WO2013073662A1 - 直接還元鉄製造システム - Google Patents
直接還元鉄製造システム Download PDFInfo
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- WO2013073662A1 WO2013073662A1 PCT/JP2012/079765 JP2012079765W WO2013073662A1 WO 2013073662 A1 WO2013073662 A1 WO 2013073662A1 JP 2012079765 W JP2012079765 W JP 2012079765W WO 2013073662 A1 WO2013073662 A1 WO 2013073662A1
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- gas
- reduced iron
- direct
- production system
- reduction furnace
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/16—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/20—Carbon monoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/025—Other waste gases from metallurgy plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
- C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/42—Sulphur removal
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Definitions
- the present invention relates to a direct reduced iron production system.
- direct reduced iron When iron ore such as fine ore or agglomerate is reduced in a solid phase with a modified natural gas at a temperature of, for example, about 1000 ° C., direct reduced iron (DRI) is obtained.
- DRI direct reduced iron
- the efficiency of the reducing furnace exhaust gas is increased by returning it to the reducing gas flow and reusing it.
- Water (H 2 O) and carbon dioxide (CO 2 ) generated in the reduction furnace are inactive in the reduction furnace, so it is necessary to remove them when they are reused. Carbon dioxide is removed by a removal unit such as an amine solvent (Patent Document 1).
- the amine solvent is replaced with a new one to reduce the concentration of deteriorated substances and managed.
- the amine solvent is frequently replaced. There is a problem that a large amount of solvent is consumed.
- the present invention provides a direct reduced iron production system capable of reducing the amount of acid gas absorbent used when removing acidic gas such as CO 2 in exhaust gas from a direct reduction iron furnace.
- the task is to do.
- the first invention of the present invention for solving the above-mentioned problems is a direct reduction furnace for directly reducing iron ore to reduced iron using a high-temperature reducing gas containing hydrogen and carbon monoxide, and from the direct reduction furnace
- An acid gas removal device comprising an acid gas component absorption tower for removing an acid gas component in the exhaust gas from the reduction furnace discharged by an acid gas absorption liquid and a regeneration tower for discharging the acid gas, the acid gas component absorption tower, and the regeneration
- the present invention provides a direct reduced iron production system comprising a deteriorated substance removing device that separates and removes deteriorated substances in an absorbing solution that is circulated and used between towers.
- the first invention in the first invention, it comprises a bypass circuit for bypassing a part of the lean solution returned from the regeneration tower to the absorption tower, and a filter interposed in the bypass circuit.
- a bypass circuit for bypassing a part of the lean solution returned from the regeneration tower to the absorption tower, and a filter interposed in the bypass circuit.
- an introduction line for introducing the reduction furnace exhaust gas into the acidic gas removal device and a heat exchanger interposed in the introduction line and exchanging heat of the reduction furnace exhaust gas.
- a bag filter provided on the upstream side of the heat exchanger, and a scrubber provided on the downstream side of the heat exchanger.
- the fourth invention is the direct reduced iron production system according to any one of the first to third inventions, wherein the acid gas absorbing liquid has a low boiling point.
- a fifth invention is the direct reduced iron production system according to any one of the first to fourth inventions, wherein the high-temperature reducing gas is a gas derived from natural gas, coal gasification gas, or coke oven gas. It is in.
- the high-temperature reducing gas is a gas derived from natural gas, coal gasification gas, or coke oven gas. It is in.
- the deteriorated product in the acidic gas absorbent that circulates between the absorption tower and the regeneration tower can be separated by the deteriorated substance removing device, so that frequent replacement of the acidic gas absorbent is unnecessary.
- the amount of solvent used can be greatly reduced.
- by continuously managing the concentration of solvent-degraded products it is possible to suppress the occurrence of forming, realize stable operation, and suppress corrosion of equipment.
- By stabilizing the operation it is possible to realize a stable operation of the entire directly reduced iron process and cost reduction by reducing solvent consumption.
- the deteriorated material removal apparatus is operated using the heat in the direct reduced iron process system, it does not require additional energy consumption and is economical.
- FIG. 1 is a schematic diagram of a directly reduced iron production system according to the first embodiment.
- FIG. 2 is a schematic diagram of a directly reduced iron production system according to the second embodiment.
