order to keep the turning oil temperature often to be higher than 3～5 ° of C of gas temperature, with 2 pairs of washing oil heating of saturation steam process interchanger of 0.6MPa.The washing naphthalene operation and will contain the naphthalene amount and be reduced to below the 80mg/m3 from 400mg/m3 of washing oil, in order to keep the Absorption Activity of washing oil, need to partly replace washing oil every day, and fresh washing oil fills in the oil groove of material filling type oil wash naphthalene tower 1.
Establish electrical tar precipitator 3 after washing naphthalene tower 1, to capture most of remaining washing oil mist, tar fog.Tar content reaches below the 10mg/m3 substantially behind electrical tar precipitator 3.Tar under electrical tar precipitator 3 captures enters sewage lagoon by pipeline and sneaks into and contain naphthalene sewage and handle together.
Secondly, dry method section part, the coal gas that goes out electrical tar precipitator 3 enters the oil removing that is in adsorbed state and takes off naphthalene device 5, adsorb in the hole that the components such as the tar in the coal gas, naphthalene, part sulphur, benzene are loaded sorbent material, thereby coal gas is purified, be reduced to below the 20mg/m3 from 80mg/m3 containing the naphthalene amount in the coal gas, tar content takes off to 5mg/m3.
Filling solid adsorbent in the naphthalene device is taken off in oil removing, and sorbent material is described below:
A.TZ-D0101 floods macromolecule organic again and forms take coal as raw material behind high temperature cabonization, be exclusively used in and remove that coke-oven gas is coal-tar middle oil, the sorbent material of naphthalene, mist of oil;
B.TZ-B0302 belongs to ature of coal class gac, has added multiple promotor through high temperature cabonization and activation, is mainly used in removing the sorbent material of the impurity such as sulphur in coke oven gas, naphthalene, benzene, tar, mist of oil, and impurity is had the effect that removes preferably.
C.TZ-B0103 belongs to ature of coal class gac, has added multiple promotor through high temperature cabonization and activation, is exclusively used in the sorbent material of impurity such as removing sulphur in coke oven gas, naphthalene, benzene, mist of oil, is used for the deep purifying of coal gas.
The resistant to elevated temperatures magnetic ball that is used for gas distribution that d.TZ-C0102 mainly is comprised of alchlor.
Oil removing is taken off and need be carried out filler regeneration after the naphthalene device uses for some time.Renovation process: heat with 4 pairs of low-pressure steam of electric heater, form 350 ℃ superheated vapour and the naphthalene device is taken off in oil removing directly purge, de-oiling is taken off the impurity desorptions such as tar in the naphthalene device, naphthalene out, thereby make the regeneration of sorbent material filler.
Go out the coke-oven gas that oil removing takes off the naphthalene device and enter thionizer, through the absorption of desulfurization inner-tower filling material, go out H in the coal gas behind the tower
2S content is no more than 5mg/Nm
3This operation is comprised of 3 smart thionizers.Filling solid desulfurating agent in the thionizer, this sweetening agent has the advantages such as capacity is large, resistance is little, activity is high, applicable wide, easy to operate.It is with ferric oxide (a-Fe
2O
3.H
2O and r-Fe
2O
3.H
2O) be main active constituent, added the high-effective gas sweetening agent that multiple promotor and organic carrier oxidation are composited.In order to improve the utilising efficiency of sweetening agent, but 3 thionizers can parallel connection also serial operation.
Coke-oven gas flows out the refining coal gas that purifies of thionizer 6 rear formation.
Claims (3)
1. a coke-oven gas is done the refining streamline that purifies of wet combined techniques, it is characterized in that comprise wet method section and dry method section, described wet method section comprises following equipment:
Wash naphthalene tower (1), described naphthalene tower (1) bottom of washing is provided with oil groove (1b), and top is provided with shower nozzle (1a), is provided with oil pump (7) between described oil groove (1b) and the shower nozzle (1a); Also be provided with interchanger (2) between described oil pump (7) and the shower nozzle (1a), described interchanger (2) pipeline is connected with low-pressure steam;
Electrical tar precipitator (3), described electrical tar precipitator is connected with the outlet of washing naphthalene tower (1);
Described dry method section comprises following equipment:
The naphthalene device is taken off in oil removing, and described oil removing is taken off the naphthalene device and is connected with the outlet of electrical tar precipitator (3), and filling solid adsorbent in the naphthalene device is taken off in described oil removing;
Desulfurizer, described desulfurizer is connected with the outlet that the naphthalene device is taken off in described oil removing, filling solid desulfurating agent in the described desulfurizer.
2. coke-oven gas as claimed in claim 1 is done the refining streamline that purifies of wet combined techniques, and it is characterized in that: it is that naphthalene device (5) is taken off in two oil removings that are connected in parallel that the naphthalene device is taken off in described oil removing.
3. coke-oven gas as claimed in claim 1 is done the refining streamline that purifies of wet combined techniques, and it is characterized in that: described desulfurizer is the thionizer (6) that three parallel/series connect.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220467298.3U CN202829975U (en) | 2012-09-13 | 2012-09-13 | Coke oven coal gas refining and purification assembly line with dry and wet combination method |
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| CN201220467298.3U CN202829975U (en) | 2012-09-13 | 2012-09-13 | Coke oven coal gas refining and purification assembly line with dry and wet combination method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104449877A (en) * | 2014-11-24 | 2015-03-25 | 斯日古郎 | Combustible refuse high-temperature pyrolysis conversion clean gas machine set |
| CN106190191A (en) * | 2016-08-30 | 2016-12-07 | 上海梅山工业民用工程设计研究院有限公司 | A kind of coke oven stove seat clearing apparatus |
-
2012
- 2012-09-13 CN CN201220467298.3U patent/CN202829975U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104449877A (en) * | 2014-11-24 | 2015-03-25 | 斯日古郎 | Combustible refuse high-temperature pyrolysis conversion clean gas machine set |
| CN106190191A (en) * | 2016-08-30 | 2016-12-07 | 上海梅山工业民用工程设计研究院有限公司 | A kind of coke oven stove seat clearing apparatus |
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| GR01 | Patent grant | ||
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Granted publication date: 20130327 |
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