KR100321049B1

KR100321049B1 - A fluidized-bed type reduction method and apparatus for fine iron ores

Info

Publication number: KR100321049B1
Application number: KR1019980038700A
Authority: KR
Inventors: 김행구; 최낙준; 강흥원; 정우창
Original assignee: 이구택; 포항종합제철 주식회사; 신현준; 재단법인 포항산업과학연구원; 암루쉬 만프레드, 프로머 우어줄라; 뵈스트-알핀 인두스트리안라겐바우 게엠바하
Priority date: 1998-09-18
Filing date: 1998-09-18
Publication date: 2002-04-17
Also published as: KR20000020206A

Abstract

본 발명은 용융선철 및 용융강 제조시 분철광석을 환원시키는 유동층식 환원방법 및 그 환원장치에 관한 것으로서,넓은 입도분포의 분철광석을 안정하게 유동시킬 수 있고, 또한 환원율과 가스이용율을 향상시킬 수 있고, 또한 예열/예비환원공정을 단축시킬 수 있음과 더불어 분철광석의 입도분포에 따라 그 입도별로 체류시간을 융통성있게 제어함으로서 보다 짧은 시간에 보다 높은 평균환원율을 얻을 수 있는 분철광석의 유동층식 환원방법 및 그 환원장치를 제공하고자 함에 그 목적이 있다.The present invention relates to a fluidized bed reduction method and a reducing apparatus for reducing iron ore in the manufacture of molten pig iron and molten steel, and can stably flow the iron ore of a wide particle size distribution, and can also improve the reduction rate and gas utilization rate. In addition, it is possible to shorten the preheating / preliminary reduction process and to flexibly control the residence time for each particle size according to the particle size distribution of the iron ore, thereby reducing the fluidized-bed reduction of the iron ore to obtain a higher average reduction rate in a shorter time. The object is to provide a method and a reducing apparatus thereof.

본 발명은 분철광석을 유동층식 환원장치에서 환원하는 방법에 있어서, 원통형 대경 상부로와 소경 하부로로 이루어진 시리얼 트윈(serial twin)형 유동층로의 하부로에 분철광석을 장입하고, 중/소립광석의 종말속도이상,대립광석의 종말속도 이하의 유속으로 상기 하부로의 저부에 환원가스를 공급하여 대립광석과 중/소립광석을 유동층로의 하부로와 상부로로 각각 분급하여 대립광석은 유동층로의 하부로에서, 그리고 중/소립광석은 유동층로의 상부로에서 하부로의 저부 및 상부로의 하부측벽을 통해 공급된 환원가스에 의해 예열 및 예비환원시키는 단계; 및 상기에서 예열 및 예비환원된 중/소립광석은 하나의 상광하협의 원추형 유동층로에서 최종 환원시키고, 그리고 예열 및 예비환원된 대립광석은 원통형 유동층로에서 1차 환원시킨 다음, 상기 상광하협의 원추형 유동층로로 보내어 최종환원시키는 단계를 포함하여 구성되는 분철광석의 유동층식 환원방법및 환원장치를 그 요지로 한다.The present invention is a method of reducing the iron ore in the fluidized bed reduction apparatus, charged iron ore into the lower portion of the serial twin-type fluidized bed consisting of a cylindrical large diameter upper path and a small diameter lower, the medium / small ore By supplying reducing gas to the bottom of the lower part at a flow rate above the terminal speed of the ore and below the terminal speed of the ore, the ore and the medium and small ore are classified into the lower part and the upper part of the fluidized bed, respectively. Preheating and pre-reduction at the bottom of and through the reducing gas supplied through the bottom side to the bottom and the top to the bottom of the fluidized bed furnace; And the preheated and pre-reduced medium / small-size ore is finally reduced in a conical fluidized bed furnace of a single subangular substrait, and the pre-heated and pre-reduced allele ore is first reduced in a cylindrical fluidized bed furnace, and then the conical shape of the sub-single channel Summary of the Invention The present invention relates to a fluidized bed reduction method and a reduction apparatus of ferrous ore including the steps of sending the fluidized bed to a final reduction.

Description

Fluidized-bed reduction method for iron ore and reduction device {A FLUIDIZED-BED TYPE REDUCTION METHOD AND APPARATUS FOR FINE IRON ORES}

본 발명은 용융선철 및 용융강 제조시 분철광석을 환원시키는 유동층식 환원방법 및 그 환원장치에 관한 것으로서, 보다 상세하게는, 넓은 입도분포를 갖는 분철광석을 안정된 유동상태에서 효율적이며 경제적으로 환원할 수 있는 분철광석의 유동층식 환원방법 및 그 환원장치에 관한 것이다.The present invention relates to a fluidized bed reduction method and a reducing apparatus for reducing iron ore in the manufacture of molten pig iron and molten steel, and more particularly, to efficiently and economically reduce the iron ore having a wide particle size distribution in a stable flow state. The present invention relates to a fluidized bed reduction method of ferrous ore and a reduction apparatus thereof.

철광석을 환원하여 용철을 생산하는 방법으로는 입도가 큰 철광석을 환원시키는 고로법이 종래부터 채용되고 있다.As a method of producing iron by reducing iron ore, a blast furnace method for reducing iron ore having a large particle size has been conventionally employed.

상기 고로법은 입도가 큰 광석을 환원시키므로 고정층방식으로 철광석의 환원이 가능하게 된다.Since the blast furnace method reduces ore having a large particle size, iron ore can be reduced in a fixed bed manner.

그러나, 미분 광석을 환원하고자 하는 경우 고정층방식인 고로법에서는, 로내 가스 유속이 낮아 스티킹(sticking)등으로 인해 조업중단이 발생할 우려가 있는 등의 문제점이 있게된다.However, when the fine ore is to be reduced, in the blast furnace method, which is a fixed bed method, there is a problem such that there is a possibility that operation stoppage may occur due to sticking due to low gas flow velocity in the furnace.

따라서, 미분광석을 환원하는 경우 환원이 일어나는 반응기내의 통기성을 확보하기 위해서는 유속을 충분히 하여 고체입자(철광석입자)의 움직임을 원활하게 하는 것이 요구되었으며, 이러한 요구에 부응하여 개발된 방법이 유동층식 환원방법 및 환원장치이다.Therefore, in order to secure the air permeability in the reactor in which reduction occurs when reducing fine ore, it is required to smooth the movement of solid particles (iron ore particles) by providing a sufficient flow rate. Method and reducing apparatus.

유동층을 이용하여 분철광석을 환원하는 유동층식 환원장치의 일례가 일본실용신안공보 소 58-217615호에 개시되어 있다.An example of a fluidized bed reduction apparatus for reducing iron ore using a fluidized bed is disclosed in Japanese Utility Model Publication No. 58-217615.

상기 일본실용신안공보에 제시되어 있는 분철광석의 유동층식 환원장치는 도1에 도시된 바와 같이, 원통형 환원로(1)와 사이클론(5)을 포함하며, 상기 원통형 환원로(1)의 측벽에는 원료철광석이 장입되는 철광석 장입구(2), 및 환원된 철광석을 배출하는 광석 배출구(4)가 형성되고, 그리고 그 저부에는 가스공급관(3)을 통해 가스를 분산시키는 가스 분산판(6)이 구비되어 있다.The fluidized bed reduction apparatus of the iron-iron ore presented in the Japanese Utility Model Publication includes a cylindrical reduction furnace 1 and a cyclone 5, as shown in FIG. An iron ore charging hole 2 into which raw iron ore is charged, and an ore outlet 4 for discharging reduced iron ore is formed, and at the bottom thereof, a gas distribution plate 6 for dispersing gas through the gas supply pipe 3 is provided. It is provided.

상기 분철광석의 유동층식 환원장치를 사용하여 분철광석을 환원하는 경우에는, 원통형 환원로(1)에 철광석 장입구(2)를 통해 분립상의 철광석을 장입하고 환원가스 공급관(3) 및 가스분산판(6)을 거쳐 적절한 유속의 환원가스를 공급하면 가스분산판(6)위의 철광석이 유동층을 형성하면서 혼합 교반되고 이 상태에서 환원가스와 접촉 반응하여 환원되며, 환원된 분철광석은 광석배출구(4)를 통해 배출된다.In the case of reducing the iron ore using the fluidized bed reduction device of the iron ore, charged iron ore into the cylindrical reduction furnace (1) through the iron ore charging inlet (2) and reducing gas supply pipe (3) and gas distribution plate When supplying reducing gas at an appropriate flow rate through (6), the iron ore on the gas distribution plate (6) is mixed and stirred while forming a fluidized bed. In this state, the reduced ore is reduced by contact with the reducing gas. 4) is discharged through.

이때 형성된 유동층의 형태는 원통형 환원로에서 공급되는 환원가스가 기포로 되어 환원로 상부의 입자층을 통과하면서 기포가 성장하는 기포유동층이다.In this case, the formed fluidized bed is a bubble fluidized bed in which bubbles are grown while reducing gas supplied from a cylindrical reduction furnace becomes bubbles and passes through a particle layer in the upper part of the reduction furnace.

그러나, 상기 분철광석의 유동층식 환원장치를 사용하여 분철광석을 환원하는 경우에는 비산되는 미립 철광석의 양을 줄이고, 환원가스 소모량을 최소화하고, 가스이용율을 높이기 위하여 환원로에 장입되는 분철광석의 입도가 엄격히 제한되어야 한다.However, in the case of reducing the iron ore by using the fluidized bed reduction device of the iron ore, the particle size of the iron ore charged in the reduction furnace to reduce the amount of fine iron ore scattered, minimize the reducing gas consumption, and increase the gas utilization rate Should be strictly limited.

상기 분철광석의 유동층식 환원장치에 장입되는 철광석의 입도분포는 넓은 입도분포를 갖지 못하고 0-0.5㎜, -1㎜, 1-2㎜등으로 제한된다.The particle size distribution of the iron ore charged into the fluidized bed reduction device of the iron ore does not have a wide particle size distribution and is limited to 0-0.5 mm, -1 mm, 1-2 mm and the like.

그러나, 실제로 존재하는 분철광석의 입도는 대부분이 8㎜이하로 그 입도범위가 대단히 넓다.However, the particle size of the iron ore that is actually present is mostly 8 mm or less, the particle size range is very wide.

