CN101906532B - Process and equipment for producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting - Google Patents
Process and equipment for producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting Download PDFInfo
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- CN101906532B CN101906532B CN 201010252066 CN201010252066A CN101906532B CN 101906532 B CN101906532 B CN 101906532B CN 201010252066 CN201010252066 CN 201010252066 CN 201010252066 A CN201010252066 A CN 201010252066A CN 101906532 B CN101906532 B CN 101906532B
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- 229910000476 molybdenum oxide Inorganic materials 0.000 title claims abstract description 37
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 28
- 239000011593 sulfur Substances 0.000 title claims abstract description 28
- 125000004122 cyclic group Chemical group 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 101
- 239000012716 precipitator Substances 0.000 claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 29
- 239000002893 slag Substances 0.000 claims abstract description 17
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052750 molybdenum Inorganic materials 0.000 claims abstract description 13
- 239000011733 molybdenum Substances 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 91
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000002253 acid Substances 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 14
- 239000003546 flue gas Substances 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000001354 calcination Methods 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 10
- 230000005611 electricity Effects 0.000 claims description 9
- 238000007654 immersion Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 7
- 230000005587 bubbling Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 abstract description 3
- MEFBJEMVZONFCJ-UHFFFAOYSA-N molybdate Chemical compound [O-][Mo]([O-])(=O)=O MEFBJEMVZONFCJ-UHFFFAOYSA-N 0.000 abstract description 3
- 238000003723 Smelting Methods 0.000 abstract description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000446 fuel Substances 0.000 abstract description 2
- 239000012141 concentrate Substances 0.000 abstract 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000002269 spontaneous effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 8
- 241001417490 Sillaginidae Species 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 210000000038 chest Anatomy 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
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Abstract
The invention discloses a process and equipment for producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting. In the invention, a two-stage fluidized bed roasting production mode is adopted to produce molybdenum oxide; a first-stage roasting dust collection device, a second-stage roasting dust collection device and an electro-precipitator are utilized to feed molybdenum concentrate into a first-stage fluidized bed furnace so that the molybdenum concentrate and the air sent by an air blower in the furnace are subject to roasting reaction; the materials from the discharge port of the first-stage fluidized bed furnace enters into a second-stage fluidized bed furnace to be subject to roasting reaction; and the materials from the discharge port of the second-stage fluidized bed furnace is transmitted to a finished material bin through an immersed roller slag extractor. The invention can solve the problems existing in the prior art, enable molybdenum oxide production to occupy less personnel and have high automaticity, realize energy conservation and emission reduction, and adopt a mode of not using fuel spontaneous ignition to improve production capacity; and the produced molybdenum oxide has the sulfur content less than 0.1%, satisfies smelting requirements, has the solubility above 99% and can satisfy molybdate production.
Description
Technical field
The present invention relates to technical field of smelting, relate generally to a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technology and equipments.
Background technology
At present, the technology status of molybdenum roasting both at home and abroad, the technology and equipment of employing is single thorax reverberatory furnace, inside and outside heating rotary pipe kiln, multiple hearth furnace.The reverberatory furnace mechanization degree is low owing to adopting, labour intensity is large, the molybdenum loss is many, and only can batch operation, therefore seldom use in scale operation, adopt the return bend kiln to have the following disadvantages: 1. 4. how low 3. operator of the little 2. rate of recovery of separate unit stove throughput produce the molybdenum oxide soluble rate low 5. the stove stopping property be poor; Adopt multiple hearth furnace that following deficiency is arranged: 1. investment is large, and more 3. fixed cost height 2. energy consumption produces that 4. the molybdenum oxide soluble rate is low requires that in the raw material concentrated molybdenum ore, Ca and Cu content can not be too high.
Summary of the invention
Deficiency for the technology and equipment that overcomes existing roasting exists the purpose of this invention is to provide a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technology and equipments.Can solve the problem that prior art exists, realize energy-saving and emission-reduction, take not use the mode of fuel nature, improve throughput, the molybdenum oxide of production not only sulphur content less than 0.1%, satisfies and smelts needs, soluble rate reaches more than 99% simultaneously, can satisfy molybdate production.