- FIG. 3 is a schematic diagram of a directly reduced iron production system according to the third embodiment.
- FIG. 4 is a schematic diagram of a directly reduced iron production system according to the fourth embodiment.
- FIG. 5 is a schematic diagram of another directly reduced iron production system according to the fourth embodiment.
- FIG. 6 is a schematic diagram of a directly reduced iron production system according to the fifth embodiment.
- FIG. 7 is a schematic diagram of another directly reduced iron production system according to the fifth embodiment.
- FIG. 1 is a schematic diagram of a directly reduced iron production system according to the first embodiment.
- the directly reduced iron production system 10A directly reduces iron ore 12a to reduced iron 12b using a high-temperature reducing gas (hereinafter referred to as “reducing gas”) 11 containing hydrogen and carbon monoxide.
- reducing gas high-temperature reducing gas
- the acidic gas component (CO 2 , H 2 S) in the reduction furnace (hereinafter referred to as “reduction furnace”) 13 and the reduction furnace exhaust gas 14 discharged from the direct reduction furnace 13 is converted into an acidic gas absorbing liquid such as an amine solvent (
- An acid gas removing device 16 comprising an acid gas component absorption tower (hereinafter referred to as “absorption tower”) 16a to be removed by 15) and a regeneration tower 16b for releasing the acid gas and regenerating the absorption liquid 15;
- a deteriorated substance removing device 17 that separates and removes deteriorated substances in the absorbing liquid 15 that is circulated and used in the absorption tower 16a and the regeneration tower 16b.
- L 1 is a gas supply line for introducing the reducing furnace exhaust gas 14 to the acid gas removal device 16
- L 2 is a rich solution line
- L 3 is a lean solution line
- L 4 is a lean solution branch line
- L 5 is A reboiler line that circulates the lean solution in the lower part of the regeneration tower
- L 6 is a gas discharge line
- L 7 is a condensed water line
- L 8 is a recovered gas discharge line
- L 9 is a purified gas discharge line
- L 10 is a gas discharge line.
- the reducing gas 11 is heated to a predetermined high temperature (for example, 900 to 1,050 ° C.) when being introduced into the reducing furnace 13.
- the iron ore 12a is supplied from the top, and the supplied iron ore 12a moves toward the furnace bottom.
- the iron ore is oxidized by hydrogen (H 2 ) and carbon monoxide (CO), which are main components of the reducing gas 11, in countercurrent contact with the high-temperature reducing gas 11 supplied from the side of the reducing furnace 13.
- (Iron) 12a is reduced to become reduced iron 12b, and hydrogen (H 2 ) and carbon monoxide (CO) are converted into water (H 2 O) and carbon dioxide (CO 2 ), respectively.
- the reduced iron ore 12a is taken out from the lower side of the reduction furnace 13 as reduced iron 12b.
- hydrogen (H 2 ) and carbon monoxide (CO) in the reducing gas 11 are not used in the reduction furnace 13, and most of the hydrogen (H 2 ) and carbon monoxide (CO) are used. It is discharged from the gas supply line L 1 as reducing furnace exhaust gas 14 without being used.
- the reduction furnace exhaust gas 14 from the reduction furnace 13 contains dust such as iron powder generated from the reduction furnace 13 and adversely affects the operation of the acidic gas removal device 16 connected to the downstream side, so that the scrubber 20 In addition to removing dust, water (H 2 O) generated in the reduction furnace 13 is removed.
- the reducing furnace exhaust gas 14 is pressurized by a compressor 21 interposed in the gas supply line L 1 and then introduced into the cooling and cleaning tower 22.
- the gas temperature is lowered by cooling water and then introduced into the absorption tower 16 a of the acidic gas removal device 16.
- the CO 2 and H 2 S acidic gases are removed from the reducing furnace exhaust gas 14 by the chemical absorption reaction of the absorbing liquid 15 to form a purified gas 14A from which the acidic gases have been removed, and a purified gas supply line from the top side. It is discharged from the L 9. Since this purified gas 14A contains unused H 2 and CO, they may be combined with the reducing gas 11 and reused as the reducing gas 11 (described later).