따라서, 상기 입도를 가지는 분철광석을 사용하기 위하여 장입하는 철광석을 미리 규정입도로 체질하여 분급 사용하거나 규정입도 이하로 분쇄하여 사용함으로써 생산속도저하, 공정및 추가설비부담으로 인하여 경제적인 면에서 손실을 초래하는 문제점이 있다.Therefore, in order to use the iron ore having the above-mentioned particle size, the iron ore charged into the prescribed granularity is sieved in advance or classified and used below the prescribed granularity, thereby reducing the economical loss due to reduced production speed, process and additional equipment burden. There is a problem that results.

상기한 문제점을 해결하기 위해 제안된 환원장치 및 환원방법이 대한민국 특허 제117065호에 제시되어 있다.A reducing device and a reducing method proposed to solve the above problems are presented in Korean Patent No. 117065.

상기 특허에 제시되어 있는 환원장치 및 환원방법은, 도 2에 도시된 바와 같이 원추형의 3단 유동층식 환원장치 및 이를 이용한 환원방법이다.The reduction device and the reduction method proposed in the patent are a conical three-stage fluidized bed reduction device and a reduction method using the same, as shown in FIG. 2.

상기 3단 유동층식 환원장치는 넓은 입도분포를 갖는 분철광석을 안정하게 유동시킬 수 있도록 유동층의 형태를 상광하협의 원추형으로 하고, 환원율과 가스 이용율을 향상시키기 위해 분철광석이 기포유동층 상태에서 건조/예열되는 제 1유동층로(10), 상기 제 1유동층로의 배가스에 함유된 미립철광석을 집진하기 위한 제 1사이클론(40), 상기 제 1유동층로에서 건조예열된 분철광석을 예비환원하는 제 2유동층로(20), 상기 제 2유동층로의 배가스에 함유된 미립철광석을 집진하기 위한 제 2사이클론(50), 상기 제 2유동층로에서 예비환원된 분철광석을 최종환원하는 제3유동층로(30), 상기 제 3유동층로의 배가스에 함유된 미립철광석을 집진하기 위한 제 3사이클론(60)을 그 주요 구성으로 한다.The three-stage fluidized-bed reduction device has a conical shape of a fluidized bed so as to stably flow the iron ore having a wide particle size distribution, and the iron ore is dried / buried in a bubble fluidized bed to improve the reduction rate and gas utilization rate. The first fluidized bed 10 to be preheated, the first cyclone 40 for collecting particulate iron ore contained in the exhaust gas of the first fluidized bed, and the second to pre-reduce dry iron preheated in the first fluidized bed. Fluidized bed furnace 20, the second cyclone (50) for collecting the fine iron ore contained in the exhaust gas of the second fluidized bed furnace, the third fluidized bed furnace (30) for the final reduction of the reduced iron ore pre-reduced in the second fluidized bed furnace The main structure is a third cyclone 60 for collecting the fine iron ore contained in the exhaust gas of the third fluidized bed.

도 2에서, 미설명부호 70은 광석호퍼를, 그리고 미설명부호 80은 용융로를 나타낸다.In FIG. 2, reference numeral 70 denotes an ore hopper, and reference numeral 80 denotes a melting furnace.

상기한 원추형의 3단 유동층 환원장치는, 종래의 1단 원통형 유동층식 환원장치에 비해 넓은 입도분포를 갖는 분철광석을 안정하게 유동시킬 수 있으며 환원율과 가스 이용율을 상당히 향상시킬 수 있다.The conical three-stage fluidized bed reduction apparatus can stably flow the ferrite ore having a wider particle size distribution than the conventional single stage cylindrical fluidized bed reduction apparatus, and can significantly reduce the reduction rate and the gas utilization rate.

그러나, 상기한 원추형의 3단 유동층 환원장치를 사용하여 분철광석을 환원하는 경우에는 예열/예비환원단계가 2개의 단계로 필요이상으로 길고, 최종환원단계에서는 완전히 환원되는 시간이 긴 대립자나 완전히 환원되는 시간이 짧은 소립자가 동일한 시간동안 체류되므로, 환원시간이 짧은 경우에는 대립자의 환원율이 낮아져 전체 평균 환원율이 낮아지며 그 반대의 경우에는 소립자가 필요이상의 체류시간을 갖게 되므로 비경제적인 문제점이 있게 된다.However, in the case of reducing the iron ore using the conical three-stage fluidized bed reduction apparatus, the preheating / preliminary reduction stage is longer than necessary in two stages, and in the final reduction stage, alleles or long reductions are long. Since the small particles are shortened for the same time, when the reduction time is short, the reduction rate of the alleles is lowered and the overall average reduction rate is lowered, and vice versa, since the small particles have a residence time longer than necessary, there is an uneconomic problem.

본 발명자들은 상기한 종래기술의 문제점을 해결하기 위하여 연구 및 실험을 행하고, 그 결과에 근거하여 본 발명을 제안하게 된 것으로서, 본 발명은 넓은 입도분포의 분철광석을 안정하게 유동시킬 수 있고, 또한 환원율과 가스이용율을 향상시킬 수 있고, 또한 예열/예비환원공정을 단축시킬 수 있음과 더불어 분철광석의 입도분포에 따라 그 입도별로 체류시간을 융통성있게 제어함으로서 보다 짧은 시간에 보다 높은 평균환원율을 얻을 수 있는 분철광석의 유동층식 환원방법 및 그 환원장치를 제공하고자 함에 그 목적이 있다.The present inventors conducted research and experiments to solve the above problems of the prior art, and based on the results, the present invention proposes the present invention, and the present invention can stably flow iron powder ore of a wide particle size distribution, and The reduction rate and gas utilization rate can be improved, and the preheating / preliminary reduction process can be shortened and the average reduction rate can be obtained in a shorter time by flexibly controlling the residence time for each particle size according to the particle size distribution of iron ore. It is an object of the present invention to provide a fluidized bed reduction method and a reduction apparatus thereof for iron ore.

도 1은 종래의 분철광석의 유동층 환원로를 개략적으로 도시한 구조도1 is a structural diagram schematically showing a fluidized bed reduction furnace of a conventional iron ore

도 2는 종래의 3단 원추형 분철광석의 유동층식 환원장치를 나타내는 구성도Figure 2 is a block diagram showing a fluidized bed reduction device of a conventional three-stage cone-shaped iron ore

도 3은 본 발명에 부합되는 분철광석의 유동층식 환원장치의 일례를 나타내 는 구성도Figure 3 is a block diagram showing an example of a fluidized bed reduction device of the iron ore according to the present invention

* 도면의 주요 부분에 대한 부호의 설명 *Explanation of symbols on the main parts of the drawings

100...제 1유동층로 101...제 1가스공급구100 ... 1 fluidized bed furnace 101 ... 1st gas supply port

102...제 1가스분산판 103...제 1광석공급구102 first gas distributor 103 first ore supply port

104...제 1광석배출구 105...제 1가스배출구104 ... First Ore Outlet 105 ... First Gas Outlet

106...제 2가스공급구 108...제 2광석배출구106 Second Gas Supply Hole 108 Second Ore Outlet

112...제 2가스분산판 200...제 2유동층로112 Second gas dispersion plate 200 Second fluidized bed furnace

201...제 3가스공급구 202...제 3가스분산판201 ... 3rd gas supply port 202 ... 3rd gas distribution plate

203...제 2광석공급구 204...제 3광석배출구203 ... 2nd ore supply port 204 ... 3rd ore outlet

205...제 2가스배출구 300...제 3유동층로205 2nd gas outlet 300 ... 3rd fluidized bed furnace

301...제 4가스공급구 302...제 4가스분산판301 ... Fourth Gas Inlet 302 ... Fourth Gas Distributor

303...제 3광석공급구 304...제 4광석배출구303 3rd ore supply port 304 ... 4th ore outlet

305...제 3가스배출구 400...제 1사이클론305 ... 3rd gas outlet 400 ... 1st cyclone

500...제 2사이클론 600...제 3사이클론500 ... Second Cyclone 600 ... Third Cyclone

700...용융로700 ... melting furnace

이하, 본 발명에 대하여 설명한다.EMBODIMENT OF THE INVENTION Hereinafter, this invention is demonstrated.

본 발명은 분철광석이 공급되는 환원로에 환원가스를 공급하여 유동상태에서 분철광석을 환원하는 방법에 있어서,The present invention provides a method for reducing the iron ore in the flow state by supplying a reducing gas to the reducing furnace is supplied with iron ore,

원통형 대경 상부로(100A)와 소경 하부로(100B)로 이루어진 시리얼 트윈(serial twin)형 제1유동층로(100)의 하부로(100B)에 분철광석을 장입하고, 중/소립광석의 종말속도이상 대립광석의 종말속도 이하의 유속으로 상기 하부로(100B)의 저부에 환원가스를 공급하여 대립광석과 중/소립광석을 유동층로의 하부로(100B)와 상부로(100A)로에 각각 분급하여 대립광석은 유동층로의 하부로(100B)에서, 그리고 중/소립광석은 유동층로의 상부로(100A)에서, 하부로(100B)의 저부 및 상부로(100A)의 하부측벽을 통해 공급된 환원가스에 의해 예열 및 예비환원시키는 단계; 및The ferrite ore is charged into the lower furnace 100B of the serial twin type first fluidized bed furnace consisting of a cylindrical large diameter upper furnace 100A and a small diameter lower furnace 100B, and the terminal speed of the medium / small particle ore Supplying reducing gas to the bottom of the lower furnace (100B) at a flow rate less than or equal to the end speed of the allele ore to classify the allele and the medium / small ore to the lower (100B) and the upper (100A) of the fluidized bed furnace, respectively Allele ore is reduced at the bottom of the fluidized bed furnace (100B), and the medium / small particle ore is reduced at the top of the fluidized bed furnace (100A), through the bottom of the bottom (100B) and the bottom side wall of the upper furnace (100A) Preheating and pre-reducing with gas; And

상기에서 예열 및 예비환원된 중/소립광석은 하나의 상광하협의 원추형 유동층로(300)에서 최종 환원시키고, 그리고 예열 및 예비환원된 대립광석은 원통형 유동층로(200)에서 1차 환원시킨 다음 상기 상광하협의 유동층로(300)로 보내어 최종 환원시키는 단계를 포함하여 구성되는 분철광석의 유동층식 환원방법에 관한 것이다.The pre-heated and pre-reduced medium / small ore is finally reduced in the conical fluidized bed furnace 300 of one sub-angular narrow, and the pre-reduced and pre-reduced allelic ore is first reduced in a cylindrical fluidized bed 200 and then The present invention relates to a fluidized bed reduction method of ferrous ore comprising the step of sending to the fluidized bed (300) of the ordinary light strait.

