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EP1188843B1 - Process and installation for supplying oxygen enriched air to a production unit of non-ferrous metals - Google Patents

Process and installation for supplying oxygen enriched air to a production unit of non-ferrous metals Download PDF

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Publication number
EP1188843B1
EP1188843B1 EP01402174A EP01402174A EP1188843B1 EP 1188843 B1 EP1188843 B1 EP 1188843B1 EP 01402174 A EP01402174 A EP 01402174A EP 01402174 A EP01402174 A EP 01402174A EP 1188843 B1 EP1188843 B1 EP 1188843B1
Authority
EP
European Patent Office
Prior art keywords
air
oxygen
converter
compressor
enriched
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.)
Expired - Lifetime
Application number
EP01402174A
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German (de)
French (fr)
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EP1188843A1 (en
Inventor
Didier Magnet
Norbert Rieth
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP1188843A1 publication Critical patent/EP1188843A1/en
Application granted granted Critical
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    • 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
    • C22B15/00—Obtaining copper
    • C22B15/0026—Pyrometallurgy
    • C22B15/0028—Smelting or converting
    • 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
    • C22B15/00—Obtaining copper
    • C22B15/0026—Pyrometallurgy
    • C22B15/0028—Smelting or converting
    • C22B15/003—Bath smelting or converting
    • C22B15/0041—Bath smelting or converting in converters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • F25J3/04515—Simultaneously changing air feed and products output
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04551—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the metal production
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F25J3/046—Completely integrated air feed compression, i.e. common MAC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the present invention relates to a method for supplying enriched air in oxygen from a non-ferrous metal production unit, comprising, share, an ore concentrate smelting unit of said metal supplied by continuous injection of oxygen-enriched air, on the other hand, a conversion unit mattes from the melting unit, fed by variable-rate injection of oxygen-enriched air, and to an installation for the implementation of this process.
  • the invention applies in particular to the production of copper.
  • Copper production units are conventionally made up of a continuous operation melter, such as a Flash oven, a Noranda oven or a Teniente oven, and a discontinuous conversion unit such as a Pierce converter or a Hoboken converter.
  • a continuous operation melter such as a Flash oven, a Noranda oven or a Teniente oven
  • a discontinuous conversion unit such as a Pierce converter or a Hoboken converter.
  • the raw material composed of copper ore concentrate, is charged in the melting unit, in which it is enriched with copper.
  • a mixture rich in copper called matte, containing about 60 to 70% in weight of copper.
  • This matte is then further enriched in copper in the unit of conversion and is transformed into copper known as "blister" containing approximately 99% of copper.
  • the bag When the bag is emptied, a slight flow of air is enriched with oxygen to maintain the flame of the burners of the conversion unit.
  • the rate oxygen enrichment of the air depends on the composition of the material first and expected production. Generally the air flow supplying the melting unit is enriched with up to 28% oxygen and the air flow feeding the unit conversion is enriched with 50 to 60% oxygen.
  • each unit has an air blower whose air flow is enriched by injecting oxygen produced by an installation independent of the two air blowers.
  • the consumption of oxygen-enriched air in the melting unit being constant, the air blower connected to the fuser constantly produces a air flow corresponding to the maximum flow of the copper production cycle.
  • the consumption of oxygen-enriched air in the conversion unit being variable, the difference between the air flow produced by the blower connected to the conversion unit, which operates continuously, and the one consumed by this unit conversion is generally vented.
  • the oxygen production installation consists of a compressor air and an air separation unit capable of delivering a variable flow oxygen, to enrich the blower air flow with a constant flow of oxygen of the melting unit, and enriching the unit's air flow with a variable oxygen flow conversion.
  • Compressor here means a compressor proper or several compressors mounted in parallel and having a common discharge.
  • This process for producing oxygen-enriched air by an installation comprising two independent air blowers connected to a oxygen production has various drawbacks such as congestion significant, significant energy consumption, as well as a loss significant energy due to the venting of air supplied by one of the blowers.
  • the invention therefore aims to provide a method and a supply system for oxygen-enriched air from a production unit non-ferrous metal, which involves a reduced bulk and which allows significantly reduce energy costs.
  • the invention essentially consists in combining the production of air and oxygen in order to produce more economically oxygen-enriched air to supply the melting unit and the conversion unit a non-ferrous metal production unit.
  • a copper production plant which includes a single air compressor 1 with three levels of compression (i.e. for example 4 or 5 stages) respectively supplying compressed air to a firstly a fusion unit 2 via a first pipe 3, secondly a air separation 4 via a second line 5, and finally, a conversion unit 6 or a buffer tank 7 via a third pipe 8.
  • the separation unit air 4 producing oxygen has two separate output circuits delivering oxygen at different pressures, one 9 supplying the melting unit 2, the other 10 supplying the conversion unit 6. Each circuit 9, 10 has a flow rate constant.
  • Buffer 7 is capable of storing compressed air as well as the oxygen of the second circuit 10 when the consumption of air enriched in oxygen in conversion unit 6 is low, i.e. below a threshold predetermined.
  • An expansion valve 11, constituted by a pressure regulator downstream, is placed on a line 12 which connects the conversion unit and the buffer capacity 7, so that the oxygen-enriched air flow circulates in the circuit 12 and either injected into the conversion unit 6, when the consumption of this unit 6 is high, that is to say greater than said threshold.
  • Figure 2 differs from the previous one in that the unit air separation unit 4 is here equipped with a so-called “toggle” system, described below, allowing to deliver a variable flow of oxygen to the conversion unit 6 while unit 4 processes a constant air flow.
  • the expansion valve 11 is placed between the capacity 7 and the point 13 of arrival of the oxygen produced by the circuit 10 on line 12 for supply of enriched air to the conversion unit 6.
  • Part of the air from one of the following compression levels (e.g. example, the second level of compression) of compressor 1 goes into the air separation unit 4.
  • This provides on the one hand a flow of oxygen 9 to a pressure from 1.2 to 1.7 bar supplying the fuser 2, and on the other hand a second oxygen flow 10 at a pressure of 5 to 10 bars intended for the conversion unit 6.
  • the rest 8 of the compressed air is extracted from the last stage of compressor 1 at a pressure of about 5 to 10 bars and is combined with the oxygen flow 10 above.
  • the air enriched thus obtained feeds either buffer capacity 7 when consumption in enriched air is low, i.e. the conversion unit 6 through the expansion valve 11 when the consumption of enriched air is high.
  • the air separation unit 4 provides a first flow of oxygen 9 at constant flow rate at a pressure of 1.2 to 1.7 bar, feeding the melting unit 2. It also provides a second flow of oxygen 10 to a pressure of approximately 1.5 bar which feeds the conversion unit 6, a rocker being provided to supply oxygen at a variable rate depending on the consumption of enriched air from the conversion unit 6.
  • the rest 8 of the compressed air is extracted from the last stage of the compressor at a pressure of around 5 to 10 bars.
  • this air is partially stored in the buffer capacity 7.
  • an air flow equal to the difference between the enriched air flow required by the conversion unit 6 and the oxygen flow 10 through the expansion valve.
  • the air produced by the air compressor and feeding the air separation unit and the capacity 7 is at a pressure corresponding to an economic optimum and energy between the energy spent on air compression and the cost corresponding to the investment of the buffer capacity allowing the supply discontinuous in enriched air from the conversion unit.
  • the air pressure produced by the air compressor to supply the air separation unit is preferably 5 to 6 bar, and the air pressure produced by the air compressor to supply the gas capacity is preferably from 5 to 10 bars.
  • the double column 23 is of the minaret type and has a medium pressure column 26 surmounted by a low pressure column 27, this extending upwards by a short distillation section or minaret 28 of smaller diameter.
  • a vaporizer-condenser main 29 puts the overhead vapor (approximately pure nitrogen) from the column 26 in indirect heat exchange relationship with the tank liquid (liquid oxygen) from column 27.
  • the double column 23 produces at constant flow rates of liquid oxygen 31 in the tank of the column 27, low pressure nitrogen gas 32 at the head of minaret 28, and medium pressure liquid nitrogen 33 at the head of medium pressure column 26.
  • the liquid oxygen withdrawn from the low pressure column is stored in the buffer capacity 21 and, from there, is compressed to the pressure of circuit 10 by the pump 20, then sprayed against the current with a constant flow of air overpressed in 16.
  • the air thus liquefied is, after expansion at medium pressure in an expansion valve 34, stored in the buffer capacity 22 before being partly introduced in the liquid state in the lower part of column 26 and, for the rest, relaxed at low pressure in an expansion valve 35 and introduced at an intermediate level of column 27.
  • Unit 4 also produces a constant flow of gaseous oxygen for the circuit 9, for example from another oxygen withdrawal line 36 liquid from column 27, then vaporization / reheating at 15 and possibly compression of the resulting gaseous oxygen.
  • Unit 4 still produces a low pressure nitrogen gas flow from minaret 28 and heated in 24 then in 15, as well as a high nitrogen gas flow pressure obtained by pumping medium pressure liquid nitrogen at 25 then by vaporization / reheating in 15. These two nitrogen streams serve for inerting and / or conveying in the copper production facility.
  • the turbo-compressor group 18.19 operating by overpressure and expansion of part of the incoming air, used to keep the unit cool 4.
  • An air separation unit like the one in Figure 3 provides a rate of variation of the oxygen flow produced at 10 which is typically of around 5% per minute.
  • the invention can also be applied to the production of metals non-ferrous other than copper, such as nickel.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Emergency Medicine (AREA)
  • Health & Medical Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)

