CN105779683B - Converter gas recovery system and recovery method - Google Patents
Converter gas recovery system and recovery method Download PDFInfo
- Publication number
- CN105779683B CN105779683B CN201410810257.3A CN201410810257A CN105779683B CN 105779683 B CN105779683 B CN 105779683B CN 201410810257 A CN201410810257 A CN 201410810257A CN 105779683 B CN105779683 B CN 105779683B
- Authority
- CN
- China
- Prior art keywords
- converter
- valve
- coal gas
- gas
- recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000011084 recovery Methods 0.000 title claims abstract description 109
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000003034 coal gas Substances 0.000 claims abstract description 222
- 238000001816 cooling Methods 0.000 claims abstract description 40
- 230000008016 vaporization Effects 0.000 claims abstract description 27
- 229910000831 Steel Inorganic materials 0.000 claims abstract description 25
- 239000010959 steel Substances 0.000 claims abstract description 25
- 238000003860 storage Methods 0.000 claims abstract description 23
- 238000009792 diffusion process Methods 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 238000002309 gasification Methods 0.000 claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 8
- 230000000087 stabilizing effect Effects 0.000 claims abstract description 6
- 239000000843 powder Substances 0.000 claims description 29
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 238000009413 insulation Methods 0.000 claims description 5
- 238000004458 analytical method Methods 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 238000013461 design Methods 0.000 claims description 2
- 241000196324 Embryophyta Species 0.000 claims 1
- 235000003140 Panax quinquefolius Nutrition 0.000 claims 1
- 240000005373 Panax quinquefolius Species 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 6
- 238000009628 steelmaking Methods 0.000 abstract description 5
- 239000002893 slag Substances 0.000 abstract description 3
- 230000003139 buffering effect Effects 0.000 abstract description 2
- 238000009834 vaporization Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 238000012432 intermediate storage Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 67
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 8
- 229910052742 iron Inorganic materials 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 238000007664 blowing Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 230000001535 kindling effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 206010022000 influenza Diseases 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
Landscapes
- Carbon Steel Or Casting Steel Manufacturing (AREA)
Abstract
The invention discloses a converter gas recovery system and a recovery method, which comprises a gasification cooling section flue, a dust remover, a gas enricher, a converter gas middle storage tank, N2The converter gas recovery system is arranged at the outlet end of a flue of a vaporization cooling section of an original converter gas recovery system. The technological process includes the steps of feeding the high temperature converter gas from the gasifying and cooling section flue into a dust collector, feeding the converter gas into a gas enriching device for gasifying reaction, and introducing over 80% of CO in the converter gas2And converting the enriched converter gas into CO, buffering and stabilizing the enriched converter gas by a converter gas intermediate storage tank, and then sequentially entering a switching station and a converter gas recovery cabinet under the suction of an induced draft fan to finish the recovery of the converter gas. The invention has the following effects: can realize the improvement of the heat value of the coal gas recovered per ton of steel and increase the recovery of the coal gas per ton of steel of the converterThe amount of the slag is reduced, the waste of diffusion and the pollution to the atmosphere are avoided, and the steel-making cost is reduced.
Description
Technical field
It is more particularly to a kind of to expand coal gas of converter by way of enrichment the invention belongs to energy-conserving and emission-cutting technology field
Ton steel yield, and the converter gas recovery system and recovery method for greatly improving gas recovery calorific value can be realized.
Background technology
Coal gas of converter is the important secondary energy sources of iron and steel enterprise, and RECOVERY OF CONVERTER GAS accounts for whole converter procedure energy recovery
80%-90%.RECOVERY OF CONVERTER GAS and the level utilized are improved, is to realize the negative important means that can be made steel.Iron and steel enterprise at present
RECOVERY OF CONVERTER GAS is differed greatly using level, and the average yield of many iron and steel enterprise's coal gas of converter is few, and calorific value is low, and user is few,
Coal gas of converter, which exists, diffuses situation.Calculating shows that the ton steel converter coal-gas recovering maximum desired value under preferable operating mode is
128.8m3/ t, average heat production is up to 8.8MJ/m3More than.General iron and steel enterprise RECOVERY OF CONVERTER GAS amount is in 60~80m at present3/
T, calorific value are commonly 6.7~7.1MJ/m3, and advanced enterprises RECOVERY OF CONVERTER GAS amount is more than 110m3/ t, Rate of Converter Gas Recovery
88% is reached as high as, close to 90%.If by annual pneumatic steelmaking yield in terms of 100,000,000 tons, RECOVERY OF CONVERTER GAS level often improves
10m3/ t steel, whole year will just reclaim the m of coal gas of converter 1,000,000,000 more3, equivalent to saving 280,000 tons of (coal gas of converter mean calories of standard coal
By 8.37MJ/m3Note).Come with it, the further reduction of STEELMAKING PRODUCTION environmental pollution, its environmental benefit is even more can not
Estimate.Therefore see, the work of converter current coal-gas recovering also needs further to strengthen, and there are larger potentiality.
Recovery operation problem for strengthening coal gas of converter, present steel-making worker have realized that raising coal gas of converter
Recovery be a system engineering, the coordinating and unifying need to be used from being supplied to, and in order to obtain the coal gas of converter of high quality, Ying Congzhuan more
Stove blowing operation, gas recovery system controls and each side cooperative developments such as coal gas utilizes.