또한, 본 발명은 분철광석의 유동층식 환원장치에 있어서, 원통형 대경상부로(100A)와 소경 하부로(100B)로 이루어져 장입된 분철광석중 대립광석은 하부로(100B)로, 중/소립광석은 상부로(100A)로 각각 분급하여 대립광석은 하부로(100B)에서, 중/소립광석은 상부로(100A)에서 환원성 분위기에 의해 예열 및 예비환원되도록 구성되는 시리얼 트윈(serial twin)형 제1유동층로(100);In addition, the present invention, in the fluidized bed reduction apparatus of the iron ore, the large ore of the iron ore of the charged iron ore consisting of a cylindrical large diameter upper furnace (100A) and a small diameter lower furnace (100B) to the lower (100B), medium / small ore The serial twin type agent is configured to be preheated and pre-reduced by a reducing atmosphere in the lower furnace 100B and the medium / small particle ore in the upper furnace 100A by classifying the silver into the upper furnace 100A. 1 fluidized bed furnace 100;

상기 제1 유동층로(100)에서 예열 및 예비환원된 대립광석을 1차 환원시키도록 구성되는 원통형의 제2유동층로(200);A cylindrical second fluidized bed furnace (200) configured to primarily reduce preheated and pre-reduced alleles in the first fluidized bed (100);

상기 제1유동층로(100)에서 예열 및 예비환원된 중/소립광석 및 제2유동층로(200)에서 1차 환원된 대립광석을 최종환원시키도록 구성되는 상광하협의 원추형인 제3유동층로(300);The third fluidized bed furnace, which is a conical shape of the Sangsang River Strait, configured to finally reduce the primary ore reduced mineral pre-heated and pre-reduced in the first fluidized bed furnace 100 and the second reduced allele ore in the second fluidized bed furnace 200 ( 300);

상기 제1 유동층로(100)의 배가스중에 함유된 미립광석을 포집하여 제1유동층로(100)의 상부측벽을 통해 제1유동층로(100)에 공급하고, 미립광석이 분리된 배가스는 외부로 배출하도록 구성되는 제1사이클론(400);The particulate ore contained in the exhaust gas of the first fluidized bed furnace 100 is collected and supplied to the first fluidized bed furnace 100 through the upper side wall of the first fluidized bed furnace 100, and the exhaust gas from which the fine ore is separated is discharged to the outside. A first cyclone 400 configured to be discharged;

상기 제2유동층로(200)의 배가스중에 함유된 미립광석을 포집하여 제2유동층로(200)의 측벽을 통해 제2유동층로(200)에 공급하고, 미립광석이 분리된 배가스는 환원가스로서 제1유동층로(100)에 공급되도록 구성되는 제2사이클론(500); 및The particulate ore contained in the exhaust gas of the second fluidized bed furnace 200 is collected and supplied to the second fluidized bed furnace 200 through the sidewall of the second fluidized bed furnace 200, and the exhaust gas from which the fine ore is separated is a reducing gas. A second cyclone 500 configured to be supplied to the first fluidized bed furnace 100; And

상기 제3유동층로(300)의 배가스중에 함유된 미립광석을 포집하여 제3유동층로(300)의 측벽을 통해 제3유동층로(300)에 공급하고, 미립광석이 분리된 배가스는 환원가스로서 제1유동층로(100)에 공급되도록 구성되는 제3사이클론(600)을 포함하여 구성되는 분철광석의 유동층식 환원장치에 관한 것이다.The particulate ore contained in the exhaust gas of the third fluidized bed 300 is collected and supplied to the third fluidized bed 300 through the side wall of the third fluidized bed 300, and the exhaust gas from which the fine ore is separated is a reducing gas. The present invention relates to a fluidized bed reduction apparatus for iron ore including a third cyclone (600) configured to be supplied to the first fluidized bed (100).

이하, 도 3을 참고로 하여, 본 발명에 대하여 상세히 설명한다.Hereinafter, the present invention will be described in detail with reference to FIG. 3.

본 발명에 따라 분철광석을 유동층식 환원장치에서 환원하기 위해서는, 원통형 대경 상부로(100A)와 소경 하부로(100B)로 이루어진 시리얼 트윈(serial twin)형 제1유동층로(100)의 하부로(100B)에 분철광석을 장입하고, 중/소립광석의 종말속도이상 대립광석의 종말속도 이하의 유속으로 상기 하부로(100B)의 저부에 환원가스를 공급하여 대립광석과 중/소립광석을 유동층로의 하부로(100B)와 상부로(100A)로에 각각 분급하여 대립광석은 유동층로의 하부로(100B)에서, 그리고 중/소립광석은 유동층로의 상부로(100A)에서, 하부로(100B)의 저부 및 상부로(100A)의 하부측벽을 통해 공급된 환원가스에 의해 예열 및 예비환원시킨다.In order to reduce the iron ore in the fluidized bed reduction apparatus according to the present invention, to the lower portion of the serial twin type first fluidized bed (100) consisting of a cylindrical large diameter upper path (100A) and a small diameter lower path (100B) ( Charged iron ore into 100B), supplying reducing gas to the bottom of the lower furnace (100B) at a flow rate equal to or greater than the terminal velocity of the medium or small ore and less than the terminal velocity of the allele. Are classified into the lower furnace (100B) and the upper furnace (100A), respectively, so that the opposing ore is at the bottom of the fluidized bed (100B), and the medium / small ore is at the top of the fluidized bed (100A), and the lower (100B). It is preheated and pre-reduced by the reducing gas supplied through the bottom and the lower side wall of the upper furnace (100A).

다음에, 상기에서 예열 및 예비환원된 중/소립광석은 하나의 상광하협의 원추형 유동층로(300)에서 최종 환원시키고, 그리고 예열 및 예비환원된 대립광석은 원통형 유동층로(200)에서 1차 환원시킨 다음 상기 상광하협의 유동층로(300)로 보내어 최종 환원시킨다.Next, the pre-heated and pre-reduced medium / small ore is finally reduced in the conical fluidized bed furnace 300 of one upper and lower subsoils, and the pre-heated and pre-reduced allele is reduced first in the cylindrical fluidized bed furnace 200. And then sent to the fluidized bed (300) of the Sangsangha River is finally reduced.

상기 시리얼 트윈(serial twin)형 제1유동층로(100)에서의 예열 및 예비환원온도는 700 ~ 800℃로, 그리고 원통형 유동층로(200)와 원추형 유동층로(300)에서의 1차환원과 최종환원온도는 750 ~ 900℃로 선정함이 바람직하다.The preheating and pre-reduction temperatures in the serial twin first fluidized bed reactor (100) are 700 to 800 ° C., and the primary and final reduction in the cylindrical fluidized bed (200) and conical fluidized bed (300). The reduction temperature is preferably selected to 750 ~ 900 ℃.

또한, 조업압력은 절대압으로 2 ~ 6기압으로 선정함이 바람직한데, 이는 일반적으로 조업압력이 커질수록 환원반응속도는 빨라지나 최소유동화속도는 감소하므로 이를 고려한 것이다.In addition, it is preferable to select the operating pressure of 2 to 6 atm as the absolute pressure, which is generally considered as the reduction reaction speed increases but the minimum fluidization rate decreases as the operating pressure increases.

또한, 상기 시리얼 트윈(serial twin)형 제1유동층로(100)와 원추형 유동층로(300)내에서의 광석체류시간은 30 ~ 60분으로, 그리고 원통형 유동층로(200)내에서의 광석체류시간은 10 ~ 40분으로 선정함이 바람직한데, 이는 분철광석의 최적의 환원성 확보를 위함이다.In addition, the ore residence time in the serial twin first fluidized bed furnace 100 and the conical fluidized bed furnace 300 is 30 to 60 minutes, and the ore residence time in the cylindrical fluidized bed furnace 200. Is preferably selected from 10 to 40 minutes, in order to ensure optimal reducibility of the iron ore.

이하, 본 발명의 바람직한 분철광석의 유동층식 환원장치에 대하여 설명한다.Hereinafter, the fluidized bed reduction apparatus of the preferred iron ore of the present invention will be described.

도3에 나타난 바와 같이, 본 발명의 분철광석 유동층식 환원장치는, 원통형의 대경 상부로(100A)와 소경 하부로(100B)로 이루어져 장입된 분철광석중 대립광석은 하부로(100B)로, 중/소립광석은 상부로(100A)로 각각 분급하여 대립광석은 하부로(100B)에서, 중/소립광석은 상부로(100A)에서 환원성 분위기에 의해 예열 및 예비환원되도록 구성되는 시리얼 트윈(serial twin)형 제1유동층로(100);As shown in Figure 3, the iron-iron ore fluidized bed reduction apparatus of the present invention, the large ore of the iron-iron ore of the charged iron ore is composed of a cylindrical large diameter upper furnace (100A) and a small diameter lower furnace (100B) to the lower (100B), The medium / small ore is classified into the upper furnace (100A), so that the opposing ore is in the lower furnace (100B), the medium / small ore is in the upper furnace (100A), the serial twin is configured to be preheated and reduced by a reducing atmosphere. twin) first fluidized bed (100);

상기 제1유동층로(100)에서 예열 및 예비환원된 중/소립광석 및 제2유동층로(200)에서 1차 환원된 대립광석을 최종환원시키도록 구성되는 제3유동층로(300);A third fluidized bed furnace 300 configured to finally reduce the primary / reduced small ore minerals preheated and pre-reduced in the first fluidized bed furnace 100 and the first reduced allele ore in the second fluidized bed furnace 200;

상기 제1 유동층로(100)의 배가스중에 함유된 미립광석을 포집하여 제1유동층로(100)의 상부 측벽을 통해 제1유동층로(100)에 공급하고, 미립광석이 분리된 배가스는 외부로 배출하도록 구성되는 제1사이클론(400);The fine ore contained in the exhaust gas of the first fluidized bed furnace 100 is collected and supplied to the first fluidized bed furnace 100 through the upper sidewall of the first fluidized bed furnace 100, and the exhaust gas from which the fine ore is separated is discharged to the outside. A first cyclone 400 configured to be discharged;

상기 제3유동층로(300)의 배가스중에 함유된 미립광석을 포집하여 제3유동층로(300)의 측벽을 통해 제3유동층로(300)에 공급하고, 미립광석이 분리된 배가스는 환원가스로서 제1유동층로(100)에 공급되도록 구성되는 제3사이클론(600)을 포함하여 구성된다.The particulate ore contained in the exhaust gas of the third fluidized bed 300 is collected and supplied to the third fluidized bed 300 through the side wall of the third fluidized bed 300, and the exhaust gas from which the fine ore is separated is a reducing gas. It is configured to include a third cyclone 600 is configured to be supplied to the first fluidized bed (100).