Description

La présente invention est relative à un procédé d'alimentation en air enrichi en oxygène d'une unité de production de métal non ferreux, comprenant, d'une part, une unité de fusion de concentré de minerai dudit métal alimentée par injection continue d'air enrichi en oxygène, d'autre part, une unité de conversion des mattes issues de l'unité de fusion, alimentée par injection à débit variable d'air enrichi en oxygène, et à une installation pour la mise en oeuvre de ce procédé. L'invention s'applique en particulier à la production de cuivre.The present invention relates to a method for supplying enriched air in oxygen from a non-ferrous metal production unit, comprising, share, an ore concentrate smelting unit of said metal supplied by continuous injection of oxygen-enriched air, on the other hand, a conversion unit mattes from the melting unit, fed by variable-rate injection of oxygen-enriched air, and to an installation for the implementation of this process. The invention applies in particular to the production of copper.

Les pressions dont il est question ci-dessous sont des pressions absolues.The pressures discussed below are absolute pressures.

Les unités de production de cuivre sont classiquement constituées d'une unité de fusion à fonctionnement continu, telle qu'un four Flash, un four Noranda ou un four Teniente, et d'une unité de conversion à fonctionnement discontinu telle qu'un convertisseur Pierce ou un convertisseur Hoboken.Copper production units are conventionally made up of a continuous operation melter, such as a Flash oven, a Noranda oven or a Teniente oven, and a discontinuous conversion unit such as a Pierce converter or a Hoboken converter.

La matière première, composée de concentré de minerai de cuivre, est chargée dans l'unité de fusion, dans laquelle elle s'enrichit en cuivre. On obtient alors une mixture riche en cuivre appelée matte, contenant environ 60 à 70% en poids de cuivre. Cette matte est ensuite encore enrichie en cuivre dans l'unité de conversion et est transformée en cuivre dit " blister " contenant environ 99% de cuivre.The raw material, composed of copper ore concentrate, is charged in the melting unit, in which it is enriched with copper. We obtain then a mixture rich in copper called matte, containing about 60 to 70% in weight of copper. This matte is then further enriched in copper in the unit of conversion and is transformed into copper known as "blister" containing approximately 99% of copper.

Afin que la fusion et la conversion s'effectuent dans de bonnes conditions, les deux unités sont alimentées par des flux d'air enrichi en oxygène. L'unité de fusion consomme un flux constant d'air enrichi en oxygène. En revanche, l'unité de conversion consomme un flux variable d'air enrichi en oxygène. Ce flux peut d'ailleurs être proche de zéro au moment où, la transformation en cuivre blister étant terminée, on vide la poche de l'unité de conversion pour récupérer le cuivre blister et pouvoir ainsi commencer un nouveau cycle de production de cuivre. Typiquement, un cycle de production de cuivre dure environ deux heures réparties comme suit :

  • on injecte de l'air enrichi en oxygène dans l'unité de conversion pendant environ une heure ;
  • on stoppe l'injection, on retire le laitier surnageant à la surface du cuivre liquide, on vide la poche pour récupérer le cuivre, à la suite de quoi on recharge de mattes la poche et on recommence un nouveau cycle.
In order for the fusion and conversion to take place in good conditions, the two units are supplied with air flows enriched with oxygen. The fuser consumes a constant flow of oxygen-enriched air. On the other hand, the conversion unit consumes a variable flow of air enriched with oxygen. This flow can moreover be close to zero at the moment when, the transformation into copper blister being completed, the pocket of the conversion unit is emptied to recover the copper blister and thus be able to start a new cycle of copper production. Typically, a copper production cycle lasts about two hours divided as follows:
  • oxygen-enriched air is injected into the conversion unit for approximately one hour;
  • the injection is stopped, the supernatant slag is removed from the surface of the liquid copper, the bag is emptied to recover the copper, after which the bag is refilled with mattes and a new cycle is started again.