Current converter gas recovery system, typically use OG methods or LT methods.Either OG methods or LT methods, former coal gas of converter
Recovery system is substantially to be made up of three parts：Vaporizing cooling section, dedusting temperature descending section, coal-gas recovering tower, as shown in Figure 2.
In the concrete operations control of converter current gas recovery system, have been carried out converter and drop cover operation automatically, automatically control
Fire door pressure-fired, control oxygen supply intensity, outfit simultaneously improve dynamic control blowing end point technology；
At present in coal gas of converter using upper, and by rational allocation Gas Resource, to utilize coal gas of converter more than needed to develop high
Added value chemical products, make Gas Resource benefit.
Most scientific evaluation is operated to RECOVERY OF CONVERTER GAS, it may be that from coal gas of converter ton steel yield (m3/ t) or converter
Coal-gas recovering total amount (m3/ stove), 3 metrics evaluations such as coal gas of converter calorific value and dust content of gas.But in actual production individually
Compare " coal gas of converter ton steel yield (m3/ t) " this index do not have direct comparativity, it is necessary to reference to the coal gas reclaimed
Calorific value jointly consider.Therefore, gross calorific value (GJ/ stoves steel) (the i.e. converter of converter per heat gas recovery should be used in practice
Coal gas mean calorie × coal gas of converter ton steel yield), additional reference dust content of gas come weigh and evaluate coal gas of converter return
Bring drill to an end work.
Coal gas of converter calorific value covers two aspects：1. chemical heat --- CO% of coal gas of converter and 2. physical thermal --- is final
The physical temperature of obtained purified gas.The chemical heat being embodied in its contained CO mass percent, its weight account for more than 80%, remaining
Under be coal gas of converter physical thermal.So really to do RECOVERY OF CONVERTER GAS operation well, in actual production, find a kind of
Suitable for the system and recovery method of RECOVERY OF CONVERTER GAS, make its can online enrichment coal gas of converter to improve receipts coal gas of converter
Chemical heat simultaneously can expand coal gas of converter ton steel yield as far as possible, moreover it is possible to ensure that the cleanliness factor for receiving coal gas of converter is (i.e. low
Dustiness:5~10mg/m3) while retain the higher physical temperature of coal gas of converter, to realize per heat gas recovery calorific value
Maximize.A kind of invention of such RECOVERY OF CONVERTER GAS operation is only science.Thus it is energy-saving to iron and steel enterprise,
It is significant that production cost is greatly reduced.
The content of the invention
It is an object of the invention to provide a kind of converter gas recovery system and recovery method, the system is arranged on former converter
The Vaporizing cooling section flue outlet end of gas recovery system, can be to go out the high temperature of Vaporizing cooling section flue by the system
Coal gas of converter is raw material, and using CDQ powder as reducing catalyst, enrichment is carried out to coal gas of converter；And a system is taken by coal gas enriching apparatus
Row method is to RECOVERY OF CONVERTER GAS, the final mesh for realizing " improving coal gas of converter ton steel yield and ton steel gas recovery calorific value "
's.The gas recovery " calorific value " of " raising " described here includes chemical heat (CO% for improving coal gas of converter) and physical thermal is (most
The physical temperature of the purified gas obtained eventually substantially can be more than 700 DEG C).
A kind of recovery system of coal gas of converter of the present invention, it is by gasification cooling section flue, deduster, coal gas enriching apparatus, turns
Storage tank, N in producer gas2Pipeline and valve A~valve F, air-introduced machine, diffusing tower, switching station, RECOVERY OF CONVERTER GAS cabinet composition, this
Converter gas recovery system is arranged on former producer gas recovery system Vaporizing cooling section flue outlet end.
Before Vaporizing cooling section flue outlet end, dedusting temperature descending section arrival end, set up one section and carry inlet non return check valve valve A
Coal gas escape pipe, in the pipe and deduster, coal gas enriching apparatus, coal gas of converter in storage tank, coal gas of converter storage tank outlet conduit
Air-introduced machine, diffusing tower, switching station, coal gas of converter are connected to behind upper setting inlet non return check valve valve E, non-return valve valve E successively to return
Receive cabinet, in coal gas of converter storage tank simultaneously with the N with flow control valve valve F2Pipeline connect, deduster, coal gas enriching apparatus it
Between diffusion valve valve C is set, storage tank carries diffusion valve valve D in coal gas of converter, and vaporization is arranged in converter gas recovery system
Between cooling section flue outlet end and dedusting temperature descending section arrival end, and after the coal gas escape pipe with inlet non return check valve valve A
Inlet non return check valve valve B is set up on the pipeline in face.
Concrete structure of the present invention has, and coal gas enriching apparatus outer side band thermal insulating warm-keeping layer, coal gas enriching apparatus sets automatic temperature control system,
Installation temperature detection signal device in coal gas of converter of the present invention between storage tank and valve E；
Valve A, valve B, valve E are inlet non return check valve in the present invention；Valve C, valve D are diffusion valve；Installed in N2Pipe
Valve F on road is flow control valve.