상기 제 1유동층로(100)는 원통형의 대경 상부로(100A)와 소경 하부로(100B)로 이루어지며, 상기 하부로(100B)의 저부에는 환원가스를 공급받기 위한 제1 가스공급구(101)이 형성되어 있고, 이 제1 가스공급구(101)에는 제1 유동층로(100)의 하부로(100B)로 가스를 도입하기 위한 제12 도관(604)이 연결되어 있고, 그리고 상기 하부로(100B)의 하부내에는 제1 가스공급구(101)를 통해 공급되는 가스를 분산시키기 위한 제 1가스분산판(102)이 내장되어 있으며, 이 제 1가스분산판(102)으로는 평판(flat)형이 바람직하다.The first fluidized bed furnace 100 is composed of a cylindrical large diameter upper furnace 100A and a small diameter lower furnace 100B, and a first gas supply port 101 for receiving a reducing gas at the bottom of the lower furnace 100B. Is formed, and the first gas supply port 101 is connected to a twelfth conduit 604 for introducing gas into the lower portion 100B of the first fluidized bed passage 100 and to the lower portion. In the lower portion of 100B, a first gas distribution plate 102 for dispersing the gas supplied through the first gas supply port 101 is incorporated, and the first gas distribution plate 102 includes a flat plate ( flat) type is preferred.

또한, 상기 하부로(100B)의 측벽에는 분철광석을 공급받기 위한 제 1광석공급구(103) 및 예열/예비환원된 대립광석을 배출하기 위한 제 2광석배출구(108)가 형성되어 있고, 상기 제 2광석배출구(108)는 제 1광석공급구(103)보다 위에 형성된다,In addition, the lower side (100B) of the side wall is formed with a first ore supply port 103 for supplying the iron ore and a second ore outlet 108 for discharging the preheated / pre-reduced allel ore, The second ore outlet 108 is formed above the first ore supply port 103,

상기 제 2광석배출구(108)는 제2도관(107)을 통해 제2 유동층로(200)의 하부와 광석소통관계로 연결되어 있으며, 상기 제1광석공급구(103)는 광석공급관(111)을 통해 광석공급원(도시되어 있지 않음)에 연결되어 있다.The second ore outlet 108 is connected to the lower portion of the second fluidized bed 200 through the second conduit 107 in an ore communication relationship, and the first ore supply port 103 is an ore supply pipe 111. Through an ore source (not shown).

한편, 상기 하부로(100B)의 상부내에는 가스유속을 증가시키기 위한 리듀싱 핀(reducing fin)(110)을 구비시키는 것이 바람직하다.On the other hand, it is preferable to include a reducing fin (110) to increase the gas flow rate in the upper portion of the lower passage (100B).

상기 상부로(100A)의 하부측벽에는 환원가스를 공급받기 위한 제2 가스공급구(106)이 형성되어 있고, 이 제2 가스공급구(106)에는 가스를 도입하기 위한 제13 도관(605)이 연결되어 있고, 그리고 상기 상부로(100A)의 하부내에는 제2 가스공급구(106)를 통해 공급되는 가스를 분산시키기 위한 원추형의 제2 가스분산판(112)이 내장되어 있다.A second gas supply hole 106 for receiving a reducing gas is formed in the lower side wall of the upper passage 100A, and the second gas supply hole 106 has a thirteenth conduit 605 for introducing gas. The second gas distribution plate 112 of a conical shape for dispersing the gas supplied through the second gas supply port 106 is embedded in the lower portion of the upper passage 100A.

또한, 상기 상부로(100A)의 측벽에는 예열/예비환원된 중립/소립광석을 배출하기 위한 제1 광석배출구(104)가 형성되어 있으며, 이 제1 광석배출구(104)는 제1 도관(109) 및 제14 도관(209)을 통해 제3 유동층로(300)의 하부와 광석소통관계로 연결되어 있다.In addition, a first ore outlet 104 for discharging preheated / pre-reduced neutral / small ore is formed on the side wall of the upper passage 100A, and the first ore outlet 104 is a first conduit 109. And the 14th conduit 209 are connected to the lower part of the third fluidized bed 300 in an ore communication relationship.

상기 상부로(100A)의 정부에는 배가스를 배출하기 위한 제1 가스배출구(105)가 형성되어 있으며, 이 제1 가스배출구(105)는 제3도관(113)을 통해 제1 사이클론(400)과 연결되어 있다.The first gas outlet 105 for discharging exhaust gas is formed at the top of the upper passage 100A, and the first gas outlet 105 is connected to the first cyclone 400 through the third conduit 113. It is connected.

상기 제1 사이클론(400)에는 미립광석이 분리된 배가스를 외부로 배출하기 위한 제6도관(402)이 연결되어 있고, 포집된 미립광석을 상기 제1 유동층로(100)내로 공급하기 위한 제4도관(401)이 연결되어 있으며, 이 제4도관(401)은 그 일단이 제1유동층로(100)의 상부로(100A)내부 깊숙이 위치되도록 하는 것이 바람직하다.The first cyclone 400 is connected with a sixth conduit 402 for discharging the exhaust gas from which the fine ore is separated to the outside, and a fourth for supplying the collected fine ore into the first fluidized bed furnace 100. The conduit 401 is connected, and the fourth conduit 401 is preferably such that one end thereof is located deep inside the upper passage 100A of the first fluidized bed 100.

상기 제1 유동층로의 상부로(100A)의 높이는 그 내경의 3~7배로, 그리고 하부로(100B)의 높이는 그 내경의 15~25배로 형성하는 것이 바람직하다.The height of the upper passage 100A of the first fluidized bed passage is preferably 3 to 7 times the inner diameter, and the height of the lower passage 100B is 15 to 25 times the inner diameter.

상기 제2 유동층로(200)의 저부에는 환원가스를 공급받기 위한 제3 가스공급구(201)이 형성되어 있고, 상기 제2유동층로(200)의 하부내에는 제3 가스공급구(201)를 통해 공급되는 가스를 분산시키기 위한 제3 가스분산판(202)이 내장되어 있으며, 이 제2 가스분산판(202)으로는 평판(flat)형이 바람직하다.A third gas supply hole 201 is formed at a bottom of the second fluidized bed furnace 200 to receive a reducing gas, and a third gas supply hole 201 is provided in a lower part of the second fluidized bed furnace 200. A third gas distribution plate 202 is built in to disperse the gas supplied through the gas, and a flat type is preferable as the second gas distribution plate 202.

또한, 상기 제2유동층로(200)의 측벽에는 상기 제1 유동층로(100)의 하부로(100B)에서 예열/예비환원된 광석을 공급받기 위한 제2광석공급구(203) 및 1차 최종환원된 대립광석을 배출하기 위한 제3 광석배출구(204)가 형성되어 있다.In addition, the second ore supply port 203 and the first final end to receive the preheated / pre-reduced ore in the lower passage (100B) of the first fluidized bed (100) on the side wall of the second fluidized bed (200) A third ore outlet 204 for discharging the reduced allele ore is formed.

상기 제2 광석공급구(203)는 제2 도관(107)을 통해 상기 제1 유동층로(100)의 하부로(100B)의 제2 광석배출구(108)에 연통되어 있고, 그리고 상기 제3 광석배출구(204)는 제10 도관(207)을 통해 제3 유동층로(300)의 하부와 광석소통관계로 연결되어 있다.The second ore supply port 203 is in communication with the second ore outlet 108 in the lower portion 100B of the first fluidized bed passage 100 through the second conduit 107, and the third ore The outlet 204 is connected to the lower portion of the third fluidized bed 300 in the ore communication relationship through the tenth conduit 207.

또한, 상기 제2 유동층로(200)의 측벽에는 상기 제2 사이클론(500)에서 배가스로 부터 분리된 미립광석을 공급받기 위한 미립광석 공급구(208)가 형성되어 있다.In addition, a particulate ore supply port 208 is formed on a sidewall of the second fluidized bed 200 to receive particulate ore separated from the exhaust gas in the second cyclone 500.

상기 제2 유동층로(200)의 정부에는 배가스를 배출하기 위한 제2 가스배출구(205)가 형성되어 있으며, 이 제2 가스배출구(205)는 제8도관(206)을 통해 제2 사이클론(500)과 연결되어 있다.A second gas outlet 205 for discharging exhaust gas is formed at the government of the second fluidized bed furnace 200, and the second gas outlet 205 is connected to the second cyclone 500 through the eighth conduit 206. )

상기 제2 사이클론(500)에는 미립광석이 분리된 배가스를 외부로 배출하기 위한 제7도관(502)이 연결되어 있고, 포집된 미립광석을 상기 제2 유동층로(200)내로 공급하기 위한 제9도관(501)이 연결되어 있으며, 이 제9도관(501)은 그 일단이 제2 유동층로(200)의 미립광석 공급구(208)에 연결되어 있다.The second cyclone 500 is connected to the seventh conduit 502 for discharging the exhaust gas from which the fine ore is separated to the outside, the ninth for supplying the collected fine ore into the second fluidized bed 200 A conduit 501 is connected, one end of which is connected to the particulate ore supply port 208 of the second fluidized bed 200.

본 발명에 있어 바람직하게는, 상기 제7도관(502)으로부터 배출되는 제2 유동층로(200)의 청청 배가스는 상기 제1 유동층로(100)의 상부로(100A)의 하부 측벽에 형성되어 있는 제2 가스공급구(106)를 통해 상부로(100A)내로 공급하여 환원가스로 사용되도록 하는 것이 바람직하다.In the present invention, preferably, the blue exhaust gas of the second fluidized bed furnace 200 discharged from the seventh conduit 502 is formed on the lower sidewall of the upper furnace 100A of the first fluidized bed furnace 100. It is preferable to supply the gas into the upper path 100A through the second gas supply port 106 to be used as the reducing gas.