- a part of the gas 14 a exiting the scrubber 20 is on the downstream side of the scrubber 20. in, and to discharge out of the system by a gas discharge line L 10 branched from the gas supply line L 1.
- the absorption tower 16 a absorbs and removes CO 2 and H 2 S acid gas components from the absorption liquid 15 out of CO, H 2 , CO 2 and H 2 S contained in the reduction furnace exhaust gas 14. is doing.
- the absorbent 15 is what has absorbed CO 2 and H 2 S in the absorber tower 16a called rich solution 15a, the rich solution 15a is supplied to the regenerator 16b side rich solution line L 2.
- the rich solution 15a introduced into the regeneration tower 16b releases the absorbed CO 2 and H 2 S by the heat of water vapor superheated by the reboiler 23 in the inside of the tower to become the lean solution 15b, and the lean solution line L 3 is returned again to the absorption tower 16a and recycled.
- a cooling unit (not shown) is provided for removing the absorption liquid accompanying the purified gas 14A. Further, in the regeneration tower 16b, the recovered gas 14B mainly composed of CO 2 and H 2 S released from the rich solution 15a is discharged out of the system through the gas discharge line L 6 from the top.
- the recovered gas 14B is cooled by the cooler 25 interposed in the gas discharge line L 6 , and then the condensed water 27 is separated by the gas-liquid separator 26. Condensed water 27 is separated is returned through the condensed water line L 7 to the regenerator within 16b.
- the reduction furnace exhaust gas 14 from the reduction furnace 13 contains a large amount of CO and iron components, and those that cannot be removed by the scrubber 20 interposed in the gas supply line L 1 may be mixed into the acid gas removal device 16. is there.
- a part of the absorbing liquid 15 undergoes a chemical reaction with such CO and iron components due to a long operation, thereby generating a deteriorated product, resulting in a decrease in processing capability.
- the CO-deteriorated product generates formic acid due to the dissolution of CO in the reducing furnace exhaust gas 14 in the absorbent 15, and this formic acid reacts with an absorbent such as an amine solvent.
- an absorbent such as an amine solvent.
- the salt By making the salt, it becomes a heat-stable salt, which accumulates in the absorbent 15. Due to the accumulation of the thermally stable salt in the absorption liquid system, for example, the boiling point of the absorption liquid rises. If this boiling point rise occurs, the temperature rise in the reboiler 23 of the regeneration tower 16b promotes the thermal deterioration of the solvent, and the thermal efficiency of the reboiler 23 decreases, which is not preferable. Further, when the viscosity increases, the pressure loss increases and foaming occurs, which is not preferable.
- the iron-derived deteriorated product is caused by the deterioration of the absorbent.
- glycine such as bicine (N, N-bis (2-hydroxyethyl) glycine) is generated due to the deterioration.
- bicine N, N-bis (2-hydroxyethyl) glycine
- the trivalent iron complex participates in the oxidation-reduction reaction, which promotes dissolution of iron and accelerates it. Since corrosion is accelerated, it is not preferable.
- the dust derived from iron ore flowing from the reduction furnace 13 has a large specific surface area, rapid generation of an iron complex is expected.
- the absorbing solution 15 itself is also decomposed by heating in the reboiler 23 to generate a deteriorated component, so that the acid gas absorbing ability is lowered.
- the absorption liquid 15 Since the absorption liquid 15 is circulated and reused as the rich solution 15a and the lean solution 15b, the above-described deteriorated substances accumulate in the absorption liquid 15, causing a reduction in processing capacity and corrosion of the apparatus.
- the lean solution branch line L 4 branched from the lean solution line L 3 returning from the regeneration tower 16b to the absorption tower 16a is provided, and the deteriorated substance removing device 17 is provided in the lean solution branch line L 4 .
- the absorption liquid is regenerated by separating and removing the deteriorated substances.
- the lean solution 15b to be supplied to the lean-solution branch line L 4 are, are managed as needed by opening and closing the valve V interposed in the lean-solution branch line L 4.
- the concentration of the deteriorated material accumulated in the absorbing liquid 15 is reduced, and the performance of the absorbing liquid 15 is recovered or maintained, and the performance of the absorbing liquid 15 over a long period of time is improved. Maintenance is performed.