The present invention is a kind of RECOVERY OF CONVERTER GAS method, and converter gas recovery system is arranged on Vaporizing cooling section flue outlet
End, its technical process are, when starting to reclaim coal gas of converter, open inlet non return check valve valve A, simultaneously close off inlet non return check valve valve
Door B, deduster will be entered from the high temperature coal gas of converter that converter comes out through Vaporizing cooling section flue, removing dust device removes quality percentage
Stove dirt than 80%~95%, and after eliminating red-hot slag iron grain kindling material, the high temperature coal gas of converter of removing dust is passed through and filled
Gasification reaction is carried out in the coal gas enriching apparatus of excessive coke-oven plant's dry cooled coke powder (CDQ powder) with high response, by converter coal
The CO of percent by volume more than 80% in gas2CO is converted into, the coal gas of converter of enrichment is completed in coal gas enriching apparatus through converter coal
In gas storage tank buffering voltage stabilizing after, via inlet non return check valve valve E, air-introduced machine attraction under, sequentially enter switching station, coal gas of converter
Cabinet is reclaimed, completes the recovery of coal gas of converter.If off analysis, switching station is closed, coal gas of converter is lighted by diffusing tower and diffused.
Concrete technology is：
1. by slightly adjusting the intensity of cooling of gasification cooling flue, to realize out gasification cooling flue, turn into deduster
Producer gas temperature will be maintained at 1100~1200 DEG C, and temperature meets following two requirements during ensureing that coal gas of converter goes out deduster：
First, the gasification reaction CO that coal gas of converter is carried out in coal gas enriching apparatus2+ C (surplus)=2CO (705 DEG C) (⊿ H0>0) requirement；
Two are to ensure that the CO of percent by volume more than 80%2CO is changed into, corresponding reaction temperature should be more than 1000 DEG C, and gasify
The maximum reaction rate of reaction should appear in 1100 ± 50 DEG C, now normal CO in coal gas of converter2Percent by volume 15~
25%.
2. coal gas enriching apparatus uses fixed bed form, CDQ powder makees catalyst.Coal gas enriching apparatus sets attemperator and temperature automatically controlled
System, it is ensured that make coal gas enriching apparatus internal temperature be maintained at 900 DEG C~1250 DEG C, to realize the converter coal into coal gas enriching apparatus
Temperature degree is more than 610 DEG C, the final low temperature blast for eliminating coal gas of converter.
3. preliminary examination meets after requiring, CDQ powder is added into coal gas enriching apparatus with the excess quantity of mass percent 10%~15%
(can be previously added), with the total chemically active stabilization of CDQ powder in coal gas enriching apparatus is macroscopically ensured.Often complete a stove converter
The recovery of coal gas, all change the CDQ powder in a coal gas enriching apparatus.The utilization rate of CDQ powder presses 50% (matter in coal gas enriching apparatus
Amount) meter, consider CDQ powder excess rate 10%~15%, then CDQ powder is initially added in coal gas enriching apparatus corresponding to converter steel per ton
Measure as 20~25kg.
4. the coal gas of converter after dedusting is entered by coal gas enriching apparatus bottom, discharged by coal gas enriching apparatus top.
5. under converter normal operating conditions, the recovery condition of coal gas of converter is generally CO >=35%, O2<2%, utilize this hair
Bright technology, the O for only considering safety factor can be relaxed to2<2%, without considering CO mass percents (converter normal operating conditions
Under, O2CO mass percents when=2% are generally higher than 15%, more than a minimum oxygen for the maximum return value of recovery coal gas of converter
Change carbon recovery concentration 10%), as long as the O that is, in coal gas of converter2<2%, you can recovery, such RECOVERY OF CONVERTER GAS time situation
In former recovery time section, " front and rear substantially all to prolong 1min, removal combined influence factor, as a result more recovery 2min, about increase converter
Coal-gas recovering amount percent by volume 10%.With theoretical maximum yield 128.8m3/ t is counted, and can reclaim 12m more3/t±2m3。
6. valve A, valve B, valve E are inlet non return check valve, effect is the valve A under the normal condition of present invention process
Open while valve B be closed, now inlet non return check valve valve E open and meanwhile diffusion valve valve C, diffusion valve valve D and
N2Flow control valve valve F on pipeline is closed, and newly-increased coal gas of converter enrichment technique of the invention is normally carried out.
7. the coal gas of converter enrichment system of the present invention disables, inlet non return check valve valve A is closed while valve B is in and opened
State, now inlet non return check valve valve E closings while diffusion valve valve C, diffusion valve valve D and N2Flow-rate adjustment on pipeline
Valve valve F close, former converter gas recovery system normal operation, i.e., from converter come out high temperature coal gas of converter through Vaporizing cooling section
Flue enters dedusting temperature descending section etc., finally enters coal-gas recovering tower.
8. the air-introduced machine in road, diffusing tower, switching station are considered as resistance to 1000 DEG C of high temperature problems, converter after system in this programme
Coal-gas recovering cabinet is considered as insulation problem.
9. coal gas of converter state detector is set between diffusing tower, switching station, when the CO% in the coal gas of converter reclaimed,
O2When % etc. meets safe retrieving standard, switching station is opened, and carries out normal coal-gas recovering；Otherwise, switching station is closed, and receives coal gas
Light and diffuse through diffusing tower.