Lorsque l'on vide la poche, on maintient un léger flux d'air enrichi en oxygène pour maintenir la flamme des brûleurs de l'unité de conversion. Le taux d'enrichissement en oxygène de l'air dépend de la composition de la matière première et de la production attendue. Généralement le flux d'air alimentant l'unité de fusion est enrichi jusqu'à 28% d'oxygène et le flux d'air alimentant l'unité de conversion est enrichi à 50 à 60% d'oxygène.When the bag is emptied, a slight flow of air is enriched with oxygen to maintain the flame of the burners of the conversion unit. The rate oxygen enrichment of the air depends on the composition of the material first and expected production. Generally the air flow supplying the melting unit is enriched with up to 28% oxygen and the air flow feeding the unit conversion is enriched with 50 to 60% oxygen.

Conventionnellement, chaque unité possède une soufflante d'air dont le flux d'air est enrichi par injection d'oxygène produit par une installation indépendante des deux soufflantes d'air.Conventionally, each unit has an air blower whose air flow is enriched by injecting oxygen produced by an installation independent of the two air blowers.

La consommation en air enrichi en oxygène de l'unité de fusion étant constante, la soufflante d'air reliée à l'unité de fusion produit en permanence un débit d'air correspondant au débit maximal du cycle d'élaboration du cuivre. En revanche, la consommation en air enrichi en oxygène de l'unité de conversion étant variable, la différence entre le débit d'air produit par la soufflante reliée à l'unité de conversion, qui fonctionne en continu, et celui consommé par cette unité de conversion est généralement mise à l'air.The consumption of oxygen-enriched air in the melting unit being constant, the air blower connected to the fuser constantly produces a air flow corresponding to the maximum flow of the copper production cycle. In however, the consumption of oxygen-enriched air in the conversion unit being variable, the difference between the air flow produced by the blower connected to the conversion unit, which operates continuously, and the one consumed by this unit conversion is generally vented.

L'installation de production d'oxygène est constituée d'un compresseur d'air et d'une unité de séparation d'air capable de délivrer un débit variable d'oxygène, afin d'enrichir d'un flux d'oxygène constant le flux d'air de la soufflante de l'unité de fusion, et d'enrichir d'un flux d'oxygène variable le flux d'air de l'unité de conversion.The oxygen production installation consists of a compressor air and an air separation unit capable of delivering a variable flow oxygen, to enrich the blower air flow with a constant flow of oxygen of the melting unit, and enriching the unit's air flow with a variable oxygen flow conversion.

On entend ici par " compresseur " un compresseur proprement dit ou plusieurs compresseurs montés en parallèle et ayant un refoulement commun."Compressor" here means a compressor proper or several compressors mounted in parallel and having a common discharge.

Ce procédé de production d'air enrichi en oxygène par une installation comprenant deux soufflantes d'air indépendantes reliées à une unité de production d'oxygène présente divers inconvénients comme un encombrement important, une consommation énergétique importante, ainsi qu'une perte d'énergie non négligeable due à la mise à l'air de l'air délivré par l'une des soufflantes.This process for producing oxygen-enriched air by an installation comprising two independent air blowers connected to a oxygen production has various drawbacks such as congestion significant, significant energy consumption, as well as a loss significant energy due to the venting of air supplied by one of the blowers.

L'invention a donc pour but de proposer un procédé ainsi qu'une installation d'alimentation d'air enrichi en oxygène d'une unité de production de métal non ferreux, qui implique un encombrement réduit et qui permette de réduire sensiblement les dépenses énergétiques.The invention therefore aims to provide a method and a supply system for oxygen-enriched air from a production unit non-ferrous metal, which involves a reduced bulk and which allows significantly reduce energy costs.

L'invention a donc pour objet un procédé d'alimentation en air enrichi en oxygène d'une unité de production de métal non ferreux, comprenant, d'une part, une unité de fusion de concentré dudit métal alimenté par injection continue d'air enrichi en oxygène, d'autre part, une unité de conversion des mattes issues de l'unité de fusion, alimentée par injection à débit variable d'air enrichi en oxygène, caractérisé en ce que :

  • l'on comprime la totalité de l'air dans un compresseur unique susceptible d'alimenter l'unité de fusion et l'unité de conversion ;
  • l'on traite une partie de cet air comprimé dans une unité de séparation d'air pour obtenir deux flux d'oxygène qu'on injecte respectivement dans l'air comprimé destiné à alimenter l'unité de fusion et dans l'air comprimé destiné à alimenter l'unité de conversion ;et
  • l'on stocke de l'air comprimé ou de l'air comprimé enrichi en oxygène destiné à l'unité de conversion dans une capacité-tampon lorsque la consommation en air enrichi en oxygène de l'unité de conversion est inférieure à un seuil déterminé, et l'on prélève de l'air comprimé ou de l'air comprimé enrichi en oxygène dans la capacité-tampon lorsque la consommation en air enrichi en oxygène de l'unité de conversion est supérieure audit seuil ;
The subject of the invention is therefore a method for supplying air enriched with oxygen to a non-ferrous metal production unit, comprising, on the one hand, a unit for melting concentrate of said metal supplied by continuous injection of air enriched in oxygen, on the other hand, a matte conversion unit from the melting unit, supplied by injection at variable flow rate of oxygen-enriched air, characterized in that:
  • all the air is compressed in a single compressor capable of supplying the melting unit and the conversion unit;
  • part of this compressed air is treated in an air separation unit to obtain two oxygen flows which are injected respectively into the compressed air intended to supply the melting unit and into the compressed air intended supplying the conversion unit; and
  • compressed air or oxygen-enriched compressed air intended for the conversion unit is stored in a buffer capacity when the consumption of oxygen-enriched air from the conversion unit is less than a determined threshold , and compressed air or oxygen-enriched compressed air is taken from the buffer capacity when the consumption of oxygen-enriched air from the conversion unit is greater than said threshold;