상기 제 2유동층로(200)의 높이는, 그 내경의 15~25배로 형성함이 바람직하다.The height of the second fluidized bed 200 is preferably formed to be 15 to 25 times the inner diameter.

상기 제3 유동층로(300)는 원통형 상부(300A)와 원추형 하부(300B)로 이루어지고, 그 저부에는 환원가스를 공급받기 위한 제4 가스공급구(301)이 형성되어 있고, 상기 제3 유동층로(300)의 하부내에는 제4 가스공급구(301)를 통해 공급되는 가스를 분산시키기 위한 제4 가스분산판(302)이 내장되어 있으며, 이 제4 가스분산판(302)으로는 평판(flat)형이 바람직하다.The third fluidized bed 300 is formed of a cylindrical upper portion 300A and a conical lower portion 300B, and a fourth gas supply port 301 for receiving a reducing gas is formed at a bottom thereof, and the third fluidized layer A fourth gas distribution plate 302 for dispersing the gas supplied through the fourth gas supply port 301 is built in the lower portion of the furnace 300, and the fourth gas distribution plate 302 includes a flat plate. (flat) type is preferable.

또한, 상기 제3 유동층로(300)의 측벽에는 상기 제1 유동층로(100)의 상부로(100A)에서 예열/예비환원된 중/소립광석과 상기 제2 유동층로(200)에서 1차 최종환원된 대립광석을 공급받기 위한 제3 광석공급구(303) 및 최종환원된 광석을 배출하기 위한 제4 광석배출구(304)가 형성되어 있다.In addition, the side wall of the third fluidized bed furnace 300 has a primary final in the pre-heated / pre-reduced medium / small ore and the second fluidized bed furnace 200 in the upper passage (100A) of the first fluidized bed furnace (100) A third ore supply port 303 for receiving the reduced allele ore and a fourth ore discharge port 304 for discharging the finally reduced ore are formed.

상기 제3 광석공급구(303)는 제14 도관(209) 및 제1 도관(109)을 통해 상기 제1 유동층로(100)의 상부로(100A)의 제1 광석배출구(104)에 연통되어 있고, 그리고 제14 도관(209) 및 제10 도관(207)을 통해 제3 광석배출구(204)에 연통되어 있다.The third ore supply port 303 communicates with the first ore outlet 104 of the upper passage 100A of the first fluidized bed passage 100 through the fourteenth conduit 209 and the first conduit 109. And a third ore discharge port 204 through a fourteenth conduit 209 and a tenth conduit 207.

상기 제4 광석배출구(304)에는 제16 도관(307)이 연결되어 있다.A sixteenth conduit 307 is connected to the fourth ore outlet 304.

상기 제3 유동층로(300)의 정부에는 배가스를 배출하기 위한 제3 가스배출구(305)가 형성되어 있으며, 이 제3 가스배출구(305)는 제15 도관(306)을 통해 제3 사이클론(600)과 연결되어 있다.The third gas outlet 305 for discharging the exhaust gas is formed at the government of the third fluidized bed furnace 300, and the third gas outlet 305 is connected to the third cyclone 600 through the fifteenth conduit 306. )

상기 제3유동층로(300) 원추형 하부(300B)의 가스분산판(302)에서부터의 높이는 그 하부 가스분산판 내경의 3~7배, 원통형 상부(300A)의 높이는 그 내경의 2~5배, 원추형 하부(300B)의 경사각은 수직선에서 5~20°로 함이 바람직한데, 이는 각 환원로내에 장입된 분철광석의 적정한 유동성 확보를 도모하고 분철광석의 비산을 막기 위함이다.The height from the gas distribution plate 302 of the conical lower portion 300B of the third fluidized bed 300 is 3 to 7 times the inner diameter of the lower gas distribution plate, the height of the cylindrical upper portion 300A is 2 to 5 times the inner diameter, The inclination angle of the conical lower portion 300B is preferably 5 to 20 ° from the vertical line, in order to ensure proper fluidity of the iron ore charged in each reduction furnace and to prevent the scattering of the iron ore.

상기 제3 사이클론(600)에는 미립광석이 분리된 배가스를 외부로 배출하기 위한 제11 도관(602)이 연결되어 있고, 포집된 미립광석을 상기 제3 유동층로(300)내로 공급하기 위한 제17 도관(601)이 연결되어 있으며, 이 제17 도관(601)은 그 일단이 제3 유동층로(300)의 내부 깊숙히 위치되도록 하는 것이 바람직하다.The third cyclone 600 is connected with an eleventh conduit 602 for discharging the exhaust gas from which the fine ore is separated to the outside, and the seventeenth for supplying the collected fine ore into the third fluidized bed 300. Conduit 601 is connected, and this seventeenth conduit 601 is preferably such that its one end is located deep inside the third fluidized bed passage (300).

본 발명에 있어 바람직하게는, 상기 제11 도관(602)으로부터 배출되는 제3 유동층로(300)의 청청 배가스는 상기 제1 유동층로(100)의 상부로(100A)의 하부 측벽에 형성되어 있는 제2 가스공급구(106) 및 하부로(100B)의 저부에 형성되어 있는 제1 가스공급구(101)를 통해 제1유동층로(100)내로 공급하여 환원가스로 사용되도록 하는 것이 바람직하다.In the present invention, preferably, the blue exhaust gas of the third fluidized bed furnace 300 discharged from the eleventh conduit 602 is formed on the lower sidewall of the upper furnace 100A of the first fluidized bed furnace 100. The first gas supply port 101 formed at the bottom of the second gas supply port 106 and the lower passage 100B may be supplied into the first fluidized bed furnace 100 to be used as a reducing gas.

한편, 상기와 같이 제2 유동층로(200)의 청청 배가스를 제1 유동층로(100)의 환원가스로 사용하기 위해서는, 제7 도관(502)을 상기 제13 도관(605)에 연통 되도록하는 것이 바람직하다.On the other hand, in order to use the blue and blue flue gas of the second fluidized bed furnace 200 as the reducing gas of the first fluidized bed furnace 100 as described above, it is to ensure that the seventh conduit 502 is in communication with the thirteenth conduit 605. desirable.

그리고, 상기 제2 유동층로(200) 및 제3 유동층로(300)의 환원가스로는 용융가스화로(700)의 배가스를 이용하는 것이 바람직하다.In addition, as the reducing gas of the second fluidized bed furnace 200 and the third fluidized bed furnace 300, it is preferable to use exhaust gas of the molten gasifier 700.

상기와 같이, 용융가스화로(700)의 배가스를 환원가스로 사용하기 위해서는, 상기 용융가스화로(700)의 상부에 제19 도관(701)을 구비시키고, 그리고 제2 유동층로(200)에 가스를 공급하는 제20 도관(702)와 제3 유동층로(300)에 가스를 공급하는 제21 도관(703)을 상기 제19 도관(701)에 연통되도록 한다.As described above, in order to use the exhaust gas of the molten gasifier 700 as the reducing gas, the nineteenth conduit 701 is provided on the upper part of the molten gasifier 700, and the gas is provided in the second fluidized bed furnace 200. The twenty-first conduit 702 for supplying gas and the twenty-first conduit 703 for supplying gas to the third fluidized bed passage 300 may communicate with the nineteenth conduit 701.

그리고, 도3에 나타난 바와 같이, 상기 제16 도관(307)를 용융가스화로(700)에 연통 되도록 하여 제3 유동층로(300)에서 최종환원된 광석을 용융가스화로(700)에 투입되도록 할 수도 있다.As shown in FIG. 3, the sixteenth conduit 307 communicates with the melt gasifier 700 so that the finally reduced ore from the third fluidized bed furnace 300 is introduced into the melt gasifier 700. It may be.

또한, 상기 제3 유동층로(300)의 청정 배가스를 제1 유동층로(100)의 환원가스로 사용하기 위해서는, 제1 가스공급구(101)에 연통되어 제1 유동층로(100)의 하부로(100B)에 가스를 공급하는 제12 도관(604)과 제2 가스공급구(106)에 연통되어 제1 유동층로(100)의 상부로(100A)에 가스를 공급하는 제13 도관(605)이 상기 제11 도관(602)과 연통되도록 해야한다.In addition, in order to use the clean exhaust gas of the third fluidized bed furnace 300 as the reducing gas of the first fluidized bed furnace 100, it is communicated with the first gas supply port 101 to the lower portion of the first fluidized bed furnace 100. A thirteenth conduit 605 in communication with the twelfth conduit 604 for supplying gas to the 100B and the second gas supply port 106 for supplying gas to the upper passage 100A of the first fluidized bed passage 100. This should be in communication with the eleventh conduit 602.

이하, 본 발명의 바람직한 환원방법을 상기한 분철광석의 유동층식 환원장치(첨부도면)를 이용하여 설명한다.Hereinafter, the preferred reduction method of the present invention will be described using the fluidized bed reduction apparatus (attached drawing) of the above-described ferrous ore.

도 3에 나타난 바와 같이, 제 3사이클론(600)으로부터 공급되는 배가스(환원가스)가 제 1유동층로(100)의 하부로(100B)의 제 1가스공급구(101)로 중/소립의 종말속도 이상 그리고 대립의 종말속도 이하의 적정 유동화속도로 공급되면서 제 1유동층로 (100)의 하부로(100B)의 제1 광석공급구(103)로 원료 분철광석이 장입되면, 구경의 차이에 의하여 제 1유동층로의 대경 상부로(100A)가 그 소경 하부로(100B)보다 그 환원가스유속이 느려지게 된다.As shown in FIG. 3, the exhaust gas (reduction gas) supplied from the third cyclone 600 is the end of the medium / small particles to the first gas supply port 101 of the lower path 100B of the first fluidized bed 100. When the raw iron ore is charged into the first ore supply port 103 in the lower portion 100B of the first fluidized bed passage 100 while being supplied at an appropriate fluidization speed above the speed and below the end speed of the opposition, The reducing gas flow rate of the large diameter upper path 100A of the first fluidized bed furnace is lower than that of the small diameter lower path 100B.