10. the high temperature coal gas of converter reclaimed, it is desirable to there is stable user, and nearby.
The effect of the RECOVERY OF CONVERTER GAS cabinet of the system, in addition to coal gas of converter is stored, also voltage stabilizing, mixing, stably into
The effect of grading.
Following positive effect can be realized using the present invention：
1st, the implementation of the technology of the present invention, the raising of ton steel gas recovery calorific value can be achieved.Result of calculation, coal gas of converter enrichment
Afterwards, CO mass percents, which can averagely improve more than 20%, coal gas of converter calorific value, can averagely improve more than 35%.
2nd, the realization of coal gas of converter enrichment, the drop of CO mass percent standards in RECOVERY OF CONVERTER GAS precondition can be achieved
It is low, so as to extend the recovery time of coal gas of converter, coal gas of converter ton steel yield is increased, result of calculation shows, can increase
RECOVERY OF CONVERTER GAS amount 10% or so.
3rd, by the method, the coal gas of converter for not meeting existing recovery standard largely is not only caused to be able to recovery, so as to keeping away
The waste diffused and the pollution to air are exempted from, and have improved the calorific value of coal gas of converter, enable its more scientific utilization, dropped
Low steel-making cost.
4th, CDQ powder is more scientific, more reasonably utilizes in the present invention, and one is have found preferably for the renewable resources of CDQ powder
Approach.
5th, the technology of the present invention is particularly useful for the factory that the coal gas of converter calorific value that is reclaimed is low, yield is few.
Brief description of the drawings
Fig. 1 is the schematic diagram of present system.
Fig. 2 is the process flow diagram of former converter gas recovery system.
In figure：Storage tank, 6 dedustings in 1 converter, 2 Vaporizing cooling section flues, 3 dedusters, 4 coal gas enriching apparatus, 5 coal gas of converter
Temperature descending section, 7 air-introduced machines, 8 diffusing towers, 9 switching stations, 10 RECOVERY OF CONVERTER GAS cabinets, 11 coal-gas recovering towers, 21 valve A, 22 valve B,
25 valve E, 23 valve C, 24 valve D, 26 valve F.
Embodiment
The present invention is elaborated below in conjunction with the accompanying drawings：
As shown in figure 1, present system is directly installed on the port of export of Vaporizing cooling section flue 2, its system is by dedusting
Storage tank 5, N in device 3, coal gas enriching apparatus 4, coal gas of converter2Pipeline and valve A21~valve F26 compositions, air-introduced machine 7, diffusing tower 8,
Switching station 9, RECOVERY OF CONVERTER GAS cabinet 10 form, and are set up before the outlet side of Vaporizing cooling section flue 2, the entrance of dedusting temperature descending section 6
One section of coal gas escape pipe for carrying inlet non return check valve valve A21, the pipe in deduster 3, coal gas enriching apparatus 4, coal gas of converter with storing up
Inlet non return check valve valve E25 is set in tank 5, coal gas of converter on the outlet conduit of storage tank 5, connect successively behind non-return valve valve E25
Have air-introduced machine 7, diffusing tower 8, switching station 9, a RECOVERY OF CONVERTER GAS cabinet 10, in coal gas of converter storage tank 5 simultaneously with Flow-rate adjustment
Valve valve F26 N2Pipeline connects, setting diffusion valve valve C23 between deduster 3, coal gas enriching apparatus 4, storage tank in coal gas of converter
5 carry diffusion valve valve D24, between gasification cooling flue 2 and dedusting temperature descending section 6, and with inlet non return check valve valve A21
Coal gas escape pipe behind pipeline on set up inlet non return check valve valve B22.
The outer side band thermal insulating warm-keeping layer of coal gas enriching apparatus 4 of the present invention, coal gas enriching apparatus 4 set automatic temperature control system.
As shown in figure 1, the installation temperature detection signal device between storage tank 5 of the present invention and valve E25；Valve in the present invention
A21, valve B22, valve E25 are inlet non return check valve；Valve C23, valve D24 are diffusion valve；Installed in N2Valve on pipeline
F26 is flow control valve.