For achieving the above object, the present invention adopts technical scheme as described below:
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique adopts the mode of production of boiling circulation roasting to produce molybdenum oxide, and its step is as follows:
1), concentrated molybdenum ore is sent into the first paragraph fluidizing furnace with the concentrated molybdenum ore that self-conveyor feed will be stored in loading hopper, make it with stove in the air generation calcination of being sent here by gas blower, the bubbling bed temperature of first paragraph fluidizing furnace is arranged on 550 ℃ to 650 ℃, and the water yield that enters the water tank of first paragraph fluidizing furnace by adjusting is controlled the temperature of boiling bed;
2), the high-temperature furnace gas that goes out from first paragraph fluidizing furnace top separates through first step cyclone and gathers dust, the furnace gas of separation separates and gathers dust through the cooling second stage cyclonic separator that enters of a pair of burner-gas cooler again, the furnace gas of separation by T-valve to dust precipitator; The dirt that described first step cyclone is received and gathering dust by the slurrying tank of the first incoming stock feed bin of scraper conveyor that the dirt of a pair of burner-gas cooler refrigerated separation separates with second stage cyclonic separator; The material of described first paragraph fluidizing furnace discharge port enters second segment fluidizing furnace generation calcination;
3), the hot gas that the heat of first paragraph fluidizing furnace outlet high-temperature furnace gas exchanged by heat exchange by gas blower of second segment fluidizing furnace enters the material generation calcination of second segment fluidizing furnace and first paragraph fluidizing furnace discharge port, the fluidizing furnace temperature of roasting is arranged on 550 ℃ to 650 ℃; The water yield that enters the water tank of second segment fluidizing furnace by adjusting is controlled the temperature of boiling bed;
4), be cooled to cyclone (4b) from the furnace gas of the furnace gas export of second segment fluidizing furnace through burner-gas cooler and separate and gather dust, the furnace gas of separation by T-valve to dust precipitator; The dirt that the cooling dirt of receiving of described burner-gas cooler, cyclone are received turns back to the material inlet of second segment fluidizing furnace by the second scraper conveyor, the material of second segment boiling roaster discharge port enters finished product bin by the immersion drum slag discharger; Or enter finished product bin by embedded scraper transporter, drum slag discharger;
5), described dust precipitator is respectively with the roasting high-temperature furnace gas of first paragraph fluidizing furnace and second segment fluidizing furnace, furnace gas after two sections cyclones gather dust separation carries out the dry type electricity again and gathers dust, and the material that the dry type electricity gathers dust is by the slurrying tank of the incoming stock feed bin of embedded scraper transporter;
6), the raw material of described slurrying tank reenters one section roasting by the screw feed en-trance that turns back to one section stoving oven through acid proof pump;
7), through the SO after the dry type dust precipitator
2Flue gas enters the relieving haperacidity of flue gas acid preparing system.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique, the adjusting of the bubbling bed temperature of first paragraph fluidizing furnace, the water yield of employing water tank is controlled the temperature of boiling bed.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique, the ore deposit amount that adds of first paragraph fluidizing furnace, adopt the oxygen table to add ore deposit amount self-reacting device, its method is: after air output is constant, only need to regulate the ore deposit amount that adds, the temperature of bed control well between 550 ℃ to 650 ℃, control SO in the furnace gas of first paragraph fluidizing furnace
2Concentration between 5.5% to 6.5%.