Selon d'autres caractéristiques de ce procédé :

  • on alimente l'unité de fusion en mélangeant de l'air comprimé par le premier niveau de compression du compresseur avec de l'oxygène produit par l'unité de séparation d'air sensiblement à la même pression ;
  • on alimente l'unité de séparation d'air avec de l'air comprimé par un niveau de compression du compresseur situé derrière le premier niveau de compression de ce compresseur ;
  • on alimente l'unité de conversion en mélangeant de l'air comprimé par le compresseur à une pression supérieure à la pression d'alimentation de cette unité de conversion avec de l'oxygène produit par l'unité de séparation d'air sensiblement à la même pression, en stockant l'air enrichi en oxygène dans ladite capacité-tampon lorsque la consommation en air enrichi en oxygène par l'unité de conversion est inférieure audit seuil, et en prélevant de l'air enrichi en oxygène dans cette capacité-tampon à travers un organe de détente lorsque la consommation en air enrichi en oxygène par l'unité de conversion est supérieure audit seuil.
  • on stocke de l'air comprimé par le dernier étage du compresseur à une pression supérieure à la pression d'alimentation de l'unité de conversion dans ladite capacité-tampon lorsque la consommation en air enrichi en oxygène par cette unité de conversion est inférieure audit seuil, et on alimente l'unité de conversion en mélangeant de l'air stocké dans la capacité-tampon et/ou de l'air comprimé par le dernier étage du compresseur, prélevés à travers un organe de détente, avec de l'oxygène produit par l'unité de séparation d'air à un débit variable et à une pression sensiblement égale à la pression d'alimentation de l'unité de conversion ;
  • l'air destiné à l'unité de conversion est comprimé par le dernier étage du compresseur.
According to other characteristics of this process:
  • the melting unit is supplied by mixing air compressed by the first level of compression of the compressor with oxygen produced by the air separation unit at substantially the same pressure;
  • the air separation unit is supplied with compressed air by a level of compression of the compressor situated behind the first level of compression of this compressor;
  • the conversion unit is supplied by mixing compressed air from the compressor at a pressure higher than the supply pressure of this conversion unit with oxygen produced by the air separation unit substantially at the same pressure, by storing the oxygen-enriched air in said buffer capacity when the consumption of oxygen-enriched air by the conversion unit is less than said threshold, and by taking oxygen-enriched air in this buffer capacity through an expansion device when the consumption of air enriched with oxygen by the conversion unit is greater than said threshold.
  • compressed air is stored by the last stage of the compressor at a pressure higher than the supply pressure of the conversion unit in said buffer capacity when the consumption of air enriched with oxygen by this conversion unit is lower than said threshold, and the conversion unit is supplied by mixing air stored in the buffer capacity and / or compressed air by the last stage of the compressor, taken through an expansion device, with oxygen produced by the air separation unit at a variable flow rate and at a pressure substantially equal to the supply pressure of the conversion unit;
  • the air intended for the conversion unit is compressed by the last stage of the compressor.

L'invention a également pour objet une installation pour la mise en oeuvre du procédé défini ci-dessus. Cette installation est caractérisée en ce qu'elle comprend :

  • une unité de séparation d'air adaptée pour fournir de l'oxygène aux unités de fusion et de conversion ;
  • un compresseur d'air unique dont le refoulement est relié à l'unité de fusion, à l'unité de séparation d'air et à l'unité de conversion par des première, deuxième et troisième conduite respectivement ; et
  • une capacité-tampon reliée à ladite troisième conduite.
The invention also relates to an installation for implementing the method defined above. This installation is characterized in that it includes:
  • an air separation unit adapted to supply oxygen to the melting and conversion units;
  • a single air compressor, the discharge of which is connected to the melting unit, the air separation unit and the conversion unit by first, second and third lines respectively; and
  • a buffer capacity connected to said third pipe.

Selon d'autres caractéristiques de cette installation :

  • la capacité-tampon est également reliée d'une part à une sortie d'oxygène de l'unité de séparation destinée à l'unité de conversion et d'autre part à cette unité de conversion à travers un organe de détente. La capacité tampon est également reliée à l'unité de conversion à travers un organe de détente et une sortie d'oxygène de l'unité de séparation destinée à l'unité de conversion débouche dans la conduite qui relie cet organe de détente à l'unité de conversion ;
  • l'unité de séparation d'air comporte deux circuits de production d'oxygène, l'un alimentant l'unité de fusion, l'autre l'unité de conversion ;
  • le circuit de production d'oxygène alimentant l'unité de conversion est muni de moyens de réglage du débit d'oxygène ;
  • l'unité de séparation d'air comprimé est une unité de distillation d'air à double colonne qui comporte un système à bascule afin de produire un flux d'oxygène variable par distillation d'un débit d'air constant ;
  • le compresseur d'air comprend au moins deux niveaux de compression, le refoulement du premier niveau étant relié à ladite première conduite et celui du ou des niveaux suivants étant reliés auxdites deuxième et troisième conduite ;
  • le compresseur comporte trois niveaux de compression dont les refoulements sont reliés respectivement auxdites première, deuxième et troisième conduites.
According to other characteristics of this installation:
  • the buffer capacity is also connected on the one hand to an oxygen outlet of the separation unit intended for the conversion unit and on the other hand to this conversion unit through an expansion member. The buffer capacity is also connected to the conversion unit through an expansion member and an oxygen outlet from the separation unit intended for the conversion unit opens into the pipe which connects this expansion member to the conversion unit;
  • the air separation unit comprises two oxygen production circuits, one supplying the melting unit, the other the conversion unit;
  • the oxygen production circuit supplying the conversion unit is provided with means for adjusting the oxygen flow rate;
  • the compressed air separation unit is a double column air distillation unit which includes a rocking system in order to produce a variable oxygen flow by distillation of a constant air flow;
  • the air compressor comprises at least two compression levels, the discharge of the first level being connected to said first pipe and that of the following level or levels being connected to said second and third pipe;
  • the compressor has three compression levels, the outlets of which are connected to said first, second and third pipes respectively.