The present invention recovery coal gas of converter specific recovery process be：Converter gas recovery system is arranged on Vaporizing cooling section cigarette
The port of export of road 2, its technical process are, when starting to reclaim coal gas of converter, open inlet non return check valve valve A21, simultaneously close off list
To non-return valve valve B22, enter deduster 3, removing dust from the high temperature coal gas of converter that converter 1 comes out through Vaporizing cooling section flue 2
Device 3 removes the stove dirt of mass percent 80%~95%, and after eliminating red-hot slag iron grain kindling material, the high temperature of removing dust is turned
Producer gas, which is passed through in the coal gas enriching apparatus 4 for filling excessive coke-oven plant's dry cooled coke powder (CDQ powder) with high response, enters promoting the circulation of qi
Change reaction, by the CO of percent by volume in coal gas of converter more than 80%2CO is converted into, enrichment is completed in coal gas enriching apparatus 4
Coal gas of converter through storage tank in coal gas of converter 5 buffer voltage stabilizing after, via inlet non return check valve valve E25, air-introduced machine 7 attraction under, according to
It is secondary to enter switching station 9, RECOVERY OF CONVERTER GAS cabinet 10, complete the recovery of coal gas of converter.If off analysis, switching station is closed, is turned
Producer gas is lighted by diffusing tower 8 and diffused.Design parameter is as follows：
1. by slightly adjusting the intensity of cooling of Vaporizing cooling section flue 2, to realize out that gasification cooling flue 2 enters deduster 3
Coal gas of converter temperature to be maintained at 1100~1200 DEG C, during ensureing that coal gas of converter goes out deduster temperature meet it is following two will
Ask：First, the gasification reaction CO that coal gas of converter is carried out in coal gas enriching apparatus 42+ C (surplus)=2CO (705 DEG C) (⊿ H0>0)
It is required that；Two are to ensure that the CO of percent by volume more than 80%2Change into CO, corresponding reaction temperature should more than 1000 DEG C,
And the maximum reaction rate of gasification reaction should appear in 1100 ± 50 DEG C, now normal CO in coal gas of converter2Content 15~
25%.
2. coal gas enriching apparatus 4 uses fixed bed form, CDQ powder makees catalyst.Coal gas enriching apparatus 4 sets insulation and temperature automatically controlled system
System, it is ensured that make the internal temperature of coal gas enriching apparatus 4 be maintained at 900~1250 DEG C, to realize the coal gas of converter into coal gas enriching apparatus 4
Temperature is more than 610 DEG C, the final low temperature blast for eliminating coal gas of converter.
3. preliminary examination meets after requiring, CDQ powder is added into coal gas enriching apparatus with the excess quantity of mass percent 10%~15%
(can be previously added), with the total chemically active stabilization of CDQ powder in coal gas enriching apparatus 4 is macroscopically ensured.A stove is often completed to turn
The recovery of producer gas, all change the CDQ powder in a coal gas enriching apparatus 4.The utilization rate of CDQ powder is pressed in coal gas enriching apparatus 4
50% (quality) is counted, and considers CDQ powder excess rate 10%~15%, then CDQ powder in coal gas enriching apparatus 4 corresponding to converter steel per ton
Initial incremental amount is 20~25kg.
4. the coal gas of converter after dedusting is entered by the bottom of coal gas enriching apparatus 4, discharged by the top of coal gas enriching apparatus 4.
5. utilizing the technology of the present invention, under converter normal operating conditions, the recovery condition of coal gas of converter, which can be relaxed to, only to be considered
The O of safety factor2<2%, without consider CO mass percents (under converter normal operating conditions, O2CO mass percentages when=2%
Than more than 15%, the minimum carbon monoxide more than the maximum return value of recovery coal gas of converter reclaims concentration 10%), as long as i.e. converter
O in coal gas2<2%, you can recovery, such RECOVERY OF CONVERTER GAS time situation are " front and rear substantially all to prolong in former recovery time section
1min, combined influence factor is removed, as a result more recovery 2min, about increase RECOVERY OF CONVERTER GAS amount 10%.Reclaimed with theoretical maximum
Measure 128.8m3/ t is counted, and can reclaim 12m more3/t±2m3。
6. valve A21, valve B22, valve E25 are inlet non return check valve, effect be under the normal condition of present invention process,
Valve A21 is opened while valve B22 is closed, now inlet non return check valve valve E25 open and meanwhile diffusion valve valve C23,
Diffusion valve valve D24 and N2Flow control valve valve F26 on pipeline is closed, and enables the coal gas of converter enrichment technique of the present invention
It is normally carried out.
7. the coal gas of converter enrichment system of the present invention disables, inlet non return check valve valve A21 is closed while valve B22 is in
Opening, now inlet non return check valve valve E25 closings while diffusion valve valve C23, diffusion valve valve D24 and N2On pipeline
Flow control valve valve F26 close, former converter gas recovery system normal operation, i.e., from converter 1 come out high temperature converter coal
Gas enters dedusting temperature descending section etc. through Vaporizing cooling section flue 2, finally enters coal-gas recovering tower 11, technological process is as shown in Figure 2.
8. the air-introduced machine 7 in the rear road of system, diffusing tower 8, switching station 9 are considered as resistance to 1000 DEG C of high temperature and asked in this programme
Topic, RECOVERY OF CONVERTER GAS cabinet 10 are considered as insulation problem.
9. coal gas of converter state detector is set between diffusing tower 8, switching station 9, when in the coal gas of converter reclaimed
CO%, O2When % etc. meets safe retrieving standard, switching station 9 is opened, and carries out normal coal-gas recovering；Otherwise, switching station 9 is closed,
Received coal gas is lighted through diffusing tower 8 and diffused.
10. the high temperature coal gas of converter reclaimed, it is desirable to there is stable user, and nearby.
The effect of the RECOVERY OF CONVERTER GAS cabinet 10 of the system, in addition to coal gas of converter is stored, also voltage stabilizing, mixing, stably
Composition etc. acts on.