Implement a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit of above-mentioned technique, comprise: first paragraph roasting dust collection device, second segment roasting dust collection device and dust precipitator, the furnace gas export end of the furnace gas export end of described first paragraph roasting dust collection device, second segment roasting dust collection device is connected to dust precipitator by T-valve respectively; The exit end that gathers dust of gather dust exit end and the dust precipitator of described first paragraph roasting dust collection device is connected to the screw feed en-trance of first paragraph stoving oven level first paragraph fluidizing furnace by e Foerderanlage; The exit end that gathers dust of described second segment roasting dust collection device is connected to the opening for feed of second segment stoving oven level second segment fluidizing furnace by e Foerderanlage; The discharge port of described first paragraph fluidizing furnace is communicated with the opening for feed of second segment fluidizing furnace, and the discharge port of second segment fluidizing furnace is connected to finished product bin by the immersion drum slag discharger;
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit, described first paragraph roasting dust collection device is connected to burner-gas cooler by first step cyclone through interchanger by the first paragraph fluidizing furnace, and described burner-gas cooler is made of two burner-gas cooler series connection; Described burner-gas cooler by second stage cyclone through T-valve to dust precipitator; Described first paragraph fluidizing furnace exit end is communicated with the material inlet end of second segment fluidizing furnace by pipeline; The gather dust exit end of exit end, second stage cyclone bottom of exit end, burner-gas cooler bottom of described first step cyclone is connected to respectively the slurrying tank of raw material feed bin by the first scraper conveyor.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit, described second segment roasting dust collection device is connected to cyclone by the second segment fluidizing furnace by burner-gas cooler, described cyclone by T-valve to dust precipitator; The exit end of described burner-gas cooler bottom and the exit end bottom cyclone are connected to respectively the material inlet end of second segment fluidizing furnace by the second scraper conveyor; The high temperature tracheae at described second segment fluidizing furnace top is communicated with the high temperature tracheae at first paragraph fluidizing furnace top; The exit end that gathers dust of described dust precipitator is connected to slurrying tank by the 3rd scraper conveyor; The screw feed en-trance of pipeline to the section stoving oven level first paragraph fluidizing furnace that described slurrying tank connects by acid proof pump; The material of described second segment boiling roaster discharge port is connected to finished product bin by the immersion drum slag discharger.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit, the exit end gas of described dust precipitator are the relieving haperacidity flue gas SO that enters the flue gas acid preparing system
2
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit, described first paragraph fluidizing furnace, second segment fluidizing furnace are oxidized still.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit, the bottom of described first paragraph fluidizing furnace and second segment fluidizing furnace are respectively arranged with the gas blower of carrying air and warm air.
Described producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit is provided with some waterworkss above described drum slag discharger.
Owing to adopting technical scheme as above, the present invention has advantages of as described below:
This producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technology and equipments adopts boiling circulation roasting, can produce the high dissolubility molybdenum oxide of low-sulfur, and product can not only satisfy smelts use, can be used as simultaneously the production molybdate and uses.After adopting this processing unit, do not re-use the heat sources such as Sweet natural gas and coal due to roasting, can greatly reduce energy consumption, investment cost is low simultaneously, tail gas SO
2Concentration reaches more than 6%, can adopt the relieving haperacidity of conventional double conversion and double absorption mode.It is few that molybdenum oxide production takies personnel, and level of automation is high.Production capacity significantly improves, and sweetening effectiveness is good, and first-time qualification rate is high.The rate of recovery is higher, year can economize on electricity, coal etc.Easy to maintenance, good dedusting effect.
Description of drawings
Fig. 1 is the production technique figure of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting.
In figure: 1-first paragraph fluidizing furnace; The 2-cyclone; 3 (a.b)-burner-gas coolers; The 4-secondary cyclone; 5-second segment fluidizing furnace; The 6-dust precipitator; The 7-drum slag discharger; The 8-embedded scraper transporter; The 9-slurrying tank; The 10-acid proof pump; The 11-gas blower; The 12-waterworks; The 13-finished product bin; The 14-T-valve; The 15-interchanger.