Comme on l'aura compris, l'invention consiste essentiellement à combiner la production d'air et d'oxygène afin de produire de manière plus économique de l'air enrichi en oxygène pour alimenter l'unité de fusion et l'unité de conversion d'une unité de production de métal non ferreux.As will be understood, the invention essentially consists in combining the production of air and oxygen in order to produce more economically oxygen-enriched air to supply the melting unit and the conversion unit a non-ferrous metal production unit.

Des exemples de mise en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés sur lesquels :

  • la Figure 1 représente schématiquement une installation de production d'air enrichi en oxygène alimentant une unité de fusion et une unité de conversion de cuivre ; et
  • la Figure 2 représente une alternative de l'installation de la Figure 1 ; et
  • la Figure 3 représente une unité de séparation d'air destinée à l'installation de la Figure 2.
Examples of implementation of the invention will now be described with reference to the accompanying drawings in which:
  • FIG. 1 schematically represents an installation for producing oxygen-enriched air supplying a melting unit and a copper conversion unit; and
  • Figure 2 shows an alternative to the installation of Figure 1; and
  • Figure 3 shows an air separation unit for the installation of Figure 2.

Sur la Figure 1, on a représenté une installation de production de cuivre qui comprend un compresseur d'air unique 1 à trois niveaux de compressions (soit par exemple 4 ou 5 étages) alimentant respectivement en air comprimé d'une part une unité de fusion 2 via une première conduite 3, d'autre part une unité de séparation d'air 4 via une deuxième conduite 5, et enfin, une unité de conversion 6 ou une capacité-tampon 7 via une troisième conduite 8. L'unité de séparation d'air 4 produisant l'oxygène possède deux circuits de sortie distincts délivrant de l'oxygène à des pressions différentes, l'une 9 alimentant l'unité de fusion 2 , l'autre 10 alimentant l'unité de conversion 6. Chaque circuit 9, 10 est à débit constant.In Figure 1, a copper production plant is shown which includes a single air compressor 1 with three levels of compression (i.e. for example 4 or 5 stages) respectively supplying compressed air to a firstly a fusion unit 2 via a first pipe 3, secondly a air separation 4 via a second line 5, and finally, a conversion unit 6 or a buffer tank 7 via a third pipe 8. The separation unit air 4 producing oxygen has two separate output circuits delivering oxygen at different pressures, one 9 supplying the melting unit 2, the other 10 supplying the conversion unit 6. Each circuit 9, 10 has a flow rate constant.

La capacité-tampon 7 est capable de stocker l'air comprimé ainsi que l'oxygène du deuxième circuit 10 lorsque la consommation en air enrichi en oxygène de l'unité de conversion 6 est faible, c'est-à-dire inférieure à un seuil prédéterminé. Une vanne de détente 11, constituée par un régulateur de pression aval, est placée sur une conduite 12 qui relie l'unité de conversion et la capacité-tampon 7, pour que le flux d'air enrichi en oxygène circule dans le circuit 12 et soit injecté dans l'unité de conversion 6, lorsque la consommation de cette unité 6 est élevée, c'est-à-dire supérieure audit seuil.Buffer 7 is capable of storing compressed air as well as the oxygen of the second circuit 10 when the consumption of air enriched in oxygen in conversion unit 6 is low, i.e. below a threshold predetermined. An expansion valve 11, constituted by a pressure regulator downstream, is placed on a line 12 which connects the conversion unit and the buffer capacity 7, so that the oxygen-enriched air flow circulates in the circuit 12 and either injected into the conversion unit 6, when the consumption of this unit 6 is high, that is to say greater than said threshold.

L'installation de la Figure 2 diffère de la précédente par le fait que l'unité de séparation d'air 4 est ici équipée d'un système dit " à bascule ", décrit plus loin, permettant de délivrer un débit variable d'oxygène vers l'unité de conversion 6 alors que l'unité 4 traite un débit d'air constant. De plus, la vanne de détente 11 est disposée entre la capacité 7 et le point 13 d'arrivée de l'oxygène produit par le circuit 10 sur la conduite 12 d'alimentation en air enrichi de l'unité de conversion 6.The installation of Figure 2 differs from the previous one in that the unit air separation unit 4 is here equipped with a so-called "toggle" system, described below, allowing to deliver a variable flow of oxygen to the conversion unit 6 while unit 4 processes a constant air flow. In addition, the expansion valve 11 is placed between the capacity 7 and the point 13 of arrival of the oxygen produced by the circuit 10 on line 12 for supply of enriched air to the conversion unit 6.

En fonctionnement, dans le cas de la Figure 1, la totalité de l'air nécessaire au fonctionnement de l'unité de production du cuivre est comprimée dans le compresseur 1.In operation, in the case of Figure 1, all of the air required during operation of the copper production unit is compressed in the compressor 1.

Une partie de cet air, extraite du refoulement du premier niveau de compression du compresseur 1, à une pression constante comprise entre 1,2 et 1,7 bar, est injectée à débit constant dans l'unité de fusion 2 après avoir été enrichie par un flux d'oxygène 9, à une pression sensiblement égale à celle du flux d'air, produit à débit constant par l'unité de séparation d'air 4.Part of this air, extracted from the discharge of the first level of compression of compressor 1, at a constant pressure between 1.2 and 1.7 bar, is injected at constant flow rate into the melter 2 after being enriched by a flow of oxygen 9, at a pressure substantially equal to that of the air flow, produced at constant flow by the air separation unit 4.

Une partie de l'air issu d'un des niveaux de compression suivants (par exemple, le deuxième niveau de compression) du compresseur 1 passe dans l'unité de séparation d'air 4. Celle-ci fournit d'une part un flux d'oxygène 9 à une pression de 1,2 à 1,7 bar alimentant l'unité de fusion 2, et d'autre part un second flux d'oxygène 10 à une pression de 5 à 10 bars destiné à l'unité de conversion 6. Le reste 8 de l'air comprimé est extrait du dernier étage du compresseur 1 à une pression d'environ 5 à 10 bars et est réuni au flux d'oxygène 10 précité. L'air enrichi ainsi obtenu alimente soit la capacité-tampon 7 lorsque la consommation en air enrichi est faible, soit l'unité de conversion 6 à travers la vanne de détente 11 lorsque la consommation en air enrichi est élevée.Part of the air from one of the following compression levels (e.g. example, the second level of compression) of compressor 1 goes into the air separation unit 4. This provides on the one hand a flow of oxygen 9 to a pressure from 1.2 to 1.7 bar supplying the fuser 2, and on the other hand a second oxygen flow 10 at a pressure of 5 to 10 bars intended for the conversion unit 6. The rest 8 of the compressed air is extracted from the last stage of compressor 1 at a pressure of about 5 to 10 bars and is combined with the oxygen flow 10 above. The air enriched thus obtained feeds either buffer capacity 7 when consumption in enriched air is low, i.e. the conversion unit 6 through the expansion valve 11 when the consumption of enriched air is high.