Embodiment
Certain factory 158t converter, molten iron maximum charge weight are 155 tons/stove, and flue gas is into and out of temperature before and after gasification cooling flue 2
Degree is at 1550 DEG C, 750 DEG C or so, the average yield 59~86kg/t, dust content 67mg/m of steam3Left and right, coal gas of converter
Yield maintains 83m3/t±3m3, coal gas of converter calorific value is in 6.7MJ/m3Left and right, coal gas of converter CO, CO2Content is respectively
45%~65%, 20%~25% or so, RECOVERY OF CONVERTER GAS restrictive condition is CO >=35%, O2<2%, recovery time is big
Cause as the starting for the 4th minute of blowing, terminate within the 15.5th minute, totally 11.5 minutes, dust pelletizing system uses OG methods.CDQ powder utilization rates
Based on 50%.
As shown in figure 1, the technique of the port of export of Vaporizing cooling section flue 2 is directly installed on using converter gas recovery system
Method.
Prepare：After the recovery for completing last time converter coal, by the CDQ powder in the coal gas enriching apparatus 4 for using fixed bed with 15%
Excess quantity all change, the CDQ powder amount being fitted into coal gas enriching apparatus 4 be 3.8 tons.
RECOVERY OF CONVERTER GAS restrictive condition is by original CO >=35%, O2<2%, it is changed to O2<2% is (normal in converter
Under working condition, now 15%>CO>35%, the minimum carbon monoxide more than recovery coal gas of converter maximum return value reclaims concentration
10%), recovery time is changed to reclaim in original by " the 4th minute of blowing originally, terminating within the 15.5th minute, totally 11.5 points "
Time section " front and rear substantially all to prolong 1min, for the starting for the 3rd minute of blowing, to terminate for the 16.5th minute ", totally 13.5 minutes, recovery
Time lengthening 17.4%, combined influence factor is removed, as a result coal gas of converter amount reclaims 12.5m more3/ t, it is ton steel under preferable operating mode
RECOVERY OF CONVERTER GAS maximum desired value (128.8m3/ t) 9.7%, be the normal yield (83m of coal gas of converter3/ t) 15.1%.
Secondly, the intensity of cooling of Vaporizing cooling section flue 2 is limited slightly, make steam be averaged yield maintain it is relatively low
60~70kg/t or so, ensure flue gas go out Vaporizing cooling section flue after temperature at 1200 DEG C ± 50 DEG C or so, finally ensure coal gas
The internal temperature of enriching apparatus 4 is at 1150 DEG C ± 50 DEG C.
Go out Vaporizing cooling section flue 2 flue gas enter the dedusting of deduster 3 after, dust content is by initial 65mg/m3Drop
To 7mg/m3, dust removal efficiency is up to 89.2%.
After coal gas of converter sufficiently gasify enrichment into coal gas enriching apparatus 4, buffered surely through storage tank in coal gas of converter 5
Pressure, by by inlet non return check valve valve E25, in the case where air-introduced machine 7 attracts, sequentially enter switching station 9, RECOVERY OF CONVERTER GAS cabinet 10,
Complete the recovery of coal gas of converter.If off analysis, switching station 9 is closed, coal gas of converter is lighted by diffusing tower 8 and diffused.
CDQ powder catalyst bed is because of CO in coal gas enriching apparatus 42Conversion ratio is 91% ± 2%, and more than 80%, satisfaction requires technique
It is required that therefore the parameters of CDQ powder catalyst beds do not add adjustment in the coal gas enriching apparatus 4 to being determined after preliminary examination.
Final coal gas of converter composition CO, CO2Content is respectively by original 55%CO, 20%CO2Left and right is converted into 77.3%
CO, 1.54%CO2Left and right, CO2The conversion ratio for changing into combustible basis CO is 90.9%.So, the CO mass percents of coal gas of converter
Improve 22.3%；Temperature, to 925 DEG C, raises 860 DEG C by 65 DEG C of original liftings.Consider the composition of coal gas of converter calorific value：Chemistry
Heat and physical thermal, receive the calorific value of coal gas of converter by original average 6.9MJ/m3Bring up to 10.20MJ/m3, calorific value raising
47.8%, CO concentration increase by 22.3%, ton steel recovery coal gas of converter amount increase (12.5+20.45) is equal to 32.95m3, i.e., it is final
Gas volume into converter gas cabinet 10 adds 32.95m3/ t, becomes 83+32.95=115.95m3/ t, improve 39%；Calorific value
For 10.20MJ/m3, improve 47.8%.