- the degradation product removing device 17 includes an absorption liquid regeneration method by distillation using a difference in boiling point between the absorption liquid 15 to be used and the degradation product, a method of concentrating and separating degradation products by electrodialysis, and degradation products by ion exchange. There is a method of separating the above, and a method of combining them is also included.
- Examples of the reclaimer of the absorbing liquid regeneration method include a heat exchanger type reclaimer.
- the valve V When removing the deteriorated product, the valve V is opened to degrade a part of the lean solution 15b when the reference value of one or both of the deteriorated product caused by CO or the deteriorated product caused by Fe is exceeded.
- the material removal device 17 is supplied to start the operation of removing the deteriorated material. And when the density
- the reference value for starting the deterioration removal of the deterioration caused by CO for example, it may be performed when it exceeds 2% by weight.
- glycine such as bicine
- it may be performed when it exceeds 5 ppm.
- the degradation product When measuring the values of both CO-induced degradation products (thermally stable salt concentration) and Fe-induced degradation products (glycine such as bicine), the degradation product will be used when either of them reaches the reference value. A removal operation can be initiated.
- concentration of the said deteriorated material is an example, and is suitably changed with the kind of absorption liquids, such as an amine solvent of the absorption liquid 15, and various conditions in the acidic gas removal apparatus 16. FIG.
- the iron concentration is expected to increase rapidly, it is necessary to monitor the concentration frequently separately.
- Deterioration monitoring may be performed by an automatic or manual analysis operation, and may be determined by a determination unit (not shown).
- an amine-based solvent as the absorbing liquid 15 that absorbs the acidic gas components (CO 2 , H 2 S).
- the amine solvent include methylethylamine (MEA).
- MEA methylethylamine
- 1DMA2P (1-dimethylamino-2-propanol; boiling point 124 ° C)
- DMAE N, N-dimethylaminoethanol; boiling point 134 ° C
- MPZ (1-methylpiperazine; boiling point 138 ° C), PZ (piperazine; boiling point) 146 ° C.), 2MPZ (2-methylpiperazine; boiling point 155 ° C.), DEAE (N, N-diethyl-2-aminoethanol; boiling point 161 ° C.), AMP (2-amino-2-methyl-1-propanol; boiling point 166 ° C), EAE (2-ethylaminoethanol; boiling point 170 ° C), monoethanolamine (MEA; boiling point 170 ° C),
- the deteriorated concentrate 29 concentrated by the deteriorated material removing device 17 is discharged out of the system.
- the gas 30 of the volatilized absorption liquid generated when the concentration treatment is performed by the deteriorated material removing device 17 is returned to the lower side of the regeneration tower 16b.
- the deteriorated product in the absorbent 15 circulating through the absorption tower 16a and the regeneration tower 16b can be separated by the deteriorated substance removing device 17, the replacement of the absorbent 15 frequently. This eliminates the need for the solvent and can greatly reduce the amount of solvent used.
- FIG. 2 is a schematic diagram of a directly reduced iron production system according to the second embodiment.
- symbol is attached
- a bug is added to the gas supply line L 1 for supplying the reducing furnace exhaust gas 14 in the direct reduced iron manufacturing system 10A of the first embodiment shown in FIG.
- a filter 31 and a heat exchanger 32 are installed. By installing the bag filter 31, the dust removal efficiency in the reduction furnace exhaust gas 14 is improved before the scrubber 20 is processed. Further, the heat exchange efficiency of the heat exchanger 32 is maintained by removing dust in the reduction furnace exhaust gas 14 supplied to the heat exchanger 32.
- the reboiler 23 and the deteriorated material removing device 17 each require a heat source.
- the heat exchanger 32 installed in the gas supply line L 1 is used as the heat source to generate the steam 24. It is possible to use the steam 24.
- FIG. 3 is a schematic diagram of a directly reduced iron production system according to the third embodiment.
- direct reduced iron manufacturing system 10A, 10B which concerns on Example 1 and 2 shown in FIG.1 and 2, the same code
- FIG. 3 in the directly reduced iron manufacturing system 10C of the present embodiment, in the directly reduced iron manufacturing system 10B shown in FIG. 2, a part of the lean solution 15b introduced from the regeneration tower 16b to the absorption tower 16a is bypassed.