Selon la variante de la Figure 2, l'unité de séparation d'air 4 fournit un premier flux d'oxygène 9 à débit constant à une pression de 1,2 à 1,7 bar, alimentant l'unité de fusion 2. Elle fournit aussi un deuxième flux d'oxygène 10 à une pression d'environ 1,5 bar qui alimente l'unité de conversion 6, une bascule étant prévue afin de fournir l'oxygène à un débit variable en fonction de la consommation en air enrichi de l'unité de conversion 6.According to the variant of Figure 2, the air separation unit 4 provides a first flow of oxygen 9 at constant flow rate at a pressure of 1.2 to 1.7 bar, feeding the melting unit 2. It also provides a second flow of oxygen 10 to a pressure of approximately 1.5 bar which feeds the conversion unit 6, a rocker being provided to supply oxygen at a variable rate depending on the consumption of enriched air from the conversion unit 6.

Le reste 8 de l'air comprimé est extrait du dernier étage du compresseur à une pression d'environ 5 à 10 bars. Lorsque la consommation en air enrichi en oxygène de l'unité de conversion 6 est faible, cet air est partiellement stocké dans la capacité-tampon 7. A chaque instant, un débit d'air égal à la différence entre le débit d'air enrichi demandé par l'unité de conversion 6 et le débit d'oxygène 10 traverse la vanne de détente.The rest 8 of the compressed air is extracted from the last stage of the compressor at a pressure of around 5 to 10 bars. When the consumption of enriched air in oxygen from conversion unit 6 is low, this air is partially stored in the buffer capacity 7. At each instant, an air flow equal to the difference between the enriched air flow required by the conversion unit 6 and the oxygen flow 10 through the expansion valve.

Afin de satisfaire aux critères d'économie évoqués précédemment, l'air produit par le compresseur d'air et alimentant l'unité de séparation d'air et la capacité 7 est à une pression correspondant à un optimum économique et énergétique entre l'énergie dépensée pour la compression de l'air et le coût correspondant à l'investissement de la capacité-tampon permettant l'alimentation discontinue en air enrichi de l'unité de conversion.In order to meet the saving criteria mentioned above, the air produced by the air compressor and feeding the air separation unit and the capacity 7 is at a pressure corresponding to an economic optimum and energy between the energy spent on air compression and the cost corresponding to the investment of the buffer capacity allowing the supply discontinuous in enriched air from the conversion unit.

Ainsi, la pression de l'air produit par le compresseur d'air pour alimenter l'unité de séparation d'air est de préférence de 5 à 6 bars, et la pression de l'air produit par le compresseur d'air pour alimenter la capacité gazeuse est de préférence de 5 à 10 bars.So the air pressure produced by the air compressor to supply the air separation unit is preferably 5 to 6 bar, and the air pressure produced by the air compressor to supply the gas capacity is preferably from 5 to 10 bars.

L'unité de séparation d'air 4 représentée sur la Figure 3, du type classique dit " à bascule", est destinée à fournir un débit variable d'oxygène à la conduite 10 de la Figure 2. Elle comprend essentiellement le compresseur d'air 1 à trois niveaux de compression, un appareil 14 de dessication - décarbonatation d'air par adsorption, une ligne d'échange thermique principale 15, un surpresseur d'air 16, un échangeur de chaleur auxiliaire 17, un groupe turbo-compresseur comprenant une turbine 18 couplée à un compresseur 19, une pompe d'oxygène liquide 20 à débit variable, une capacité-tampon d'oxygène liquide 21, une capacité-tampon d'air liquide 22, une double colonne de distillation d'air 23, un sous-refroidisseur 24 et une pompe d'azote liquide 25. La double colonne 23 est du type à minaret et comporte une colonne moyenne pression 26 surmontée d'une colonne basse pression 27, celle-ci se prolongeant vers le haut par un court tronçon de distillation ou minaret 28 de plus petit diamètre. Un vaporiseur-condenseur principal 29 met la vapeur de tête (azote à peu près pur) de la colonne 26 en relation d'échange thermique indirect avec le liquide de cuve (oxygène liquide) de la colonne 27.The air separation unit 4 shown in Figure 3, of the conventional type says "rocker", is intended to provide a variable flow of oxygen to the pipe 10 of Figure 2. It essentially comprises the air compressor 1 to three compression levels, a desiccation device 14 - decarbonation of air by adsorption, a main heat exchange line 15, an air blower 16, an auxiliary heat exchanger 17, a turbo-compressor unit comprising a turbine 18 coupled to a compressor 19, a liquid oxygen pump 20 variable flow, liquid oxygen buffer capacity 21, buffer capacity liquid air 22, a double air distillation column 23, a sub-cooler 24 and a liquid nitrogen pump 25. The double column 23 is of the minaret type and has a medium pressure column 26 surmounted by a low pressure column 27, this extending upwards by a short distillation section or minaret 28 of smaller diameter. A vaporizer-condenser main 29 puts the overhead vapor (approximately pure nitrogen) from the column 26 in indirect heat exchange relationship with the tank liquid (liquid oxygen) from column 27.

En fonctionnement, un débit constant d'air issu du second niveau de compression du compresseur 1, ramené au voisinage de la température ambiante en 30 et épuré en 14, puis est refroidi jusqu'au voisinage de son point de rosée en 15, est injecté en cuve de la colonne 26.In operation, a constant flow of air from the second level of compression of compressor 1, brought close to ambient temperature in 30 and refined in 14, then is cooled to the vicinity of its dew point at 15, is injected into the tank of column 26.

Suivant le procédé de distillation à double colonne classique, la double colonne 23 produit à débits constants de l'oxygène liquide 31 en cuve de la colonne 27, de l'azote gazeux basse pression 32 en tête du minaret 28, et de l'azote liquide moyenne pression 33 en tête de la colonne moyenne pression 26.Following the conventional double column distillation process, the double column 23 produces at constant flow rates of liquid oxygen 31 in the tank of the column 27, low pressure nitrogen gas 32 at the head of minaret 28, and medium pressure liquid nitrogen 33 at the head of medium pressure column 26.