따라서 제 1유동층로(100)에서는, 대립의 분철광석은 가스유속이 빠른 그 소경 하부로(100B)에서 기포유동층 상태를 형성하면서 예열 및 예비환원되어 제 2광석배출구(108)를 통해 제 2유동층로(200)로 공급되고, 중/소립의 분철광석이나 제 1사이클론(400)에서 집진되어 재 장입된 극미립철광석은 가스유속이 느린 그 대경 상부(100A)에서 기포유동층 상태를 형성하면서 예열 및 예비환원되어 제 1광석배출구(104)를 통하여 제 3유동층로(300)에 공급된다.Therefore, in the first fluidized bed (100), the opposing iron ore is preheated and pre-reduced while forming a bubble fluidized bed state at the small diameter lower path (100B) having a high gas flow rate, so that the second fluidized bed is passed through the second ore outlet (108). The ultra-fine iron ore supplied to the furnace 200 and collected in the medium / small grained iron ore or the first cyclone 400 is reheated while forming a bubble fluidized bed state at a large diameter upper portion 100A having a low gas flow rate. It is preliminarily reduced and supplied to the third fluidized bed furnace 300 through the first ore outlet 104.

그리고 제 2유동층로(200)에서는, 제 1유동층로(100)의 소경 하부로(100B)에서 예열·예비환원되어 제 2광석공급구(203)를 통하여 공급되는 대립의 분철광석과 제 2사이클론(500)에서 집진되어 재장입된 극미립철광석이 제 3가스공급구(201)를 통해 공급되는 용융로(700)의 배가스(환원가스)에 의하여 기포유동층 상태를 형성하면서 1차환원되어 제 3광석배출구(204)를 통하여 제 3유동층로(300)에 공급된다. 제 3유동층로(300)에서는, 제 3광석공급구(303)를 통하여 공급되는 제 1유동층로 대경 상부(100A)에서 예열·예비환원된 중/소립의 분철광석과 제 2유동층로(200)에서 1차환원된 대립의 분철광석 및 제3 사이클론(600)에서 집진되어 재 장입되는 극미립철광석이 제 4가스공급구(301)를 통하여 공급되는 용융로(700)의 배가스(환원가스)에 의해 기포유동층 상태를 형성하면서 최종환원되어, 제 4광석배출구(304)를통하여 용융로(700)에 장입된다.In the second fluidized bed furnace 200, the opposing iron ore and the second cyclone are preheated and pre-reduced in the small diameter lower path 100B of the first fluidized bed furnace 100 and supplied through the second ore supply port 203. The ultrafine iron ore collected and reloaded at 500 is first reduced while forming a bubble fluidized bed state by exhaust gas (reduction gas) of the melting furnace 700 supplied through the third gas supply port 201 to the third ore. It is supplied to the third fluidized bed 300 through the outlet 204. In the third fluidized bed 300, the first fluidized bed furnace supplied through the third ore supply port 303, the pre-reduced and pre-reduced medium / small sized iron ore and the second fluidized bed 200 in the large diameter (100A) By the flue-gas (reduction gas) of the melting furnace 700 is supplied through the fourth gas supply port 301, the primary iron ore of the reduced allele and the fine iron ore that is collected and reloaded in the third cyclone (600) at Final reduction is performed while forming a bubble fluidized bed state, and charged into the melting furnace 700 through the fourth ore discharge port 304.

용융로(700)에서는 제 3유동층로(300)로부터 공급받은 최종환원된 분철광석이 선철 내지 용강으로 직접 제조 될 수 있다.In the melting furnace 700, the final reduced iron ore supplied from the third fluidized bed furnace 300 may be directly manufactured from pig iron or molten steel.

상기 제1 유동층로(100)에서의 예열 및 예비환원온도는 700 ~ 800℃, 제 2유동층로(200)와 제 3유동층로(300)에서의 1차환원과 최종환원온도는 750 ~ 900℃로 선정함이 바람직하다.Preheating and pre-reduction temperatures in the first fluidized bed (100) is 700 ~ 800 ℃, primary and final reduction temperature in the second fluidized bed 200 and the third fluidized bed (300) is 750 ~ 900 ℃ Is preferably selected.

또한, 조업압력은 절대압으로 2 ~ 6기압하에 행함이 바람직한데, 이는 일반적으로 조업압력이 커질수록 환원반응속도는 빨라지나 최소유동화속도는 감소하므로 이를 고려한 것이다.In addition, the operating pressure is preferably carried out under 2 to 6 atm as the absolute pressure, which is generally considered as the reduction reaction rate is faster but the minimum fluidization rate is reduced as the operating pressure is increased.

또한, 상기 제1 유동층로(100)와 제3 유동층로(300)내에서의 광석체류시간은 30 ~ 60분, 제 2유동층로(200)내에의 광석체류시간은 10 ~ 40분으로 선정함이 바람직한데, 이는 분철광석의 최적의 환원성 확보를 위함이다.In addition, the ore residence time in the first fluidized bed furnace 100 and the third fluidized bed furnace 300 is 30 to 60 minutes, the ore residence time in the second fluidized bed furnace 200 is selected from 10 to 40 minutes. This is preferable, in order to ensure the optimal reduction of the iron ore.

또한, 제1 유동층로(100)의 대경 상부로(100A)와 제3 유동층로(300)의 가스분산판 바로 위에서의 가스유속은, 로내에 체류하는 분철광석의 최소유동화속도의 1.2 ~ 2.5배 이하가 되도록 선정함이 바람직하며, 제 1유동층로(100)의 소경 하부로(100B)와 제 2유동층로(200)의 가스분산판 바로 위에서의 가스유속은 로내에 체류하는 분철광석의 최소유동화속도의 1.5 ~ 3.0배로 유지함이 바람직한데, 그 이유는In addition, the gas flow rate just above the gas distribution plate of the large diameter upper path 100A of the first fluidized bed furnace 100 and the third fluidized bed furnace 300 is 1.2 to 2.5 times the minimum fluidization rate of the iron ore staying in the furnace. Preferably, the gas flow rate just above the gas dispersion plate of the small diameter lower path 100B and the second fluidized bed furnace 200 of the first fluidized bed furnace 100 is the minimum fluidization of the iron ore staying in the furnace. It is desirable to keep it at 1.5 to 3.0 times the speed because

원활한 유동 및 비산량의 최소화를 도모하기 위함이다.This is to minimize the flow and scattering smoothly.

이하, 본 발명을 실시예를 통하여 보다 상세히 설명한다.Hereinafter, the present invention will be described in more detail with reference to Examples.

(실시예)(Example)

비교예Comparative example

하기 표1과 같은 크기를 갖는 도 2에 도시된 바와 같은 종래의 원추형 3단 유동층식 환원장치를 이용하여, 하기 표2 - 표4에 제시된 조건으로 환원을 행하고, 입도별 최종 환원률을 조사하고, 그 결과를 하기 표5에 나타내었다.Using a conventional conical three-stage fluidized bed reduction apparatus as shown in Figure 2 having the same size as Table 1 below, the reduction is performed under the conditions shown in Table 2 to Table 4, and the final reduction rate by particle size is investigated. The results are shown in Table 5 below.

유동층 환원로의 높이 및 내경Height and Internal Diameter of Fluidized Bed Reduction Furnace 제1유동층로First fluidized bed 원추형 하부(분산판) 내경 : 0.63 m원추형 하부 경사각도 : 5°원추부 하부 높이(분산판 표면에서) : 3 m원통형 상부 내경 : 1.15 m원통형 상부 높이 : 3.5 mConical lower part (distribution plate) Inner diameter: 0.63 m Conical lower inclination angle: 5 ° Cone lower part height (on the surface of the distributing plate): 3 m Cylindrical upper inner diameter: 1.15 m Cylindrical upper height: 3.5 m 제 2유동층로Second fluidized bed 원통형 하부(분산판) 내경 : 0.63 m원추형 하부 경사각도 : 5°원추부 하부 높이(분산판 표면에서) : 3 m원통형 상부 내경 : 1.15 m원통형 상부 높이 : 3.5 mCylindrical lower part (distribution plate) Inner diameter: 0.63 m Conical lower inclination angle: 5 ° Cone lower part height (on the surface of the distributing plate): 3 m Cylindrical upper inner diameter: 1.15 m Cylindrical upper height: 3.5 m 제3유동층로Third fluidized bed 원추형 하부(분산판) 내경 : 0.63 m원추형 하부 경사각도 : 5°원추부 하부 높이(분산판 표면에서) : 3 m원통형 상부 내경 : 1.15 m원통형 상부 높이 : 3.5 mConical lower part (distribution plate) Inner diameter: 0.63 m Conical lower inclination angle: 5 ° Cone lower part height (on the surface of the distributing plate): 3 m Cylindrical upper inner diameter: 1.15 m Cylindrical upper height: 3.5 m

원료 분철광석의 화학적 성분 및 입도분포Chemical Composition and Particle Size Distribution of Raw Iron Powders 화학적 조성Chemical composition T.Fe:62.17%,FeO:0.51%,SiO₂:5.5%,TiO₂:0.11%,Mn:0.05%,S:0.012%, P: 0.65%, 결정수: 2.32T.Fe: 62.17%, FeO: 0.51%, SiO ₂ : 5.5%, TiO ₂ : 0.11%, Mn: 0.05%, S: 0.012%, P: 0.65%, Crystalline number: 2.32 입도 분포Particle size distribution -0.125 ㎜: 16.4%, 0.125 ~ 0.25 ㎜: 12.7%0.25 ㎜ ~ 0.5 ㎜: 6.9%, 0.5 ~ 1.0 ㎜: 9.5%1.0 ~ 2.8 ㎜: 18.5%, 2.8 ~ 4.0 ㎜: 12.5%4.0 ~ 4.75㎜: 8.7%, 4.75 ~ 8 ㎜: 14.8%0.125 mm: 16.4%, 0.125 to 0.25 mm: 12.7% 0.25 mm to 0.5 mm: 6.9%, 0.5 to 1.0 mm: 9.5% 1.0 to 2.8 mm: 18.5%, 2.8 to 4.0 mm: 12.5% 4.0 to 4.75 mm: 8.7%, 4.75-8 mm: 14.8%

환원가스 성분, 온도 및 압력Reducing gas component, temperature and pressure 가스조성Gas composition CO:65%, H₂:25%, CO₂:5%, N₂:5%CO: 65%, H ₂ : 25%, CO ₂ : 5%, N ₂ : 5% 온 도Temperature 예열 : 약 750℃예비환원 : 약 800℃최종환원 : 약 850℃Preheating: about 750 ° C Preliminary reduction: about 800 ° C Final reduction: about 850 ° C 압 력pressure 예열 : 180 kPa,g예비환원 : 180kPa,g최종환원 : 200kPa,gPreheating: 180 kPa, g Preliminary reduction: 180kPa, g Final reduction: 200kPa, g