- a lean solution bypass line L 11 is provided, and a filter 41 is interposed in the lean solution bypass line L 11 .
- the filter 41 By installing this filter 41 in the system, it is possible to maintain the performance of the absorbent 15 such as an amine solvent for a long period of time by further removing deteriorated substances and impurities that cannot be removed by the deteriorated substance removing device 17. Become.
- the component that cannot be removed by the deteriorated material removing device 17 is a volatile deterioration factor substance having a boiling point lower than that of an absorbing solution such as an amine solvent.
- an activated carbon filter is used as the filter 41.
- the filter is not limited to the activated carbon filter as long as impurities can be removed.
- Bypass quantity of lean solution 15b to the lean solution bypass line L 11 is, although about 1/10 of the total amount may be appropriately adjusted by the concentration of impurities.
- FIG. 4 is a schematic diagram of a directly reduced iron manufacturing system according to the fourth embodiment
- FIG. 5 is a schematic diagram of another directly reduced iron manufacturing system according to the fourth embodiment.
- symbol is attached
- the directly reduced iron manufacturing system 10 ⁇ / b> D of the present embodiment a case where natural gas is used as the reducing gas 11 is illustrated.
- a gas reformer 51 for reforming the natural gas 50 is provided, and the steam 24 is supplied. Steam reforming, carbon dioxide reforming, or a combination of these is performed, and natural gas 50 is converted into hydrogen (H 2 ) and carbon monoxide (CO), and hydrogen (H 2 ) and monoxide are oxidized.
- the reformed gas 52 containing carbon (CO) as a main component is obtained.
- the reformed gas 52 reformed by the reformer 51 is gas-cooled by the gas cooler 53 and then separated from the condensed water 55 by the gas-liquid separator 54.
- the reformed gas 52 from which the moisture has been separated is introduced into the gas heater 56, heated to a predetermined high temperature (for example, 900 to 1,050 ° C.), and supplied as the reducing gas 11 into the reducing furnace 13.
- the purified gas 14A purified by the absorption tower 16a is joined to the natural gas 50 side, as shown in FIG.
- the refined gas supply line (* 1) is provided so that the refined gas 14A merges with the reformed gas 52 after separating the condensed water 55.
- this refined gas 14 ⁇ / b> A is merged with the reformed gas 52, the refined gas 14 ⁇ / b> A is adjusted to have an ideal reducing gas composition for the reduction reaction in the reduction furnace 13 and introduced into the reformer 51.
- the recovered gas 14B released from the regeneration tower 16b is mainly composed of CO 2 and H 2 S, provided with a recovered gas supply line (* 2), and used for the reforming furnace or gas heater 56 of the gas reformer 51. It has been introduced into the furnace. Then, H 2 S is burned in the furnace to form sulfur dioxide (SO 2 ), diluted with a large amount of combustion gas discharged from each furnace, and then appropriately treated as exhaust gas from each furnace (for example, desulfurization treatment). Etc.) and then release to the atmosphere.
- SO 2 sulfur dioxide
- Etc. desulfurization treatment
- the steam generated by the waste heat of the reforming furnace and the steam generated by the heat recovered by the cooler 53 for removing moisture in the reformed gas 52 emitted from the gas reformer 51 are described above.
- the reboiler 23 and the deteriorated substance removing device 17 can be used as the water vapor 24.
- a part of the gas 14a exiting the scrubber 20 is provided with a reducing furnace exhaust gas supply line (* 3) to provide gas reforming. It can be introduced into the reforming furnace of the vessel 51 or the furnace of the gas heater 56 and combusted here.
- the exhaust gas from the furnace of the gas reformer 51 or the gas heater 56 is exhausted after sufficiently recovering waste heat by heat recovery means such as a heat exchanger.
- heat recovery means for example, water vapor is produced and used in the heat-requiring part in the system such as the reboiler 23 and the deteriorated substance removing device 17, or the steam turbine is driven and used as power for the compressor 21 described above. Or it can generate electricity and use it as electricity.
- FIG. 6 is a schematic diagram of a directly reduced iron manufacturing system according to the fifth embodiment
- FIG. 7 is a schematic diagram of another directly reduced iron manufacturing system according to the fifth embodiment.