L'oxygène liquide soutiré de la colonne basse pression est stocké dans la capacité-tampon 21 et, de là, est comprimé à la pression du circuit 10 par la pompe 20, puis vaporisé à contre-courant d'un flux d'air à débit constant surpressé en 16. L'air ainsi liquéfié est, après détente à la moyenne pression dans une vanne de détente 34, stocké dans la capacité-tampon 22 avant d'être pour partie introduit à l'état liquide dans la partie inférieure de la colonne 26 et, pour le reste, détendu à la basse pression dans une vanne de détente 35 et introduit à un niveau intermédiaire de la colonne 27.The liquid oxygen withdrawn from the low pressure column is stored in the buffer capacity 21 and, from there, is compressed to the pressure of circuit 10 by the pump 20, then sprayed against the current with a constant flow of air overpressed in 16. The air thus liquefied is, after expansion at medium pressure in an expansion valve 34, stored in the buffer capacity 22 before being partly introduced in the liquid state in the lower part of column 26 and, for the rest, relaxed at low pressure in an expansion valve 35 and introduced at an intermediate level of column 27.

De façon classique, lorsque le débit d'oxygène gazeux nécessaire dans le circuit 10 est inférieur à 21% du débit d'air distillé, la pompe 20 est ralentie de façon correspondante, et le niveau d'oxygène liquide monte dans la capacité 21. Simultanément, un débit moindre d'air étant liquéfié, le niveau de l'air liquide descend dans la capacité 22. Les phénomènes s'inversent en cas d'augmentation du débit d'oxygène en 10 au delà de 21% du débit d'air distillé.Conventionally, when the flow of gaseous oxygen required in the circuit 10 is less than 21% of the distilled air flow, the pump 20 is slowed down by correspondingly, and the level of liquid oxygen rises in capacity 21. At the same time, a lower flow of air being liquefied, the level of liquid air drops in capacity 22. The phenomena are reversed in the event of an increase of the oxygen flow in 10 beyond 21% of the distilled air flow.

L'unité 4 produit par ailleurs un débit constant d'oxygène gazeux pour le circuit 9, par exemple à partir d'une autre conduite 36 de soutirage d'oxygène liquide de la colonne 27, puis vaporisation/réchauffage en 15 et éventuellement compression de l'oxygène gazeux résultant. Unit 4 also produces a constant flow of gaseous oxygen for the circuit 9, for example from another oxygen withdrawal line 36 liquid from column 27, then vaporization / reheating at 15 and possibly compression of the resulting gaseous oxygen.

L'unité 4 produit encore un flux d'azote gazeux basse pression provenant du minaret 28 et réchauffé en 24 puis en 15, ainsi qu'un flux d'azote gazeux haute pression obtenu par pompage d'azote liquide moyenne pression en 25 puis par vaporisation/réchauffage en 15. Ces deux flux d'azote servent à l'inertage et/ou au convoyage dans l'installation de production de cuivre.Unit 4 still produces a low pressure nitrogen gas flow from minaret 28 and heated in 24 then in 15, as well as a high nitrogen gas flow pressure obtained by pumping medium pressure liquid nitrogen at 25 then by vaporization / reheating in 15. These two nitrogen streams serve for inerting and / or conveying in the copper production facility.

Le groupe turbo-compresseur 18,19, fonctionnant par surpression et détente d'une partie de l'air entrant, sert au maintien en froid de l'unité 4.The turbo-compressor group 18.19, operating by overpressure and expansion of part of the incoming air, used to keep the unit cool 4.

Une unité de séparation d'air telle que celle de la Figure 3 permet d'obtenir une vitesse de variation du débit d'oxygène produit en 10 qui est typiquement de l'ordre de 5% par minute.An air separation unit like the one in Figure 3 provides a rate of variation of the oxygen flow produced at 10 which is typically of around 5% per minute.

L'invention peut s'appliquer également à la production de métaux non ferreux autres que le cuivre, tels que le nickel.The invention can also be applied to the production of metals non-ferrous other than copper, such as nickel.

Claims (14)