유동층 환원로내 가스유속Gas Flow Rate in Fluidized Bed Reduction Furnace 제 1유동층로First fluidized bed 분산판 표면에서 유속 : 1.6 m/s원통형 상부(공탑)에서 유속 : 0.49 m/sFlow rate at the surface of the dispersion plate: 1.6 m / s Flow rate at the cylindrical top (air column): 0.49 m / s 제 2유동층로Second fluidized bed 분산판 표면에서 유속 : 1.7 m/s원통형 상부(공탑)에서 유속 : 0.51 m/sFlow rate at the surface of the dispersion plate: 1.7 m / s Flow rate at the cylindrical top (air column): 0.51 m / s 제 3유동층로Third fluidized bed 분산판 표면에서 유속 : 1.7 m/s원통형 상부(공탑)에서 유속 : 0.50 m/sFlow rate at the surface of the dispersion plate: 1.7 m / s Flow rate at the top of the cylinder (air column): 0.50 m / s

제 3유동층로에서 배출된 광석의 최종환원율Final reduction rate of ore discharged from the third fluidized bed furnace 입 도(㎜)Particle size (mm) 무 게(%)weight(%) 최종환원율(%)Final reduction rate (%) < 0.1250.120 ~ 1.0> 1.0<0.1250.120-1.0> 1.0 42.118.739.342.118.739.3 90.384.375.090.384.375.0 평 균Average 83.383.3

발명예Inventive Example

하기 표6과 같은 크기를 갖는 도 3에 도시된 바와 같은 본 발명의 유동층식 환원장치를 이용하여, 상기 표2과 하기 표7 및 표8에 제시되어 있는 조건으로 환원을 행한 후, 입도별 최종 환원률을 조사하고, 그 결과를 하기 표9에 나타내었다.Using the fluidized bed reduction apparatus of the present invention as shown in Figure 3 having the size as shown in Table 6, after the reduction under the conditions shown in Table 2 and Tables 7 and 8, the final size by particle size The reduction rate was investigated and the results are shown in Table 9 below.

유동층 환원로 높이 및 내경Fluidized bed reduction furnace height and inner diameter 제 1유동층로First fluidized bed 원통형 하부(분산판) 내경 : 0.37m원통형 하부 높이(분산판 표면에서) : 6.0m원통형 상부 내경 : 1.25m원통형 상부 높이 : 5.0mCylindrical lower part (distribution plate) Internal diameter: 0.37 m Cylindrical lower part height (on the surface of the dispersing plate): 6.0 m Cylindrical upper part Internal diameter: 1.25 m Cylindrical upper part height: 5.0 m 제 2유동층로Second fluidized bed 원통형 내경 : 0.26m원통형 높이 : 5.0mCylindrical Bore: 0.26m Cylindrical Height: 5.0m 제 3유동층로Third fluidized bed 원추형 하부(분산판) 내경 : 0.63m원추형 하부 경사각도 : 5°원추형 하부 높이(분산판 표면에서) : 3m원통형 상부 내경 : 1.15m원통형 상부 높이 : 3.5mConical lower part (distribution plate) Inner diameter: 0.63 m Conical lower inclination angle: 5 ° Conical lower part height (on the surface of the distribution plate): 3 m Cylindrical upper inner diameter: 1.15 m Cylindrical upper height: 3.5 m

환원가스 성분, 온도 및 압력Reducing gas component, temperature and pressure 가스조성Gas composition CO: 65%, H₂:25%, CO₂: 5%, N₂: 5%CO: 65%, H ₂ : 25%, CO ₂ : 5%, N ₂ : 5% 온 도Temperature 예열/예비환원 : 약 800℃최종환원 : 약 850℃Preheating / Preliminary Reduction: Approx. 800 ° C Final Reduction: Approx. 850 ° C 압 력pressure 예열/예비환원 : 180 kPa,g최종환원 : 200 kPa,gPreheating / Preliminary Reduction: 180 kPa, g Final Reduction: 200 kPa, g

유동층 환원로내 가스유속Gas Flow Rate in Fluidized Bed Reduction Furnace 제 1유동층로First fluidized bed 원통형 하부(분산판표면)에서 유속 : 2.4 m/s원통형 상부에서 유속 : 0.55 m/sFlow rate at the cylindrical bottom (spread plate surface): 2.4 m / s Flow rate at the cylindrical top: 0.55 m / s 제 2유동층로Second fluidized bed 원통형에서 유속 : 2.4 m/sFlow rate in the cylinder: 2.4 m / s 제 3유동층로Third fluidized bed 분산판 표면에서 유속 : 1.7 m/s원통형 상부(공탑)에서 유속 : 0.50 m/sFlow rate at the surface of the dispersion plate: 1.7 m / s Flow rate at the top of the cylinder (air column): 0.50 m / s

제 3유동층로에서 배출된 광석의 최종환원율Final reduction rate of ore discharged from the third fluidized bed furnace 입 도(㎜)Particle size (mm) 무 게(%)weight(%) 최종환원율(%)Final reduction rate (%) < 0.1250.125 ~ 1.0> 1.0<0.1250.125-1.0> 1.0 42.325.132.642.325.132.6 88.390.884.288.390.884.2 평 균Average 87.687.6

상기한 비교예에 따라 환원한 후의 입도별 환원률을 나타내는 표5와 본 발명에 부합되는 발명예에 따라 환원한 후의 입도별 환원률을 나타내는 표9에서 알 수 있는 바와 같이, 본 발명에 따라 광석을 환원한 경우(발명예)에는 본 발명에서 벗어난 조건으로 환원하는 경우(비교예)에 비하여 입도별 환원율이 균일하여, 평균환원율도 높게 나타난 것을 알 수 있다.Ore according to the present invention, as can be seen in Table 5 showing the reduction rate for each particle size after reduction according to the comparative example and Table 9 showing the reduction rate for each particle size after reduction according to the invention example according to the present invention, In the case of reducing (invention example), it can be seen that the reduction rate for each particle size is uniform and the average reduction rate is also higher than that in the case of reducing under the present invention (comparative example).

한편, 발명예에 따라 환원한 경우에 대하여 평균가스이용율과 가스원단위를 조사한 결과, 가스이용율은 약 30~35%, 가스원단위는 1200~1500Nm³/ton-ore 이었다. 또한, 발명예의 경우에는 제1 유동층로에 분철광석 투입 후 60분 이내에 광석배출이 가능하였다.On the other hand, the average gas utilization rate and gas source unit were investigated for the case of reduction according to the invention example, and the gas utilization rate was about 30 to 35%, and the gas source unit was 1200 to 1500 Nm ³ / ton-ore. In addition, in the case of the invention example, ore discharge was possible within 60 minutes after the addition of the iron ore to the first fluidized bed furnace.

이와 같이, 발명예에서는 원료 분철광석의 입도분포에 따라 분철광석의 입경별로 체류시간을 융통성있게 제어함으로써 입경에 관계없이 균일하고 높은 평균환원율을 얻을 수 있었다.As described above, according to the invention example, it is possible to flexibly control the residence time for each particle size of the iron ore according to the particle size distribution of the raw iron ore, thereby obtaining a uniform and high average reduction rate regardless of the particle size.

상술한 바와 같이, 본 발명은 넓은 입도분포의 분철광석을 입도분포에 따라 그 입경별로 체류시간을 융통성 있게 제어함으로서, 입경에 관계없이 균일하고 높은 평균 환원율을 얻을 수 있을 뿐만 아니라 평균 가스이용율을 향상시켜 가스원단위를 낮추는데 유용한 효과가 있는 것이다.As described above, the present invention flexibly controls the residence time for each particle diameter according to the particle size distribution of the iron-iron ore having a wide particle size distribution, thereby obtaining a uniform and high average reduction rate regardless of the particle size and improving the average gas utilization rate. This is useful to lower the gas source unit.

Claims

In the method for reducing the iron ore in the flow state by supplying a reducing gas to the reducing furnace to supply the iron ore,

The ferrite ore is charged into the lower furnace 100B of the serial twin type first fluidized bed furnace consisting of a cylindrical large diameter upper furnace 100A and a small diameter lower furnace 100B, and the terminal speed of the medium / small particle ore Supplying reducing gas to the bottom of the lower furnace (100B) at a flow rate less than or equal to the end speed of the allele ore to classify the allele and the medium / small ore to the lower (100B) and the upper (100A) of the fluidized bed furnace, respectively Allele ore is reduced at the bottom of the fluidized bed furnace (100B), and the medium / small particle ore is reduced at the top of the fluidized bed furnace (100A), through the bottom of the bottom (100B) and the bottom side wall of the upper furnace (100A) Preheating and pre-reducing with gas; And

The pre-heated and pre-reduced medium / small ore is finally reduced in the conical fluidized bed furnace 300 of one sub-angular narrow, and the pre-reduced and pre-reduced allelic ore is first reduced in a cylindrical fluidized bed 200 and then Fluidized bed reduction method of iron ore, including the step of sending to the fluidized bed 300 of the Sangsangha River

According to claim 1, wherein the preheating and pre-reduction temperature in the serial twin type first fluidized bed (100) is 700 ~ 800 ℃, and in the cylindrical fluidized bed (200) and conical fluidized bed (300) The first reduction and final reduction temperature of the fluidized bed reduction method of iron ore characterized in that the 750 ~ 900 ℃

The fluidized bed reduction method for ferrous ore according to claim 1 or 2, wherein the operating pressure is 2 to 6 atm in absolute pressure.