- symbol is attached
- FIG. 6 in the directly reduced iron production system 10 ⁇ / b> E of the present embodiment, a case where a coal gasification gas 60 other than natural gas is used as the reducing gas 11 is illustrated.
- coal gasification gas 60 obtained by gasifying and refining coal in a gasification furnace (not shown) is heated by a gas heater 56 to form the reducing gas 11.
- a refined coke oven gas can be used as the reducing gas 11.
- a refined gas supply line (* 1) is provided as shown in FIG.
- the coal gasified gas 60 is merged, and then heated to a predetermined temperature by the gas heater 56 to form the reducing gas 11 and introduced into the reducing furnace 13.
- the recovered gas 14B discharged from the regeneration tower 16b is provided with a recovered gas supply line (* 2) and introduced into the furnace of the gas heater 56. Then, H 2 S is burned in the furnace to form sulfur dioxide (SO 2 ), diluted with a large amount of combustion gas discharged from the furnace, and then subjected to appropriate treatment (for example, desulfurization treatment) as exhaust gas from each furnace. After doing, release to the atmosphere.
- appropriate treatment for example, desulfurization treatment
- the gas heater 56 may be omitted.
- the coal gasification gas 60 and the like increase the amount of the reducing gas 11 by the partial oxidation reaction by introducing the fuel 70 such as oxygen and natural gas on the upstream side of the reduction furnace 13.
- the fuel 70 such as oxygen and natural gas
- the fuel 70 may be supplied as necessary in the direct reduced iron production system 10D of the fourth embodiment to increase the amount of the reducing gas 11.
- Example 5 in order to avoid accumulation of CH 4 and N 2 which are inactive components in the system, a part of the gas 14a exiting the scrubber 20 is supplied to the reducing furnace exhaust gas supply line (* 3 ) May be provided and introduced into the furnace of the gas heater 56, where the combustion treatment may be performed.
Abstract
Description
還元炉で発生する水(H2O)、二酸化炭素(CO2)とは、還元炉内では不活性なため、再利用する際には除去する必要があり、水は冷却器又はスクラバで、二酸化炭素は例えばアミン系溶剤等の除去ユニットで除去されている(特許文献1)。