  1. Process for feeding oxygen-enriched air into a non-ferrous metal production unit comprising, on the one hand, a smelter (2) for smelting the ore concentrate of the said metal, fed by continuously injecting oxygen-enriched air and, on the other hand, a converter (6) for converting the matte coming from the smelter, fed by injecting oxygen-enriched air with a variable flow rate, characterized in that:
    all of the air is compressed in a single compressor (1) capable of feeding the smelter (2) and the converter (6);
    some of this compressed air is treated in an air separation unit (4) in order to obtain two oxygen streams (9, 10) which are injected into the compressed air intended for feeding the smelter (2) and the converter (6), respectively; and
    the compressed air or oxygen-enriched compressed air intended for the converter (6) is stored in a buffer tank (7) when the consumption of oxygen-enriched air by the converter is below a predetermined threshold and compressed air or oxygen-enriched compressed air is removed from the buffer tank (7) when the consumption of oxygen-enriched air by the converter (6) is above the said threshold.
  2. Process according to Claim 1, characterized in that the smelter (2) is fed by mixing air compressed by the first compression level of the compressor (1) with oxygen produced by the air separation unit (4) substantially at the same pressure.
  3. Process according to Claim 1 or 2, characterized in that the air separation unit (4) is fed with compressed air by a compression level of the compressor (1) located behind the first compression level of this compressor.
  4. Process according to one of Claims 1 to 3, characterized in that the converter (6) is fed by mixing air compressed by the compressor (1) to a pressure above the feed pressure of this converter (6) with oxygen produced by the air separation unit (4) substantially at the same pressure, by storing the oxygen-enriched air in the said buffer tank (7) when the consumption of oxygen-enriched air by the converter (6) is below the said threshold and by removing oxygen-enriched air from this buffer tank (7) through an expansion device (11) when the consumption of oxygen-enriched air by the converter (6) is above the said threshold.
  5. Process according to any one of Claims 1 to 3, characterized in that air compressed by the final stage of the compressor (1) to a pressure above the feed pressure of the converter (6) is stored in the said buffer tank (7) when the consumption of oxygen-enriched air by this converter (6) is below the said threshold and the converter is fed by mixing air stored in the buffer tank (7) and/or air compressed by the final stage of the compressor (1), both air streams being removed through an expansion device (11), with oxygen produced by the air separation unit (4) at a variable flow rate and at a pressure substantially equal to the feed pressure of the converter (6).
  6. Process according to any one of Claims 1 to 5, characterized in that the air intended for the converter (6) is compressed by the final stage of the compressor (1).
  7. Plant for feeding oxygen-enriched air into a non-ferrous metal production unit comprising a smelter (2) and a convertor (6), for implementing a process according to any one of Claims 1-6, comprising:
    an air separation unit (4) designed to deliver oxygen to the smelter (2) and the converter (6);
    a single air compressor (1), the delivery side of which is connected to the smelter (2), to the air separation unit (4) and to the converter (6) via first, second and third lines (3, 5, 8); and
    a buffer tank (7) connected to the said third line (8).
  8. Feed plant according to Claim 7, characterized in that the buffer tank (7) is also connected, on the one hand, to an oxygen output line (10) from the separation unit (4) intended for the converter (6) and, on the other hand, to this converter (6) via an expansion device (11).
  9. Feed plant according to Claim 7, characterized in that the buffer tank (7) is also connected to the converter (6) via an expansion device (11) and in that an oxygen output line from the separation unit (4) intended for the converter (6) runs into the line (12) which connects this expansion device to the converter (6).
  10. Feed plant according to any one of Claims 7 to 9, characterized in that the air separation unit (4) comprises two oxygen production circuits, one (9) feeding the smelter (2) and the other (10) feeding the converter (6).
  11. Feed plant according to Claims 9 and 10 taken together, characterized in that the oxygen production circuit feeding the converter (6) is provided with means (20) for adjusting the oxygen flow rate.
  12. Feed plant according to Claim 11, characterized in that the air separation unit (4) is a double-column air distillation unit which includes a swing system (16, 20 to 22) so as to produce a variable stream of oxygen by distillation of a constant air input.
  13. Feed plant according to any one of Claims 7 to 12, characterized in that the air compressor (1) comprises at least two compression levels, the delivery of the first level being connected to the said first line (3) and the delivery of the following level or levels being connected to the said second and third lines (5, 8).
  14. Feed plant according to Claim 13, characterized in that the compressor (1) has three compression levels, the deliveries of which are connected to the said first, second and third lines, respectively.
EP01402174A 2000-09-18 2001-08-14 Process and installation for supplying oxygen enriched air to a production unit of non-ferrous metals Expired - Lifetime EP1188843B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0011878 2000-09-18
FR0011878A FR2814178B1 (en) 2000-09-18 2000-09-18 SUPPLY OF OXYGEN-ENRICHED AIR TO A NON-FERROUS METAL PRODUCTION UNIT

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EP1188843A1 EP1188843A1 (en) 2002-03-20
EP1188843B1 true EP1188843B1 (en) 2004-05-19

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EP (1) EP1188843B1 (en)
JP (1) JP2002155321A (en)
CN (1) CN1227380C (en)
AU (1) AU773575B2 (en)
CA (1) CA2357371A1 (en)
DE (1) DE60103339T2 (en)
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ZA (1) ZA200107030B (en)

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FR2842124B1 (en) * 2002-07-09 2005-03-25 Air Liquide METHOD FOR CONDUCTING AN ELECTRIC POWER GAS-GENERATING PLANT AND THIS PRODUCTION PLANT
FR2853407B1 (en) * 2003-04-02 2012-12-14 Air Liquide METHOD AND INSTALLATION FOR SUPPLYING GAS UNDER PRESSURE
FR2862128B1 (en) * 2003-11-10 2006-01-06 Air Liquide PROCESS AND INSTALLATION FOR SUPPLYING HIGH-PURITY OXYGEN BY CRYOGENIC AIR DISTILLATION
FR2862004B3 (en) * 2003-11-10 2005-12-23 Air Liquide METHOD AND INSTALLATION FOR ENRICHING A GASEOUS FLOW IN ONE OF ITS CONSTITUENTS
CN102168804B (en) * 2011-02-11 2012-10-10 安徽淮化股份有限公司 Oxygen-enriched air distribution device
TWI480814B (en) * 2012-01-13 2015-04-11 China Steel Corp Decision support system for determining production of oxygen
JP6115887B2 (en) * 2013-03-15 2017-04-19 住友金属鉱山株式会社 Oxygen compressor switching flow rate measurement method
JP6575499B2 (en) * 2016-12-15 2019-09-18 Ｊｆｅスチール株式会社 Oxygen supply apparatus and method in iron making process

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SU1296616A1 (en) * 1985-10-14 1987-03-15 Государственный Научно-Исследовательский Институт Автоматизации Производственных Процессов Химической Промышленности И Цветной Металлургии Method for converting copper mattes
US5194213A (en) * 1991-07-29 1993-03-16 Inco Limited Copper smelting system
FR2680114B1 (en) * 1991-08-07 1994-08-05 Lair Liquide METHOD AND INSTALLATION FOR AIR DISTILLATION, AND APPLICATION TO THE GAS SUPPLY OF A STEEL.
FR2712383B1 (en) * 1993-11-12 1995-12-22 Air Liquide Combined installation of a metal production unit and an air separation unit.
FR2745821B1 (en) * 1996-03-11 1998-04-30 Air Liquide METHOD FOR CONDUCTING AN INSTALLATION COMPRISING A METAL PROCESSING UNIT AND A GAS PROCESSING UNIT
FR2753638B1 (en) * 1996-09-25 1998-10-30 PROCESS FOR SUPPLYING A GAS CONSUMER UNIT
FR2774157B1 (en) * 1998-01-23 2000-05-05 Air Liquide COMBINED INSTALLATION OF AN OVEN AND AN AIR DISTILLATION APPARATUS AND METHOD OF IMPLEMENTING IT
JPH11335751A (en) * 1998-05-22 1999-12-07 Mitsui Mining & Smelting Co Ltd Method for operating copper converter

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DE60103339D1 (en) 2004-06-24
US20020033566A1 (en) 2002-03-21
CA2357371A1 (en) 2002-03-18
AU6556701A (en) 2002-03-21
JP2002155321A (en) 2002-05-31
FR2814178B1 (en) 2002-10-18
US6576040B2 (en) 2003-06-10
ZA200107030B (en) 2002-02-25
DE60103339T2 (en) 2005-04-14
CN1348015A (en) 2002-05-08
CN1227380C (en) 2005-11-16
EP1188843A1 (en) 2002-03-20
FR2814178A1 (en) 2002-03-22
AU773575B2 (en) 2004-05-27

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