According to claim 1 or 2, the ore residence time in the serial twin type first fluidized bed (100) and conical fluidized bed (300) is 30 to 60 minutes, and the cylindrical fluidized bed (200) Ore residence time in c) is a fluidized bed reduction method of iron ore characterized in that 10 ~ 40 minutes

The ore residence time in the serial twin first fluidized bed furnace (100) and the conical fluidized bed furnace (300) is 30 to 60 minutes, and in the cylindrical fluidized bed furnace (200). Ore residence time is fluidized bed reduction method of iron ore characterized in that 10 ~ 40 minutes

In the fluidized bed reduction apparatus of the iron ore is configured to reduce the iron ore in the flow state by supplying a reducing gas to the reducing furnace is supplied with the iron ore,

Among the iron ore loaded into the cylindrical large diameter upper furnace (100A) and the small diameter lower furnace (100B), the opposing ore is divided into the lower (100B) and the medium / small ore is divided into the upper (100A). In 100B, the medium / small particle ore is a serial twin type first fluidized bed furnace 100 configured to be preheated and pre-reduced by a reducing atmosphere in the upper furnace 100A;

A cylindrical second fluidized bed furnace (200) configured to primarily reduce preheated and pre-reduced alleles in the first fluidized bed (100);

The third fluidized bed furnace, which is a conical shape of the Sangsang River Strait, configured to finally reduce the primary ore reduced mineral pre-heated and pre-reduced in the first fluidized bed furnace 100 and the second reduced allele ore in the second fluidized bed furnace 200 ( 300);

The particulate ore contained in the exhaust gas of the first fluidized bed furnace 100 is collected and supplied to the first fluidized bed furnace 100 through the upper side of the first fluidized bed furnace 100, and the exhaust gas from which the fine ore is separated is discharged to the outside. A first cyclone 400 configured to be discharged;

The particulate ore contained in the exhaust gas of the second fluidized bed furnace 200 is collected and supplied to the second fluidized bed furnace 200 through the sidewall of the second fluidized bed furnace 200, and the exhaust gas from which the fine ore is separated is a reducing gas. A second cyclone 500 configured to be supplied to the first fluidized bed furnace 100; And

The particulate ore contained in the exhaust gas of the third fluidized bed 300 is collected and supplied to the third fluidized bed 300 through the side wall of the third fluidized bed 300, and the exhaust gas from which the fine ore is separated is a reducing gas. It includes a third cyclone (600) configured to be supplied to the first fluidized bed (100),

A first gas supply port 101 for receiving a reducing gas is formed at a bottom of the lower flow path 100B of the first fluidized bed furnace 100, and the first fluid supply port 101 has a first fluidized bed. A twelfth conduit 604 for introducing gas into the lower portion 100B of the furnace 100 is connected, and is supplied through the first gas supply port 101 in the lower portion of the lower passage 100B. The first gas distribution plate 102 for dispersing the gas is embedded, and the first ore supply port 103 and preheated / pre-reduced allelic ore are provided on the side wall of the lower passage 100B. A second ore outlet 108 for discharging is formed, and the second ore outlet 108 is connected to the lower portion of the second fluidized bed furnace 200 through an second conduit 107 in an ore communication relationship. The first ore supply port 103 is connected to an ore supply source through an ore supply pipe 111;

A second gas supply port 106 for receiving a reducing gas is formed in the lower side wall of the upper flow path 100A of the first fluidized bed path 100, and the second gas supply port 106 provides gas. A thirteenth conduit 605 for introduction is connected, and in the lower portion of the upper passage 100A, a conical second gas distribution plate for dispersing the gas supplied through the second gas supply port 106 ( 112 is built-in, and a first ore outlet 104 for discharging preheated / pre-reduced neutral / small ore is formed on the side wall of the upper passage 100A, and the first ore outlet 104 is formed. Is connected to the lower portion of the third fluidized bed 300 in the ore communication relationship through the first conduit 109 and the fourteenth conduit 209, and the exhaust gas is discharged to the government of the upper furnace 100A. 1 gas outlet 105 is formed, the first gas outlet 105 is the first company through the third conduit 113 Connected to cyclone 400:

The first cyclone 400 is connected to the sixth conduit 402 for discharging the exhaust gas from which the fine ore separated to the outside, one end thereof is located deep inside the upper passage (100A) of the first fluidized bed (100) A fourth conduit 401 for supplying the collected fine ore into the first fluidized bed furnace 100 is connected;

A third gas supply hole 201 for receiving a reducing gas is formed at a bottom of the second fluidized bed furnace 200, and a third gas supply hole 201 is provided in a lower portion of the second fluidized bed furnace 200. The third gas distribution plate 202 for dispersing the gas supplied through the built-in, and the side wall of the second fluidized bed 200 is preheated in the lower path (100B) of the first fluidized bed (100) A second ore supply port 203 for receiving the pre-reduced ore and a third ore discharge port 204 for discharging the primary ultimately reduced allele ore, and the second ore supply port 203 Is connected to a second ore outlet 108 of the lower path 100B of the first fluidized bed furnace 100 through a second conduit 107, and the third ore outlet 204 is a tenth conduit ( 207 is connected to the lower portion of the third fluidized bed passage 300 in the ore communication relationship, and the second cyclone (side) of the second fluidized bed furnace 200 The fine ore supply port 208 for receiving the fine ore separated from the exhaust gas in the 500 is formed, and the second gas outlet 205 for discharging the exhaust gas is formed in the government of the second fluidized bed furnace 200. This second gas outlet 205 is connected to the second cyclone 500 via an eighth conduit 206:

The second cyclone 500 is connected to the seventh conduit 502 for discharging the exhaust gas from which the fine ore is separated to the outside, one end thereof to the fine ore supply port 208 of the second fluidized bed 200 A ninth conduit 501 for supplying connected and collected particulate ores into the second fluidized bed 200 is connected;

The third fluidized bed 300 is formed of a cylindrical upper portion 300A and a conical lower portion 300B, and a fourth gas supply port 301 for receiving a reducing gas is formed at a bottom thereof, and the third fluidized layer A fourth gas distribution plate 302 for dispersing the gas supplied through the fourth gas supply port 301 is built in the lower part of the furnace 300, and the sidewall of the third fluidized bed furnace 300 is Third ore supply port 303 for receiving the preheated / pre-reduced medium / small ore and the primary reduced allele ore from the second fluidized bed 200 in the upper passage (100A) of the first fluidized bed (100) And a fourth ore discharge port 304 for discharging the finally reduced ore, and the third ore supply port 303 is formed through the fourteenth conduit 209 and the first conduit 109. The third light is communicated with the first ore outlet 104 of the upper passage 100A of the fluidized bed passage 100 and through the fourteenth conduit 209 and the tenth conduit 207. In communication with the outlet 204, the fourth ore outlet 304 is connected to the sixteenth conduit 307, and the third gas outlet for discharging the exhaust gas to the government of the third fluidized bed (300) ( 305 is formed, the third gas outlet 305 is connected to the third cyclone 600 through the fifteenth conduit 306; And

The third cyclone 600 is connected to the eleventh conduit 602 for discharging the exhaust gas from which the fine ore separated to the outside, one end thereof is located deep inside the third fluidized bed passage (300) Fluidized bed reduction apparatus for iron ore, characterized in that the seventeenth conduit (601) for supplying the ore into the third fluidized bed (300) is connected

The apparatus of claim 6, wherein a reducing fin 110 is provided in the upper portion of the lower portion 100B to increase the gas flow rate.

The method according to claim 6 or 7, wherein the seventh conduit 502 is in communication with the thirteenth conduit 605 so that the blue flue gas of the second fluidized bed furnace 200 is reduced to the reducing gas of the first fluidized bed furnace 100. Used;

The twelfth conduit 604 and the thirteenth conduit 605 communicate with the eleventh conduit 602 such that clean exhaust gas of the third fluidized bed furnace 300 is used as the reducing gas of the first fluidized bed furnace 100; And

The 20th conduit 702 and the 21st conduit 703 are provided in the upper part of the melt gasifier 700, and communicate with the 19th conduit 701 which discharges the exhaust gas of the melt gasifier 700, and is the melt gasifier 700 ) Flue gas is used as the reducing gas of the second fluidized bed furnace 200 and the third fluidized bed furnace (300)

The method of claim 6 or 7, wherein the height of the upper passage (100A) of the first fluidized bed furnace (100) is 3 to 7 times its inner diameter, and the height of the lower passage (100B) is 15 to 25 times its inner diameter;

The height of the second fluidized bed furnace 200 is 15-25 times the inner diameter thereof; And

The height from the gas distribution plate 302 of the conical lower portion 300B of the third fluidized bed 300 is 3 to 7 times the inner diameter of the lower gas distribution plate, and the height of the cylindrical upper portion 300A is 2 to 5 times the inner diameter. , The inclination angle of the conical lower portion (300B) is a fluidized bed reduction device of iron ore, characterized in that 5 to 20 ° from the vertical line

The method of claim 8, wherein the height of the upper passage (100A) of the first fluidized bed furnace (100) is 3 to 7 times its inner diameter, and the height of the lower passage (100B) is 15 to 25 times its inner diameter;

In the method for reducing the iron ore using the fluidized bed reduction apparatus of the iron ore of claim 6,

Charged iron ore into the lower passage 100B of the first fluidized bed furnace 100, and supplying reducing gas to the bottom of the lower passage 100B at a flow rate equal to or greater than the terminal velocity of the allele or more than the terminal velocity of the medium / small ore. By classifying the ore and the medium / small ore into the lower (100B) and the upper (100A) of the first fluidized bed (100), respectively, the opposite ore is the lower (100B) of the first fluidized bed (100), And pre-heating and pre-reducing the medium / small-size ore by the reducing gas supplied through the side of the bottom of the lower passage (100B) and the upper passage (100A) of the upper passage (100A) of the first fluidized bed furnace (100) ; And

The pre-heated and pre-reduced medium / small ore is finally reduced in the conical third fluidized bed furnace 300 of one subsidiary subsidiary, and the pre-heated and pre-reduced allele is in the cylindrical second fluidized bed furnace 200. After the first reduction and sent to the third fluidized bed (300) of the Sangsanghyang narrow down to the final reduction fluidized bed type of reduced iron ore comprising a step

The method of claim 11, wherein the preheating and pre-reduction temperature in the first fluidized bed (100) is 700 ~ 800 ℃, and the first reduction in the second fluidized bed 200 and the third fluidized bed (300) Final reduction temperature is fluidized bed reduction method of iron ore, characterized in that 750 ~ 900 ℃

The fluidized-bed reduction method for iron ore according to claim 11 or 12, wherein the operating pressure is 2 to 6 atm in absolute pressure.

The ore residence time in the first fluidized bed furnace (100) and the third fluidized bed furnace (300) is 30 to 60 minutes, and ore in the second fluidized bed furnace (200). Retention time is 10 to 40 minutes Fluidized bed reduction method of iron ore

The ore residence time in the first fluidized bed furnace (100) and the third fluidized bed furnace (300) is 30 to 60 minutes, and the ore residence time in the second fluidized bed furnace (200) is 10. Fluidized bed reduction method of iron ore, characterized in that ~ 40 minutes