また、連続した溶剤劣化物の濃度の管理を行うことにより、フォーミング発生を抑え、安定した運転を実現し、機器の腐食も抑えることができる。
この運転の安定化によって、直接還元鉄プロセス全体の安定運転、及び溶剤消費量削減による低コスト化を実現することができる。
さらに、直接還元鉄プロセス系内での熱を利用して劣化物除去装置を稼動することにより、追加のエネルギー消費を必要とせず、経済的となる。
図1中、符号15aはリッチ溶液、15bはリーン溶液、20はスクラバ、21は圧縮機、22は冷却洗浄塔、23はリボイラ、24は水蒸気、25は冷却器、26は気液分離器、27は凝縮水、L1は還元炉排ガス14を酸性ガス除去装置16へ導入するガス供給ライン、L2はリッチ溶液ライン、L3はリーン溶液ライン、L4はリーン溶液分岐ライン、L5は再生塔の下部でリーン溶液を循環させるリボイラライン、L6はガス放出ライン、L7は凝縮水ライン、L8は回収ガス排出ライン、L9は精製ガス排出ライン、L10はガス排出ラインを各々図示する。
ここで、還元ガス11は、還元炉13に導入する際には、所定の高温(例えば900~1,050℃)の温度まで加熱されている。
還元された鉄鉱石12aは、還元鉄12bとして還元炉13の下部側から取り出される。
この吸収塔16aでは、還元炉排ガス14からCO2とH2Sの酸性ガスが吸収液15の化学吸収反応によって除去され、酸性ガスが除去された精製ガス14Aとなり、頂部側から精製ガス供給ラインL9より排出される。
この精製ガス14A中には、未利用のH2とCOとが含まれているので、還元ガス11に合流し、還元ガス11として再利用するようにしてもよい(後述する)。
この吸収液15は、吸収塔16a内でCO2とH2Sを吸収したものをリッチ溶液15aと称し、このリッチ溶液15aは、リッチ溶液ラインL2で再生塔16b側に供給される。再生塔16bに導入されたリッチ溶液15aは、この塔内部において、リボイラ23で過熱された水蒸気の熱により、吸収したCO2とH2Sを放出して、リーン溶液15bとなり、リーン溶液ラインL3を介して再度吸収塔16aに戻され、循環再利用されている。
また、再生塔16bでは、リッチ溶液15aから放出されたCO2とH2Sを主成分とする回収ガス14Bがその頂部からガス放出ラインL6を介して、系外へ排出される。
また、長時間の運転によって吸収液15の一部がこのようなCOや鉄成分と化学反応を起こすことによって劣化物を生成し、処理能力が低下する。
この熱安定性塩の吸収液系内の蓄積により、例えば吸収液の沸点上昇が発生する。
この沸点上昇が発生すると、再生塔16bのリボイラ23での温度上昇により、溶剤の熱劣化が促進され、また、リボイラ23の熱効率が低下するので好ましくない。
また、粘度上昇する場合には、圧損が上昇し、フォーミングが発生するので好ましくない。
特に、還元炉13から流入する鉄鉱石起因のダストは比表面積が大きいため、鉄錯体の急激な生成が予想される。
また、吸収液15自体もリボイラ23での加熱によって分解し劣化成分を生成することで酸性ガスの吸収能力が低下することとなる。
吸収液再生方式のリクレーマとしては、例えば熱交換器型リクレーマを挙げることができる。
そして、リーン溶液15b中の劣化物の濃度が所定値未満まで低下した際に、劣化物除去操作を停止する。
なお、前記劣化物の濃度は一例であり、吸収液15のアミン系溶剤等の吸収液の種類、酸性ガス除去装置16での諸条件により適宜変更される。
なお、鉄濃度の急激な上昇が予想されるため、濃度監視は別途頻繁に行う必要がある。
特に、1DMA2P(1-ジメチルアミノ-2-プロパノール;沸点124℃)、DMAE(N,N-ジメチルアミノエタノール;沸点134℃)、MPZ(1-メチルピペラジン;沸点138℃)、PZ(ピペラジン;沸点146℃)、2MPZ(2-メチルピペラジン;沸点155℃)、DEAE(N,N-ジエチル-2-アミノエタノール;沸点161℃)、AMP(2-アミノ-2-メチル-1-プロパノール;沸点166℃)、EAE(2-エチルアミノエタノール;沸点170℃)、モノエタノールアミン(MEA;沸点170℃)、nBAE(2-ブチルアミノエタノール;沸点200℃)、4AMPR(4-ピペリジンメタンアミン;沸点200℃)のような低沸点のアミンをベースとした溶剤を用いることで、劣化物を例えば蒸発分離することを容易としている。
これは、アミン系の溶剤であっても、例えばMDEA(N-メチルジエタノールアミン)等のような高沸点(247℃)のアミンをベースとした溶剤を用いる場合には、水蒸気を用いた蒸発により劣化物の蒸発分離が困難であり、再生利用が効率的でないからである。
なお、劣化物除去装置17で濃縮処理した際に発生する揮発された吸収液のガス30は、再生塔16bの下部側に戻される。
この運転の安定化によって、直接還元鉄プロセス全体の安定運転、及び溶剤消費量削減による低コスト化を実現することができる。
図2に示すように、本実施例の直接還元鉄製造システム10Bでは、図1に示す実施例1の直接還元鉄製造システム10Aにおいて、還元炉排ガス14を供給するガス供給ラインL1に、バグフィルタ31及び熱交換器32が設置されている。