Claims (4)
- A kind of 1. RECOVERY OF CONVERTER GAS method, it is characterised in that realize the system of this method by gasification cooling section flue (2), remove Storage tank (5), N in dirt device (3), coal gas enriching apparatus (4), coal gas of converter2Pipeline and valve A (21)~valve F (26), air-introduced machine (7), diffusing tower (8), switching station (9), RECOVERY OF CONVERTER GAS cabinet (10) composition, converter gas recovery system are arranged on Vaporizing cooling Section flue (2) port of export；One section, which is set up, between the port of export and dedusting temperature descending section (6) arrival end of Vaporizing cooling section flue (2) carries one-way check Valve valve A (21) coal gas escape pipe, storage tank (5) in escape pipe and deduster (3), coal gas enriching apparatus (4), coal gas of converter, turn Inlet non return check valve valve E (25), non-return valve valve E (25) is set to connect successively below in producer gas on the outlet conduit of storage tank (5) Have air-introduced machine (7), diffusing tower (8), switching station (9), a RECOVERY OF CONVERTER GAS cabinet (10), in coal gas of converter storage tank (5) and meanwhile with band There is flow control valve valve F (26) N2Pipeline is connected, and diffusion valve valve C is set between deduster (3), coal gas enriching apparatus (4) (23), storage tank (5) carries diffusion valve valve D (24) in coal gas of converter, in Vaporizing cooling section flue (2) and dedusting temperature descending section (6) Between, and set up inlet non return check valve valve B on the pipeline behind the coal gas escape pipe with inlet non return check valve valve A (21) (22)；Its technical process is, when starting to reclaim coal gas of converter, open inlet non return check valve valve A (21), simultaneously close off it is unidirectional inverse Only valve valve B (22), the high temperature coal gas of converter that will be come out from converter (1) enter deduster (3) through Vaporizing cooling section flue (2), Removing dust device (3) removes the stove dirt of mass percent 80%~95%, afterwards, the high temperature coal gas of converter of removing dust is passed through into Sheng Have and gasification reaction is carried out in the coal gas enriching apparatus (4) of excessive coke-oven plant's dry cooled coke powder with high response, dry cooled coke powder is For CDQ powder, by the CO of percent by volume in coal gas of converter more than 80%2CO is converted into, enrichment is completed in coal gas enriching apparatus (4) Coal gas of converter through storage tank in coal gas of converter (5) buffer voltage stabilizing after, via inlet non return check valve valve E (25), air-introduced machine (7) inhale Under drawing, switching station (9), RECOVERY OF CONVERTER GAS cabinet (10) are sequentially entered, completes the recovery of coal gas of converter, if off analysis, closed Switching station (9) is closed, coal gas of converter is lighted by diffusing tower (8) and diffused, and design parameter is：1. by adjusting the intensity of cooling of Vaporizing cooling section flue (2), to realize out that Vaporizing cooling section flue (2) enters deduster (3) coal gas of converter temperature is maintained at 1100~1200 DEG C, and meets following two conditions：First, coal gas of converter is in coal gas enrichment The gasification reaction carried out in device (4)：At 705 DEG C, under conditions of C surpluses, CO2+ C=2CO reaction ⊿ H0>0；Second, protect Demonstrate,prove the CO of percent by volume more than 80%2CO is changed into, corresponding reaction temperature is more than 1000 DEG C, and the maximum of gasification reaction Reaction rate is at 1100 ± 50 DEG C, now normal CO in coal gas of converter2Content is in percent by volume 15%~25%；2. coal gas enriching apparatus (4) uses fixed bed form, CDQ powder makees catalyst, and coal gas enriching apparatus (4) sets insulation and temperature automatically controlled system System, it is ensured that make coal gas enriching apparatus (4) internal temperature be maintained at 900~1250 DEG C, it is ensured that into the converter coal of coal gas enriching apparatus (4) Temperature degree is more than 610 DEG C；3. preliminary examination meets after requiring, it is subject to the excess quantity of CDQ powder mass percent 10%~15%, often completes a stove coal gas of converter Recovery, all change the CDQ powder in a coal gas enriching apparatus (4), CDQ in coal gas enriching apparatus (4) corresponding to converter steel per ton The initial incremental amount of powder is 20~25kg；4. the coal gas of converter after dedusting is entered by coal gas enriching apparatus (4) bottom, discharged by coal gas enriching apparatus (4) top；5. at nominal conditions, valve A (21) is opened while valve B (22) is closed, now inlet non return check valve valve E (25) open while diffusion valve valve C (23), diffusion valve valve D (24) and N2Flow control valve valve F (26) on pipeline is closed Close, coal gas of converter enrichment technique is normally carried out；6. when coal gas of converter enrichment system disables, inlet non return check valve valve A (21) is closed while valve B (22) is in opening state State, now inlet non return check valve valve E (25) closings while diffusion valve valve C (23), diffusion valve valve D (24) and N2On pipeline Flow control valve valve F (26) close, former converter gas recovery system normal operation；7. the resistance to 1000 DEG C of high temperature of air-introduced machine (7), diffusing tower (8), switching station (9), RECOVERY OF CONVERTER GAS cabinet (10) plus insulation；8. coal gas of converter state detector is set between (9) in diffusing tower (8), switching station, as CO, O of the coal gas of converter reclaimed2 When meeting safe retrieving standard, switching station (9) is opened, and carries out normal coal-gas recovering；Otherwise, switching station (9) is closed, and receives coal gas Light and diffuse through diffusing tower (8)；9. the high temperature coal gas of converter reclaimed is connected to user.
- 2. a kind of RECOVERY OF CONVERTER GAS method according to claim 1, it is characterised in that the coal gas enriching apparatus (4) is outside Side band thermal insulating warm-keeping layer, coal gas enriching apparatus (4) set automatic temperature control system.
- 3. a kind of RECOVERY OF CONVERTER GAS method according to claim 1, it is characterised in that the storage tank (5) and valve E (25) the installation temperature detection signal device between.
