Classifications

• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B5/00—General methods of reducing to metals
  • C22B5/02—Dry methods smelting of sulfides or formation of mattes
  • C22B5/10—Dry methods smelting of sulfides or formation of mattes by solid carbonaceous reducing agents
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B47/00—Obtaining manganese
  • C22B47/0018—Treating ocean floor nodules
  • C22B47/0027—Preliminary treatment
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B47/00—Obtaining manganese
  • C22B47/0018—Treating ocean floor nodules
  • C22B47/0036—Treating ocean floor nodules by dry processes, e.g. smelting
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B4/00—Electrothermal treatment of ores or metallurgical products for obtaining metals or alloys
  • C22B4/08—Apparatus
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B47/00—Obtaining manganese
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
  • C22B9/10—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents
  • C22B9/103—Methods of introduction of solid or liquid refining or fluxing agents
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
  • C22B9/10—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents
  • C22B9/106—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals with refining or fluxing agents; Use of materials therefor, e.g. slagging or scorifying agents the refining being obtained by intimately mixing the molten metal with a molten salt or slag
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
  • C22B9/16—Remelting metals
  • C22B9/22—Remelting metals with heating by wave energy or particle radiation
  • C22B9/226—Remelting metals with heating by wave energy or particle radiation by electric discharge, e.g. plasma
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F27—FURNACES; KILNS; OVENS; RETORTS
  • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
  • F27B3/00—Hearth-type furnaces, e.g. of reverberatory type; Tank furnaces
  • F27B3/10—Details, accessories, or equipment peculiar to hearth-type furnaces