このバグフィルタ31の設置により、スクラバ20の処理以前において還元炉排ガス14中のダスト除去の効率化を図っている。また、熱交換器32に供給する還元炉排ガス14中のダストを除去することで、熱交換器32の熱交換効率の維持を図るようにしている。
図3に示すように、本実施例の直接還元鉄製造システム10Cでは、図2に示す直接還元鉄製造システム10Bにおいて、再生塔16bから吸収塔16aに導入されるリーン溶液15bの一部をバイパスさせるリーン溶液バイパスラインL11を設け、このリーン溶液バイパスラインL11にフィルタ41を介装している。
この劣化物除去装置17で除去できない成分とは、沸点がアミン系溶剤等の吸収液よりも低い揮発性劣化要因物質等である。
このリーン溶液バイパスラインL11へのリーン溶液15bのバイパス量は、全量の1/10程度としているが、不純物の濃度により適宜調整してもよい。
図4に示すように、本実施例の直接還元鉄製造システム10Dでは、還元ガス11として、天然ガスを用いる場合を例示する。
水分が分離された改質ガス52は、ガスヒータ56に導入され、所定の高温(例えば900~1,050℃)に加熱され、還元ガス11として、還元炉13内に供給される。
この精製ガス14Aを改質ガス52に合流する場合には、還元炉13での還元反応に理想的な還元ガス組成となるように調整して、改質器51に導入するようにしている。
そして炉内でH2Sを燃焼させて二酸化硫黄(SO2)とし、それぞれの炉から排出される大量の燃焼ガスによって希釈された後、それぞれの炉からの排ガスとして適切な処理(例えば脱硫処理等)を行った後、大気に放出する。
図6に示すように、本実施例の直接還元鉄製造システム10Eでは、還元ガス11として、天然ガス以外の石炭ガス化ガス60を用いる場合を例示する。
本実施例では、石炭をガス化炉(図示せず)でガス化し、精製して得た石炭ガス化ガス60を用い、ガスヒータ56で加熱して還元ガス11としている。
また、石炭ガス化ガス60以外としては、コークス炉ガスを精製したものを還元ガス11として利用することもできる。
そして炉内でH2Sを燃焼させて二酸化硫黄(SO2)とし、炉から排出される大量の燃焼ガスによって希釈された後、それぞれの炉からの排ガスとして適切な処理(例えば脱硫処理)を行った後、大気に放出する。
なお、この酸素と天然ガス等の燃料70は、実施例4の直接還元鉄製造システム10Dにおいても、必要に応じて供給して、還元ガス11の増量を行うようにしてもよい。
11 高温還元ガス
12a 鉄鉱石
12b 還元鉄
13 直接還元炉
14 還元炉排ガス
15 酸性ガス吸収液(吸収液)
16 酸性ガス除去装置
16a 酸性ガス成分吸収塔(吸収塔)
16b 再生塔
17 劣化物除去装置
Claims (5)
- 水素、一酸化炭素を含む高温還元ガスを用いて、鉄鉱石を還元鉄に直接還元する直接還元炉と、
該直接還元炉から排出される還元炉排ガス中の酸性ガス成分を吸収液により除去する酸性ガス成分吸収塔と酸性ガスを放出する再生塔とからなる酸性ガス除去装置と、
前記酸性ガス成分吸収塔と前記再生塔との間を循環利用される吸収液中の劣化物を分離除去する劣化物除去装置とを具備することを特徴とする直接還元鉄製造システム。 - 請求項1において、
前記再生塔から前記吸収塔に返送するリーン溶液の一部をバイパスするバイパス回路と、
該バイパス回路に介装されるフィルタとを具備することを特徴とする直接還元鉄製造システム。 - 請求項1又は2において、
前記還元炉排ガスを前記酸性ガス除去装置に導入する導入ラインと、
該導入ラインに介装され、前記還元炉排ガスを熱交換する熱交換器と、
該熱交換器の前流側に設けられるバグフィルタと、
前記熱交換器の後流側に設けられるスクラバと、を具備することを特徴とする直接還元鉄製造システム。 - 請求項1乃至3のいずれか一つにおいて、
前記酸性ガス吸収液が、低沸点であることを特徴とする直接還元鉄製造システム。 - 請求項1乃至4のいずれか一つにおいて、
前記高温還元ガスが、天然ガス又は石炭ガス化ガス又はコークス炉ガス由来のガスであることを特徴とする直接還元鉄製造システム。
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US9557113B2 (en) | 2017-01-31 |
MX2014004993A (es) | 2014-05-22 |
CA2853420C (en) | 2017-07-11 |
JP2013108108A (ja) | 2013-06-06 |
RU2567965C1 (ru) | 2015-11-10 |
CA2853420A1 (en) | 2013-05-23 |
US20140252700A1 (en) | 2014-09-11 |
MY171824A (en) | 2019-10-31 |
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