Embodiment
As shown in fig. 1, a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique adopts the mode of production of boiling circulation roasting to produce molybdenum oxide, and its step is as follows:
1), concentrated molybdenum ore is sent into the first paragraph fluidizing furnace with the concentrated molybdenum ore that self-conveyor feed will be stored in loading hopper, make it with stove in the air generation calcination of being sent here by gas blower (11a), the bubbling bed temperature of first paragraph fluidizing furnace (1) is arranged on 550 ℃ to 650 ℃, and the water yield that enters the water tank of first paragraph fluidizing furnace by adjusting is controlled the temperature of boiling bed;
2) high-temperature furnace gas that, goes out from first paragraph fluidizing furnace top separates through first step cyclone (2) and gathers dust, the furnace gas that separates separates and gathers dust through the cooling second stage cyclonic separator (4a) that enters of a pair of burner-gas cooler (3a) again, the furnace gas of separation by T-valve (14) to dust precipitator (6); What the dirt of the dirt that described first step cyclone (2) is received and a pair of burner-gas cooler (3a) refrigerated separation separated with second stage cyclonic separator (4a) gathers dust by the slurrying tank (9) of the first incoming stock feed bin of scraper conveyor; The material of described first paragraph fluidizing furnace (1) discharge port enters second segment fluidizing furnace (5) calcination occurs;
3), the hot gas that the heat of first paragraph fluidizing furnace (1) outlet high-temperature furnace gas exchange by heat exchange by gas blower (11b) of second segment fluidizing furnace (5) enters the material generation calcination of second segment fluidizing furnace (5) and first paragraph fluidizing furnace (1) discharge port, the fluidizing furnace temperature of roasting is arranged on 550 ℃ to 650 ℃; The water yield that enters the water tank of second segment fluidizing furnace (5) by adjusting is controlled the temperature of boiling bed;
4), be cooled to cyclone (4b) from the furnace gas of the furnace gas export of second segment fluidizing furnace (5) through burner-gas cooler (3b) and separate and gather dust, the furnace gas of separation by T-valve (14) to dust precipitator (6); The dirt that the cooling dirt of receiving of described burner-gas cooler (3b), cyclone (4b) are received turns back to the material inlet of second segment fluidizing furnace by the second scraper conveyor (8b), the material of second segment fluidizing furnace (5) roasting discharge port enters finished product bin (13) by immersion drum slag discharger (7); Or enter finished product bin by embedded scraper transporter, drum slag discharger;
5), described dust precipitator (6) is respectively with the roasting high-temperature furnace gas of first paragraph fluidizing furnace and second segment fluidizing furnace, furnace gas after two sections cyclones gather dust separation carries out the dry type electricity again and gathers dust, and the material that the dry type electricity gathers dust is by the slurrying tank (9) of the incoming stock feed bin of embedded scraper transporter;
6), the raw material of described slurrying tank (9) reenters one section roasting by the screw feed en-trance that turns back to one section stoving oven through acid proof pump;
7), through the SO after dry type dust precipitator (6)
2Flue gas enters the relieving haperacidity of flue gas acid preparing system.
The adjusting of the bubbling bed temperature of described first paragraph fluidizing furnace (1), the water yield of employing water tank is controlled the temperature of boiling bed.
The ore deposit amount that adds of described first paragraph fluidizing furnace (1), adopt the oxygen table to add ore deposit amount self-reacting device, its method is: after air output is constant, only need to regulate the ore deposit amount that adds, the temperature of bed control well between 550 ℃ to 650 ℃, control SO in the furnace gas of first paragraph fluidizing furnace (1)
2Concentration between 5.5% to 6.5%.
Implement a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit of above-mentioned technique, comprise: first paragraph roasting dust collection device, second segment roasting dust collection device and dust precipitator, the furnace gas export end of the furnace gas export end of described first paragraph roasting dust collection device, second segment roasting dust collection device is connected to dust precipitator (6) by T-valve (14) respectively; The exit end that gathers dust of gather dust exit end and the dust precipitator (6) of described first paragraph roasting dust collection device is connected to the screw feed en-trance of first paragraph stoving oven level first paragraph fluidizing furnace (1) by e Foerderanlage; The exit end that gathers dust of described second segment roasting dust collection device is connected to the opening for feed of second segment stoving oven level second segment fluidizing furnace (5) by e Foerderanlage; The discharge port of described first paragraph fluidizing furnace (1) is communicated with the opening for feed of second segment fluidizing furnace (5), and the discharge port of second segment fluidizing furnace (5) is connected to finished product bin (13) by immersion drum slag discharger (7);
Described first paragraph roasting dust collection device is connected to burner-gas cooler (3a) by first step cyclone (2) through interchanger by first paragraph fluidizing furnace (1), and described burner-gas cooler (3a) is made of two burner-gas cooler series connection; Described burner-gas cooler (3a) by second stage cyclone (4a) through T-valve (14) to dust precipitator (6); Described first paragraph fluidizing furnace (1) exit end is communicated with by the material inlet end of pipeline with second segment fluidizing furnace (5); The gather dust exit end of exit end, second stage cyclone (4a) bottom of exit end, burner-gas cooler (3a) bottom of described first step cyclone (2) is connected to respectively the slurrying tank (9) of raw material feed bin by the first scraper conveyor (8a);
Described second segment roasting dust collection device is connected to cyclone (4b) by the second segment fluidizing furnace by burner-gas cooler (3b), and described cyclone (4b) passes through T-valve (14) to dust precipitator (6); The exit end of described burner-gas cooler (3b) bottom and the exit end bottom cyclone (4b) are connected to respectively the material inlet end of second segment fluidizing furnace (5) by the second scraper conveyor (8b); The high temperature tracheae at described second segment fluidizing furnace (5) top is communicated with the high temperature tracheae at first paragraph fluidizing furnace (1) top; The exit end that gathers dust of described dust precipitator (6) is connected to slurrying tank (9) by the 3rd scraper conveyor (8c); Described slurrying tank (9) is by the screw feed en-trance of pipeline to the section stoving oven level first paragraph fluidizing furnace (1) of acid proof pump (10) connection; The material of described second segment fluidizing furnace (5) roasting discharge port is delivered to finished product bin (13) by immersion drum slag discharger (7).
Described first paragraph fluidizing furnace (1), second segment fluidizing furnace (5) are oxidized still.The bottom of described first paragraph fluidizing furnace (1) and second segment fluidizing furnace (5) is respectively arranged with the gas blower (11a.11b) of carrying air and warm air.The exit end gas of described dust precipitator is the relieving haperacidity flue gas SO that enters the flue gas acid preparing system
2Described drum slag discharger top is provided with some waterworkss (12).
During use, concentrated molybdenum ore is sent into fluidizing furnace with the concentrated molybdenum ore that self-conveyor feed will be stored in loading hopper, makes it the air generation calcination sent here with air-blaster, and bubbling bed temperature maintains 600 ℃, and the water yield that enters water tank by adjusting is controlled the temperature of bed.Adopt oxygen Biao-Jia ore deposit amount self-reacting device.After air output is certain, only needs to regulate and add the ore deposit amount, control the temperature of bed well, just can control SO in furnace gas
2Concentration 6%.
The high-temperature furnace gas that goes out from first paragraph fluidizing furnace (1) top, through cyclone dust collection, burner-gas cooler and secondary cyclone, the dirt of receiving turn back to first paragraph fluidizing furnace opening for feed; The material of first paragraph fluidizing furnace (1) discharge port enters second segment fluidizing furnace (5) calcination occurs, the fluidizing furnace temperature maintains 600 ℃, water cooler from second segment fluidizing furnace (5) furnace gas export, the dirt that cyclone is received returns to second segment fluidizing furnace (5) roasting opening for feed, the material of the roasting discharge port of second segment fluidizing furnace (5) enters finished product bin (13) by immersion drum slag discharger (7).
The roasting of first paragraph fluidizing furnace (1) and second segment fluidizing furnace (5) enters dry type dust precipitator (6) after two sections cyclones, the screw feed en-trance that the material that the dry type electricity gathers dust turns back to first paragraph fluidizing furnace (1) stoving oven reenters one section roasting.SO after gathering dust through dry type dust precipitator (6) electricity
2Flue gas enters the relieving haperacidity of flue gas acid preparing system.
Claims (7)
1. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique is characterized in that: adopt the mode of production of boiling circulation roasting to produce molybdenum oxide, its step is as follows:
1), concentrated molybdenum ore is sent into the first paragraph fluidizing furnace with the concentrated molybdenum ore that self-conveyor feed will be stored in loading hopper, make it with stove in the air generation calcination of being sent here by gas blower (11a), the bubbling bed temperature of first paragraph fluidizing furnace (1) is arranged on 550 ℃ to 650 ℃, and the water yield that enters the water tank of first paragraph fluidizing furnace by adjusting is controlled the temperature of boiling bed;
2) high-temperature furnace gas that, goes out from first paragraph fluidizing furnace top separates through first step cyclone (2) and gathers dust, the furnace gas that separates separates and gathers dust through the cooling second stage cyclonic separator (4a) that enters of a pair of burner-gas cooler (3a) again, the furnace gas of separation by T-valve (14) to dust precipitator (6); What the dirt of the dirt that described first step cyclone (2) is received and a pair of burner-gas cooler (3a) refrigerated separation separated with second stage cyclonic separator (4a) gathers dust by the slurrying tank (9) of the first incoming stock feed bin of scraper conveyor; The material of described first paragraph fluidizing furnace (1) discharge port enters second segment fluidizing furnace (5) calcination occurs;
3), the hot gas that the heat of first paragraph fluidizing furnace (1) outlet high-temperature furnace gas exchange by heat exchange by gas blower (11b) of second segment fluidizing furnace (5) enters the material generation calcination of second segment fluidizing furnace (5) and first paragraph fluidizing furnace (1) discharge port, the fluidizing furnace temperature of roasting is arranged on 550 ℃ to 650 ℃; The water yield that enters the water tank of second segment fluidizing furnace (5) by adjusting is controlled the temperature of boiling bed;
4), be cooled to cyclone (4b) from the furnace gas of the furnace gas export of second segment fluidizing furnace (5) through burner-gas cooler (3b) and separate and gather dust, the furnace gas of separation by T-valve (14) to dust precipitator (6); The dirt that the cooling dirt of receiving of described burner-gas cooler (3b), cyclone (4b) are received turns back to the material inlet of second segment fluidizing furnace by the second scraper conveyor (8b), the material of second segment fluidizing furnace (5) roasting discharge port enters finished product bin (13) by immersion drum slag discharger (7); Or enter finished product bin by embedded scraper transporter, drum slag discharger;
5), described dust precipitator (6) is respectively with the roasting high-temperature furnace gas of first paragraph fluidizing furnace and second segment fluidizing furnace, furnace gas after two sections cyclones gather dust separation carries out the dry type electricity again and gathers dust, and the material that the dry type electricity gathers dust is by the slurrying tank (9) of the incoming stock feed bin of embedded scraper transporter;
6), the raw material of described slurrying tank (9) reenters one section roasting by the screw feed en-trance that turns back to one section stoving oven through acid proof pump;
7), through the SO after dry type dust precipitator (6)
2Flue gas enters the relieving haperacidity of flue gas acid preparing system.
2. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production technique according to claim 1, it is characterized in that: the ore deposit amount that adds of first paragraph fluidizing furnace (1), adopt the oxygen table to add ore deposit amount self-reacting device, its method is: after air output is constant, only need to regulate the ore deposit amount that adds, the temperature of bed control well between 550 ℃ to 650 ℃, control SO in the furnace gas of first paragraph fluidizing furnace (1)
2Concentration between 5.5% to 6.5%.
3. implement a kind of producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit of the described technique of claim 1, it is characterized in that: comprising: first paragraph roasting dust collection device, second segment roasting dust collection device and dust precipitator, the furnace gas export end of the furnace gas export end of described first paragraph roasting dust collection device, second segment roasting dust collection device is connected to dust precipitator (6) by T-valve (14) respectively; The exit end that gathers dust of gather dust exit end and the dust precipitator (6) of described first paragraph roasting dust collection device is connected to the screw feed en-trance of first paragraph stoving oven level first paragraph fluidizing furnace (1) by e Foerderanlage; The exit end that gathers dust of described second segment roasting dust collection device is connected to the opening for feed of second segment stoving oven level second segment fluidizing furnace (5) by e Foerderanlage; The discharge port of described first paragraph fluidizing furnace (1) is communicated with the opening for feed of second segment fluidizing furnace (5), and the discharge port of second segment fluidizing furnace (5) is connected to finished product bin (13) by immersion drum slag discharger (7);
Wherein, first paragraph roasting dust collection device is connected to burner-gas cooler (3a) by first step cyclone (2) through interchanger by first paragraph fluidizing furnace (1), and described burner-gas cooler (3a) is made of two burner-gas cooler series connection; Described burner-gas cooler (3a) by second stage cyclone (4a) through T-valve (14) to dust precipitator (6); Described first paragraph fluidizing furnace (1) exit end is communicated with by the material inlet end of pipeline with second segment fluidizing furnace (5); The gather dust exit end of exit end, second stage cyclone (4a) bottom of exit end, burner-gas cooler (3a) bottom of described first step cyclone (2) is connected to respectively the slurrying tank (9) of raw material feed bin by the first scraper conveyor (8a);
Wherein, second segment roasting dust collection device is connected to cyclone (4b) by the second segment fluidizing furnace by burner-gas cooler (3b), and described cyclone (4b) passes through T-valve (14) to dust precipitator (6); The exit end of described burner-gas cooler (3b) bottom and the exit end bottom cyclone (4b) are connected to respectively the material inlet end of second segment fluidizing furnace (5) by the second scraper conveyor (8b); The high temperature tracheae at described second segment fluidizing furnace (5) top is communicated with the high temperature tracheae at first paragraph fluidizing furnace (1) top; The exit end that gathers dust of described dust precipitator (6) is connected to slurrying tank (9) by the 3rd scraper conveyor (8c); Described slurrying tank (9) is by the screw feed en-trance of pipeline to the section stoving oven level first paragraph fluidizing furnace (1) of acid proof pump (10) connection.
4. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit according to claim 3, it is characterized in that: the exit end gas of described dust precipitator is the relieving haperacidity flue gas SO that enters the flue gas acid preparing system
2
5. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit according to claim 3, it is characterized in that: described first paragraph fluidizing furnace (1), second segment fluidizing furnace (5) are oxidized still.
6. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit according to claim 3 is characterized in that: the bottom of described first paragraph fluidizing furnace (1) and second segment fluidizing furnace (5) is respectively arranged with the gas blower (11a.11b) of carrying air and warm air.
7. producing soluble low-sulfur molybdenum oxide by cyclic fluidized bed roasting production unit according to claim 3, is characterized in that: be provided with some waterworkss (12) above described drum slag discharger.
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| CN103031433B (en) * | 2011-09-30 | 2014-07-30 | 中国科学院过程工程研究所 | Fluidized oxidation roasting-fluidized reduction roasting system and roasting process for titaniferous iron concentrate |
| CN103031432B (en) * | 2011-09-30 | 2014-09-24 | 中国科学院过程工程研究所 | System for fluidized oxidizing/reducing roasting modification of titaniferous iron concentrate and roasting process |
| CN102653821A (en) * | 2012-04-27 | 2012-09-05 | 洛阳栾川钼业集团股份有限公司 | Fluidized bed furnace device for circularly roasting molybdenum concentrates and method for using same |
| CN104495933B (en) * | 2014-12-12 | 2016-05-18 | 江西省鼎力金属有限公司 | Molybdenum oxide nano particle process units and production method |
| CN104477996B (en) * | 2014-12-17 | 2016-03-16 | 金堆城钼业股份有限公司 | The rapid cooling technique of high soluble molybdenum oxide needed for a kind of production of molybdic ammonium |
| CN108149006B (en) * | 2017-12-25 | 2019-10-08 | 东北大学 | Molybdenite concentrate self-heating eddy flow roasting technique and equipment |
| CN110902656A (en) * | 2019-12-12 | 2020-03-24 | 南京乾盛化工科技有限公司 | Production method for preparing sulfuric acid from molybdenum concentrate |
| CN114959250A (en) * | 2022-04-21 | 2022-08-30 | 中国恩菲工程技术有限公司 | Molybdenum concentrate roasting system and method |
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