Definitions

• the invention relates to a method for preheating and smelting manganese ore sinter as defined in the preamble of independent claim 1.
• the invention also relates to an apparatus for preheating and smelting manganese ore sinter as defined in the preamble of independent claim 14. Objective of the invention
• the object of the invention is to provide a method and an arrangement for energy efficient smelting manganese ore sinter.
• the method for preheating and smelting manganese ore sinter is characterized by the definitions of independent claim 1.
• the apparatus for preheating smelting manganese ore sinter is correspondingly characterized by the definitions of independent claim 14.
• the invention is based on preheating the feed mixture containing at least manganese ore sinter and reducing agent in order to eliminate the moisture from the feed mixture and to preheat the feed mixture to as high a temperature as possible without burning or loosing carbon in the reduction agent required for reduction purposes in the feed mixture.
• Boudouard reaction (C(s) + C0 2 (g) ⁇ 2CO (g)), is an limiting factor. Water gas reaction occurs also, H 2 0 + C H 2 + CO.
• the preheating temperature in the pre-treatment silo can locally be maximum 600 to 700 °C, depending on the reactivity of the carbon in the reducing agent of the feed mixture.
• the average temperature of the hot charge to the electric furnace is typically below 600°C.
• Preheating of the feed mixture saves electrical energy of the submerged electric arc furnace, improves the operation, improves production and safety of the smelting by preventing reaction between carbon and oxygen in the feed mixture and prevents thus uncontrolled increase of temperature and possible explosions.
• Figure 2 shows a flow sheet of second embodiment.
• the method comprises a feeding step for feeding feed mixture 1 comprising at least manganese ore sinter 2, reducing agent 3 , and fluxing agent 4 into an submerged electric arc furnace 5.
• the method comprises a smelting step for smelting said feed mixture 1 in the submerged electric arc furnace 5 to form a layer containing liquid manganese alloy (not shown in the drawings) and a layer containing slag (not shown in the drawings) above the layer containing liquid manganese alloy.
• the method comprises a withdrawing step for withdrawing liquid manganese alloy and slag separately or simultaneously from the submerged electric arc furnace 5.
• the method comprises a first discharging step for discharging carbon monoxide containing carbonaceous gas 6 from the submerged electric arc furnace 5.
• the method comprises a combusting step for combusting carbon monoxide containing carbonaceous gas 6 discharged in the first discharging step from the submerged electric arc furnace 5 in presence of oxygen such as air in a burner 7 to form carbon dioxide containing carbonaceous gas 9.
• the feeding step of the method comprises a heating step for heating said feed mixture 1 with said carbon dioxide containing carbonaceous gas 9 formed in the combusting step in a pre- treatment silo 8 prior feeding feed mixture 1 into the submerged electric arc furnace 5.
• the submerged electric arc furnace 5 that is used in the method is preferably an alternating current (AC) submerged electric arc furnace 5.
• AC alternating current
• the burner 7 is preferably connected to the pre-treatment silo 8 and the pre-treatment silo 8 is preferably connected to the submerged electric arc furnace 5 so that gases such as oxygen from the ambient air is prevented from entering the burner 7, the pre-treatment silo 9 and the submerged electric arc furnace 5 so as to prevent uncontrolled reactions of said feed material 1.
• the manganese ore sinter 9 may have a particle size between 6 and 75 mm.
• the method may include heating the feed mixture 1 in the heating step to a temperature in the range between 400 and 700°C preferably to a temperature between 500 and 650°C.
• the method includes preferably, but not necessarily, adjusting the temperature of said carbon dioxide containing carbonaceous gas 9 that is used in the heating step.
• the temperature of the said carbon dioxide containing carbonaceous gas 9 that is used in the heating step may be controlled to a temperature in the range between 600 and 900°C.
• the carbon monoxide containing carbonaceous gas 6 received from the submerged electric arc furnace 5 is preferably burned by an air ratio below 1, such as between 0.9 and 0.95.
• Oxygen (0 2 ) content in the carbon dioxide containing carbonaceous gas 9 formed in the combusting step should be very low to minimize the oxidation of carbon in the feed mixture 1.
• the content of carbon monoxide (CO) and hydrogen (H 2 ) in the carbon dioxide containing carbonaceous gas 9 formed in the combusting step should be very low for avoiding the explosions in the gas lines especially between the burner 7 and the pre-treatment silo 8 or in the pre-treatment silo 8.
• the method may include burning carbon monoxide containing carbonaceous gas 6 discharged from the submerged electric arc furnace 5 by means of butane in the burning step
• the method may include burning carbon monoxide containing carbonaceous gas 6 discharged from the submerged electric arc furnace 5 by means of CO gas or e.g. butane (C 4 H 10 ) in the burning step so that the molar ratio of air to butane is in the range between 0.9 - 0.95.
• the carbon dioxide containing carbonaceous gas 9 that is formed in the combusting step and that is used in the heating step, may containing in percentages of volume:
• N 2 between 50 and 65 %
• H 2 0 between 3 and 8 % H 2 0
• the heating step comprises preferably heating said feed mixture 1 by feeding said carbon dioxide containing carbonaceous gas 9 formed in the combusting step into the pre-treatment silo 8.
• the heating step includes preferably feeding said carbon dioxide containing carbonaceous gas 9 formed in the combusting step into the pre-treatment silo 8 from below so that carbon dioxide containing carbonaceous gas 9 flows in the opposite direction, such as upwards, with respect the feed mixture in the pre-treatment silo 8.
• the method may, as shown in figure 2, include a first scrubbing step of the carbon monoxide gas 6 discharged from the submerged electric arc furnace 5. This is prior burning the carbon monoxide gas 6 in the burner 7.
• the method may, as shown in figure 2, include a second discharging step for discharging carbon dioxide containing carbonaceous gas 9 from the pre-treatment silo 8 and for feeding carbon dioxide containing carbonaceous gas 9 discharged from the pre-treatment silo 8 to the burner 7 and/or into the carbon dioxide containing carbonaceous gas 9 that is formed in the combusting step by means of the burner 7 to adjust the temperature of the carbon dioxide containing carbonaceous gas 9 that is formed in the combusting step.
• the method may include a second scrubbing step for scrubbing carbon dioxide containing carbonaceous gas 9 discharged in the second discharging step from the pre-treatment silo 8 in a second scrubber 11.
• the reducing agent 3 of the feed mixture 1 may contain carbonaceous material such as metallurgical coke, anthracite or charcoal.
• the fluxing agent 4 of the feed mixture 1 may contain e.g. calcite, coarse burned lime, quartz, dolomite.
• the chemical analysis of the manganese ore sinter 2 is depending on the chemical analysis of manganese ore.
• Manganese ores are calcium based, carbonate based and oxidized based which of chemical analyses greatly varies.
• a possible content of the manganese ore sinter 2 is:
• the apparatus comprises a submerged electric arc furnace 5 for smelting feed mixture 1 comprising at least manganese ore sinter 2, reducing agent 3, and fluxing agent 4.
• a layer containing liquid manganese alloy and a layer containing slag above the layer containing liquid manganese alloy are formed in the smelting in the submerged electric arc furnace 5.
• the apparatus comprises first feeding means 12 configured to feed said feed mixture 1 into the submerged electric arc furnace 5.
• the apparatus comprises withdrawing means 13 for withdrawing liquid manganese and slag separately or simultaneously from the submerged electric arc furnace 5.
• the apparatus comprises first discharging means 14 for discharging carbon monoxide containing carbonaceous gas 6 from the submerged electric arc furnace 5.
• the apparatus comprises a burner 7 for combusting carbon monoxide containing carbonaceous gas 6 received from the first discharging means 14 in presence of oxygen such as air to form carbon dioxide containing carbonaceous gas 9.
• the first feeding means 12 of the apparatus comprises a pre-treatment silo 8 for heating said feed mixture 1 with said carbon dioxide containing carbonaceous gas 9 formed by means of the burner 7 prior feeding said feed mixture 1 into the submerged electric arc furnace 5.
• the submerged electric arc furnace 5 in the apparatus is preferably an alternating current (AC) submerged electric arc furnace 5.
• AC alternating current
• the burner 7 is preferably connected to the pre-treatment silo 8 and the pre-treatment silo 8 is preferably connected to the submerged electric arc furnace 5 so that gases such as oxygen from the ambient air is prevented from entering the burner 7, the pre-treatment silo 9 and the submerged electric arc furnace 5 so as to prevent uncontrolled reactions of said feed material 1.
• the manganese ore sinter 9 may have a particle size between 6 and 75 mm.
• the pre-treatment silo 8 of the apparatus may be configured to heat the feed mixture 1 to a temperature in the range between 400 and 700°C, preferable to a temperature in the range between 500 and 650°C.
• the apparatus comprises preferably, but not necessarily, gas temperature adjusting means (not shown in the figures) configured to adjust the temperature of said carbon dioxide containing carbonaceous gas 9 prior feeding said carbon dioxide containing carbonaceous gas 9 to the pre- treatment silo 8.
• gas temperature adjusting means (not shown in the figures) configured to adjust the temperature of said carbon dioxide containing carbonaceous gas 9 prior feeding said carbon dioxide containing carbonaceous gas 9 to the pre- treatment silo 8.
• the temperature of the feed carbon dioxide containing carbonaceous gas 9 that is fed to the pre-treatment silo 8 may be controlled to the range between 600 and 900°C.
• the carbon monoxide containing carbonaceous gas 6 received from the submerged electric arc furnace 5 is preferably burned by an air ratio below 1, such as between 0.9 and 0.95.
• Oxygen (0 2 ) content in the carbon dioxide containing carbonaceous gas 9 formed in the combusting step should be very low to minimize the oxidation of carbon in the feed mixture 1.
• the content of carbon monoxide (CO) and hydrogen (H 2 ) in the carbon dioxide containing carbonaceous gas 9 formed in the combusting step should be very low for avoiding the explosions in the gas lines or in the pre-treatment silo 8.
• the burner 7 may be a CO, a butane, and a LPG burner.
• Said carbon dioxide containing carbonaceous gas 9, that is produced by the burner 7 contains preferably, but not necessarily, in percentages of volume
• H 2 0 between 5 and 15 % H 2 0
• the arrangement preferably the burner 7, is preferably configured to feed said carbon dioxide containing carbonaceous gas 9 into the pre-treatment silo 8 from below so that said carbon dioxide containing carbonaceous gas 9 flows upwards in the pre-treatment silo 8 through the feed mixture.
• the apparatus may, as shown in figure 2, comprise a first scrubber 10 configured to scrub carbon monoxide containing carbonaceous gas 6 discharged from the electric arc furnace 5 prior combusting carbon monoxide to the burner 7.
• the apparatus may, as shown in figure 2, comprise second discharging means 15 configured to discharge carbon dioxide containing carbonaceous gas 9 from the pre-treatment silo 8 and third feeding means (not marked with a reference numeral) configured to feed carbon dioxide containing carbonaceous gas 9 discharged from the second discharging means 15 to the burner 7 and/or to into carbon dioxide containing carbonaceous gas 9 formed by the burner 7 to adjust the temperature of the carbon dioxide containing carbonaceous gas 9 formed by the burner 7.
• third feeding means not marked with a reference numeral
• the second discharging means 15 of the apparatus may, as shown in figure 2, comprise a second scrubber 11 configured to scrub carbon dioxide containing carbonaceous gas 9 discharged from the pre-treatment silo 8.
• Cold and scrubbed gases removed from the carbon dioxide containing carbonaceous gas 9 in the second scrubber 11 may be used in the optional temperature adjustment means for adjusting the temperature of the carbon dioxide containing carbonaceous gas 9 that is fed to the pre-treatment silo 8.
• the first feeding means 12 of the apparatus may be configured to feed reducing agent 3 containing carbonaceous material such as metallurgical coke, anthracite and/or charcoal.
• the first feeding means 12 of the apparatus may be configured to feed fluxing agent 4 containing at least one of calcite, coarse burned lime, dolomite and quartz.
• the first feeding means 12 of the apparatus may be configured to feed manganese ore sinter 2 containing in percentages of mass:
• the first feeding means 12 may, as shown in figure 2, comprise a silo arrangement 16 comprising a first silo 17 for manganese ore sinter 2, a second silo 18 for reducing agent 3, and a third silo 19 for fluxing agent 4.
• Metallurgical coke having the composition defined in table 1 and calcite manganese ore sinter having the composition defined in column "Original sinter" in table 2 was mixed in ratio 80 percentages by weight (wt.%) calcite ore and 20 wt.% and heated in a vessel to four different temperatures: 500°C, 600°C, 700°C and 800°C.
• the calcite manganese ore sinter was prior the mixing crushed and sieved into a particle size of 2.38 to 6.73 mm and the metallurgical coke was prior the mixing crushed and sieved into a particle size of 0.595 to 4.76 mm
• the heating was performed by induction heating and gas containing carbon dioxide and nitrogen in ratio 30% carbon dioxide and 70% was blown into the vessel to simulate actual heating conditions.
• the composition of the calcite manganese ore sinter was measured in each case: 500°C, 600°C, 700°C and 800°C. As can be seen from columns “500°C”,” 600°C", “700°C” and “800°C” table 3, the change in the composition of the calcite manganese ore sinter was only marginal, which means for example that hardly any reduction of the oxides occurred.
• Metallurgical coke having the composition defined in table 1 and oxidized manganese ore sinter having the composition defined in column "Original sinter" in table 3 was mixed in ratio 80 wt.% calcite ore and 20 wt.% charcoal and heated in a vessel to four different temperatures: 500°C, 600°C, 700°C and 800°C.
• the oxidized manganese ore sinter was prior the mixing crushed and sieved into a particle size of 2.38 to 6.73 mm and the metallurgical coke was prior the mixing crushed and sieved into a particle size of 0.595 to 4.76 mm.
• the heating was performed by induction heating and gas containing carbon dioxide and nitrogen in ratio 30% carbon dioxide and 70% was blown into the vessel to simulate actual heating conditions.
• the composition of the oxidized manganese ore sinter was measured in each case: 500°C, 600°C, 700°C and 800°C. As can be seen from columns “500°C”,” 600°C", “700°C” and “800°C” table 3, the change in the composition of the oxidized manganese ore sinter was only marginal, which means for example that hardly any reduction of the oxides occurred.
• manganese sinter as defined in table 4 was fed at a feed rate of 131 kg/h, and reducing agent as defined in row "charcoal" in table 5 was fed at a feed rate of 24 kg/h into the pre-treatment silo 8.
• Carbonaceous gas containing 57 vol-% N 2 , 30 vol.%, C0 2 and 11 vol.% H 2 0 and having a temperature of 850°C was fed at a feed rate of 970 m 3 /h into the pre-treatment silo 8.
• Carbon components of charcoal starts to gasify at 450°C.
• manganese sinter as defined table 4 was fed at a feed rate of 131 kg/h, and reducing agent as defined in row "Coke" in table 5 was fed at a feed rate of 24 kg/h into the pre-treatment silo 8.
• Carbonaceous gas containing 57 vol-% N 2 , 30 vol- %, C0 2 and 11 vol.% H 2 0 and having a temperature of 850°C was fed at a feed rate of 970 m 3 /h into the pre-treatment silo 8
• Carbon of coke starts to gasify at 700°C.

Landscapes

• Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Mechanical Engineering (AREA)
• Manufacturing & Machinery (AREA)
• Materials Engineering (AREA)
• Metallurgy (AREA)
• Organic Chemistry (AREA)
• General Life Sciences & Earth Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Ocean & Marine Engineering (AREA)
• Oceanography (AREA)
• Environmental & Geological Engineering (AREA)
• Geochemistry & Mineralogy (AREA)
• Geology (AREA)
• Physics & Mathematics (AREA)
• Plasma & Fusion (AREA)
• General Engineering & Computer Science (AREA)
• Manufacture And Refinement Of Metals (AREA)

Priority Applications (7)

Applications Claiming Priority (2)

Publications (1)

Family

ID=57590535

Family Applications (1)

Country Status (9)

Cited By (4)

Families Citing this family (2)

Citations (2)

Family Cites Families (7)

• 2015
  • 2015-11-24 FI FI20155868A patent/FI127451B/en active
• 2016
  • 2016-11-23 UA UAA201805936A patent/UA122912C2/uk unknown
  • 2016-11-23 BR BR112018010149-4A patent/BR112018010149B1/pt active IP Right Grant
  • 2016-11-23 CN CN202010360609.5A patent/CN111394578B/zh active Active
  • 2016-11-23 CN CN201680068082.0A patent/CN108291273A/zh active Pending
  • 2016-11-23 EP EP16816320.2A patent/EP3380638B1/en active Active
  • 2016-11-23 WO PCT/FI2016/050821 patent/WO2017089651A1/en active Application Filing
  • 2016-11-23 AU AU2016360842A patent/AU2016360842B2/en not_active Ceased
  • 2016-11-23 EA EA201891065A patent/EA033946B1/ru not_active IP Right Cessation
• 2018
  • 2018-05-30 ZA ZA2018/03599A patent/ZA201803599B/en unknown

Patent Citations (2)

Non-Patent Citations (1)

Also Published As

Similar Documents

Legal Events