- 4. a kind of RECOVERY OF CONVERTER GAS method according to claim 1, it is characterised in that described valve A (21), valve B (22), valve E (25) are inlet non return check valve；Valve C (23), valve D (24) are diffusion valve；Valve F (26) is Flow-rate adjustment Valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410810257.3A CN105779683B (en) | 2014-12-23 | 2014-12-23 | Converter gas recovery system and recovery method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410810257.3A CN105779683B (en) | 2014-12-23 | 2014-12-23 | Converter gas recovery system and recovery method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105779683A CN105779683A (en) | 2016-07-20 |
| CN105779683B true CN105779683B (en) | 2018-01-05 |
Family
ID=56377821
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410810257.3A Active CN105779683B (en) | 2014-12-23 | 2014-12-23 | Converter gas recovery system and recovery method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105779683B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107557524A (en) * | 2017-09-29 | 2018-01-09 | 四川德胜集团钒钛有限公司 | A kind of converter gas recovery system |
| CN109054874B (en) * | 2018-05-24 | 2021-03-02 | 武汉科技大学 | Medical waste treatment method based on converter smoke waste heat utilization |
| CN108707718A (en) * | 2018-06-14 | 2018-10-26 | 鞍钢股份有限公司 | Device for utilizing high-temperature converter gas and improving heat value and using method thereof |
| CN109852763A (en) * | 2019-01-09 | 2019-06-07 | 无锡明天环保设备有限公司 | A kind of converter gas purification and exhaust heat recovering method |
| CN111020101A (en) * | 2019-11-29 | 2020-04-17 | 山东莱钢永锋钢铁有限公司 | Method for controlling recovery termination of converter gas |
| CN111042773B (en) * | 2019-12-21 | 2021-11-12 | 山西晋城无烟煤矿业集团有限责任公司 | Low-pressure coal bed gas well emptying and recycling linkage device |
| CN118207381B (en) * | 2024-03-20 | 2024-09-06 | 江苏恒丰能环科技股份有限公司 | Safety synergistic recovery device and recovery method for converter gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671757A (en) * | 2009-10-14 | 2010-03-17 | 中冶赛迪工程技术股份有限公司 | Converter coal gas dry-method bag-type dust collecting and waste heat recovery method |
| CN101812562A (en) * | 2010-04-21 | 2010-08-25 | 周建安 | Safe and high-efficiency recovery method for converter gas |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59100207A (en) * | 1982-12-01 | 1984-06-09 | Kobe Steel Ltd | Method for recovering converter gas |
-
2014
- 2014-12-23 CN CN201410810257.3A patent/CN105779683B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671757A (en) * | 2009-10-14 | 2010-03-17 | 中冶赛迪工程技术股份有限公司 | Converter coal gas dry-method bag-type dust collecting and waste heat recovery method |
| CN101812562A (en) * | 2010-04-21 | 2010-08-25 | 周建安 | Safe and high-efficiency recovery method for converter gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105779683A (en) | 2016-07-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105779683B (en) | Converter gas recovery system and recovery method | |
| CN105779684B (en) | Converter gas recovery system and recovery method thereof | |
| CN101250419B (en) | Low-temperature dry distillation process with coal gas internal heat | |
| CN109086949B (en) | Blast furnace gas generation amount and heat value prediction method based on gas component change | |
| CN108977615A (en) | A kind of high-efficiency comprehensive utilization method of biomass powder | |
| CN103509605B (en) | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production | |
| CN103525465B (en) | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent | |
| CN103276131B (en) | Comprehensive utilization process method of waste heat, residual pressure and residual gas of high-temperature raw gas | |
| CN205347482U (en) | System for still crude gas direct reduction is metallurgical to utilize carbide stove tail gas system | |
| CN102391892B (en) | Blast furnace gas enrichment apparatus and method | |
| CN109971916B (en) | Device and method for preheating scrap steel by using converter waste gas | |
| CN203530252U (en) | Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents | |
| CN209227008U (en) | A kind of blast furnace gas purification recovery system | |
| CN115651677A (en) | Dry quenching process without burning loss | |
| CN102277196B (en) | Method for producing and synthetizing ammonia and methyl alcohol raw material gas by virtue of fixed bed intermittence type oxygenation nature gas | |
| CN111961781B (en) | Recycling method of surplus metallurgical gas | |
| CN101988804B (en) | Device and method for drying blast furnace ores and coke groove by recycling residual heat of circular cooler | |
| CN101392187B (en) | Bidirectional oxygen-enriched continuous gasification process for atmospheric fixed bed gas furnace | |
| CN104893746A (en) | Carbocoal heat recycling system and recycling process | |
| CN112662824A (en) | Blast furnace hydrogen-rich smelting process for efficiently utilizing metallurgical waste gas | |
| CN113755658A (en) | Secondary energy storage system based on waste heat utilization of steel plant | |
| CN201737908U (en) | Biomass energy balance process control system | |
| CN111117671A (en) | Low-rank coal segmented upgrading and hot flue gas gradient utilization system and utilization method thereof | |
| CN205473585U (en) | Integrative stove of powder coal carbonization activation | |
| CN104845674A (en) | Furnace steam volume decreasing semi-water gas production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |