JPS6014808B2 - An operating method that simultaneously sinters and reduces a mixture of powdered iron oxide and heavy oil and gasifies heavy oil using a single reaction tower in which a fluidizing medium circulates. - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to the reduction of finely powdered iron oxide, in which a coarse mixture of finely divided iron oxide and young oil is ground up and reduced in a single reaction column in which a fluidizing medium is circulated. Regarding the operation method that simultaneously causes the gasification of heavy oil and the gasification of heavy oil, in particular, by simultaneously causing the reduction of fine powdered iron oxide and the gasification of heavy oil using a single reaction column, it is possible to reduce the conventional direct reduction. The purpose is to provide an operating method that does not require separate equipment for granulation, coalescence, gasification of heavy oil, reduction of heated iron oxide as a fluidizing medium, etc., as in the iron manufacturing process. It is something.

An example of a conventional method for reducing powdered iron oxide using military oil is shown in FIG. In FIG. 1, 41 is a reaction tower and 42 is a reheating tower. The amount of heat required for the endothermic reaction in which the powdered iron oxide is reduced in the reaction tower 41 is provided by circulating the high temperature fluidizing medium in the reheating tower 42 via the connecting pipe 43. The fluidizing medium is transferred from the reaction column 41 to the reheating column 42 through a connecting pipe 50 and a cyclone 45 between the two columns.
On the other hand, powdered iron oxide is supplied into the reaction tower 41 from the supply port 44 and is fluidized by the fluidizing gas introduced from the gas inlet 51, and at the same time, the powdered iron oxide is supplied from the inlet 48 to a separately provided reducing gas production device. A reducing gas produced by gasifying heavy oil (not shown) is blown in to cause a reduction reaction, and the reduced powdered iron ore is granulated and consolidated for use. In contrast, carbonaceous materials such as coke and coal are
V is supplied into the reheating tower 42 from 7, and the gas inlet 50 of Shimousa
A fluidized bed is formed by the fluidized gas introduced from the gas injection nozzle 46, and the medium is combusted and heated by being brought into contact with an oxidizing gas such as oxygen or air blown from the gas injection nozzle 46 to obtain a high-temperature fluidized medium that serves as a heat source for the reaction.

As mentioned above, in the secondary method, young oil is gasified to produce a reducing gas rich in hydrogen, carbon monoxide, etc., and this reducing gas is sent to a separate reduction reaction device for powdered iron oxide. Since the powdered iron oxide is reduced by this method, there is a drawback that an expensive reducing gas production device is required. In addition, if the ore raw material is finely powdered iron oxide obtained by flotation treatment, granulation or coalescence equipment for finely divided iron oxide is required, which increases the construction cost for these facilities. Since the energy loss is multiplied between each device, the overall energy loss is large and it is difficult to achieve the beauty of energy saving.

Furthermore, iron ore resources in the future will tend to gradually change from soul ore to fine powder, and in particular, it is expected that the proportion of fine powder ore resulting from flotation processing will increase.

Even in such a situation, when reducing fine powdered iron oxide, it is necessary to separately install the granulation and sintering equipment, reduction gas generation equipment, reduction reaction equipment, fluidization medium heating equipment, etc. as described above. is not a good thing. The present inventor has achieved the goal of simultaneously performing various processes such as granulation, refinement and reduction of powdered iron oxide, and production of reducing gas from heavy oil in the same reaction tower, thereby reducing equipment construction costs and reducing energy consumption. With the aim of developing a highly efficient operating method, the company first established
No. 361 (Patent Registration No. 901553) "Fluidization operation method that simultaneously causes sintering and reduction of fine powder iron oxide and gasification of heavy oil ↓ Japanese Patent Publication No. 52-30362 (Patent Registration No. 901554) ``Operation method for simultaneous reduction of powdered iron oxide and gasification of heavy oil using a circulating fluidized bed'' The company provided an operating method that simultaneously produces competitive mackerel reduction and gasification of virgin oil.

In order to simultaneously produce the refining and reduction of fine powdered iron oxide and the gasification of car oil, it is necessary to continuously supply thermal energy into the reaction tower. Publication No. 52-30362' is an operation method that achieves the integration of thermal energy into the reaction tower by heating from the outside of the reaction tower and circulation of high-temperature solid particles from the outside. This method of operation is achieved by introducing hot combustion gas with oxygen or oxygen-enriched gas into the upper part of the reaction column. This invention continuously supplies the necessary thermal energy into the reaction tower.
This technology does not supply thermal energy from outside the reaction tower as in the secondary reactor technology, but efficiently supplies thermal energy within a single reaction tower. By installing a partition wall in the reaction tower and continuously circulating the solid particles as a fluidizing medium through the reaction tower, the purpose is achieved, and at the same time, the reduced iron coarse particles can be easily separated from the solid particles that are the fluidizing medium. This is for the purpose of discharging the water.

In this invention, by providing a partition wall in a reaction tower that forms a single fluidized bed using high-temperature solid particles as a heat medium, a portion of one fluidizing medium is connected to the upper end of the partition wall and a portion of another fluidizing medium. Continuous circulating flow of the fluidizing medium is caused in the fluidized bed through the lower end, and in one part separated by the partition wall, the fluidizing medium is heated, and a mixture of fine powdered iron oxide and heavy oil is heated. is added to the other high-temperature fluidized bed formed by the partition walls, the virgin oil is gasified in the presence of fine powdered iron oxide to produce a reducing gas, and the fine powdered iron oxide is Residual carbon from the oil, high temperature and reducing atmosphere in the fluidized bed cause coagulation and reduction.

The features of this invention will be further explained in detail below. In this invention, a cylindrical reaction column having a lower bottom whose cross-sectional area gradually decreases toward the bottom and a partition wall inside the reaction column has an average particle size of 0.1 to 1. A fluidizing medium consisting of a particulate solid is contained, and a continuous circulation of the fluidizing medium is formed in the fluidized bed by feeding a fluidizing gas into this fluidizing medium, and the fluidizing medium is formed by a partition wall. Oxygen or oxygen-rich gas is fed into one fluidized bed to flow the fluidizing medium, and at the same time gasify and burn the combustible materials packed in the fluidized bed. The fluidized medium is heated to 800 to 120,000 ℃, and the overflowing fluidized medium is circulated and moved into the other fluidized bed formed by the partition walls, and the transferred high-temperature fluidized medium causes a high temperature. In the high-temperature fluidized bed, more than 80% by weight is zero.
．． Finely powdered iron oxide having a particle size of 1 side or less is supplied as a mixed granule with 10% to 50% by weight of the finely divided iron oxide, and 700% to 1100%
This is a fluidization operation method that simultaneously causes the competitive regeneration and reduction of fine powdered iron oxide and the gasification of bulk oil in a temperature range of 0.00°C.

The fluidizing medium used in this invention allows the coarse particles of the mixture of fine powdered iron oxide and heavy oil to be evenly dispersed in the fluidized bed formed within the cylindrical body, and
Helps promote stable granulation of finely divided iron oxide reduced in high temperature and reducing atmosphere,
If the average particle size of the fluidizing medium exceeds 1.0, it is undesirable because it becomes difficult to separate the fluidizing medium from the reduced granular ring iron. If this is the case, the amount of the fluidizing medium that is blown away from the top of the fluidized bed by the fluidizing gas and dissipated increases, which is not preferable. As fluidizing media, refractories such as sand and alumina, metal oxides such as iron ore, lime, and dolomite are used, and carbonaceous solids such as coke and char are used to enhance reduction and reduce gas Effective in increasing the amount generated.
In the reaction tower of this invention, the cylindrical body housing the fluidized bed inside has a shape in which the cross-sectional area gradually decreases toward the bottom. In addition to increasing the reaction efficiency within the cylindrical body by sufficiently separating the body and the fluidizing medium, it is also necessary to prevent the fluidizing medium from mixing with the reduced jaw granular reduced iron discharged from the bottom of the cylindrical body. This is to prevent this.

In order to form a fluidized bed of fluidized media within the cylindrical body, a fluidized gas is passed through one of the fluidized media formed by the partition wall.

As this fluidizing gas, it is preferable to use a reducing gas consisting of one or more hydrocarbon gases such as hydrogen, carbon monoxide, and methane. Try to maintain a reducing atmosphere throughout your body. Furthermore, the fluidizing gas may be used by purifying and recirculating the exhaust gas discharged from the upper part of the cylindrical body.Even if it contains nitrogen, water vapor, carbon dioxide, etc., the essential point is to fluidize the fluidizing medium. Any material may be used as long as it does not interfere with the generation of reducing gas due to the decomposition of car oil and the reduction of finely powdered iron oxide. Among the high-temperature fluidized beds formed in the cylindrical body, in the other fluidized bed separated by a partition, 80% or more by weight of finely powdered iron oxide having a particle size of 0.1 rib or less, A mixture of young oil adjusted to 10 to 50% by weight is added to this powdered iron oxide as a granule to simultaneously burn and reduce the fine powdered iron oxide and gasify the heavy oil. However, the reason why more than 80% by weight of the fine powdered iron oxide has a particle size of 0.1 or less is as follows.
This is because if the particles are coarser than this, the formation of a mixture granule with heavy oil is insufficient, and it becomes difficult to form fine particles of iron oxide in the fluidizing medium.

The fluidized bed formed by the fluidizing gas sufficiently reduces the coarse particles of the mixture of finely powdered iron oxide and heavy oil in the cylindrical body and forms neck particles, increasing reaction efficiency and reducing the In order to prevent the fluidization medium from mixing with the reduced iron, it is desirable that the height is at least twice the maximum inner diameter. Temperature required for reduction of iron, i.e. 700-1100
Must be held at oo.

In addition, the vehicle oil to be mixed with the above-mentioned fine powdered iron oxide is used in the distillation residual oil such as heavy crude oil and heavy oil, or in the carbonization and gasification of coal.

Suitable young oils such as raw young oil, natural asphalt, sand tar bitumen, etc. are suitable.This young oil acts as a binder for fine powdered iron oxide, and also acts as a binder for fine powdered iron oxide at high temperatures. Along with performing stripes and reduction,
It plays the role of generating reducing gas. The mixing ratio of child oil, which plays such a role, to fine powdered iron oxide is 10 to 50%. In other words, the mixing ratio is 1
If it is less than 0%, it will not be able to fulfill its role as a binder, and if it exceeds 50%, the mixture of fine powdered iron oxide and car oil will not become coarse particles but will become a slurry, and will not be able to handle high temperatures. This is not preferable because it becomes difficult to obtain reduced particles in the form of jaw granules in the fluidized bed. The size of the aggregated particles of the above-mentioned mixture of fine powdered iron oxide and car oil is 2~
It is advantageous to have two revenges. If the particle size is less than 2, it will be difficult to separate it from the fluidizing medium, and if it exceeds 2, the coarse particles of the mixture will be easily destroyed, and even if the particle size is reduced within the fluidized bed. Even if it were to be maintained until later, it would be undesirable because the time required for competition and return would be longer. Under the above conditions, a high-temperature fluidized bed of fluidizing medium and fluidizing gas is formed inside the cylindrical body.
When coarse particles of a mixture of finely powdered iron oxide and heavy oil are fed into one fluidized bed formed by a partition wall installed in the cylindrical body, the finely powdered iron oxide is sintered and the heavy oil is pulverized. The iron oxide is gasified in the presence of iron oxide, and at the same time the fine iron oxide is reduced to become jaw grains of reduced iron, which are separated from the fluidizing medium at the bottom of the cylindrical body with a small cross-sectional area and discharged outside the cylinder. . The fluidizing medium separated from the jaw granular reduced iron at the lower part of the cylindrical body is transported upward by the reducing gas introduced into the lower part of the cylindrical body, and the other side formed by the partition wall installed inside the cylindrical body. The fluidized bed enters the fluidized bed, and the combustible material in the fluidized medium or the combustible material charged into the fluidized medium is gasified and combusted by the oxygen or fluidized gas containing oxygen gas introduced into the fluidized bed. heat the heating medium. In this case, instead of introducing oxygen and combustible substances, hot combustion gas can be introduced. By circulating the fluidized medium heated to a high temperature over the partition wall to the side of the fluidized bed to which the coarse particles of the mixture of fine powder iron oxide and heavy oil formed by the partition wall are supplied, the mixture of fine powder iron oxide and heavy oil is Thermal energy necessary for sintering and reducing iron oxide and gasifying virgin oil is supplied. Next, the configuration of the method of the present invention will be explained in detail with reference to the drawings based on specific embodiments. FIG. 2 schematically shows a cylindrical reaction tower that simultaneously causes three reactions: sintering of finely powdered iron oxide, gasification of car oil, and reduction of finely divided iron oxide in one embodiment of the present invention. It is a joint cross-sectional side view shown.

In Fig. 2 above, the cross-sectional area of the bottom of the reaction tower 1 is funnel-shaped, which gradually becomes smaller toward the bottom. However, it is not limited to this shape; The granular reduced iron produced by the reaction from the mixed granules is sufficiently separated from the fluidizing medium, and furthermore, when the granular reduced iron is discharged from the bottom of the reaction tower, a large amount of the fluidizing medium is removed. Any shape may be used as long as it can avoid mixing. The shape of the middle and upper part of the reaction tower 1 is arbitrary, and even if the cross-sectional area is constant up to the vicinity of the upper end as in the reaction tower 1 shown in FIG. 2, there is no problem even if the cross-sectional area in the upper part is large. Inside the reaction column 1, a fluidizing medium made of powder or granules with an average particle size of 0.1 to 1.0 mm, such as sand, alumina, iron ore, lime, or carbon materials such as coke and char, is placed. The fluidizing medium is divided into two parts, namely 3 and 4, which are connected at the upper and lower ends of the partition wall by a partition wall 2 installed in the reaction column 1. It is fluidized by a fluidizing gas, such as a reducing gas rich in hydrogen to carbon monoxide, fed from the feed pipe 6 through the rectifier 5 to form a fluidized bed.

At this time, hydrocarbons such as methane and ethane are added to the fluidizing gas.
Gases such as water vapor, carbon dioxide, and nitrogen may be present. Fluidizing gas inlets 7, 7', 7'' may be provided at the side of the reaction column 1 to assist in fluidizing the portion 3 of the fluidizing medium separated by the partition.
The positions, numbers, and shapes of the inlets 7, 7', and 7'' are determined appropriately so that the fluidized bed formed here is suitable for the reaction of the coarse mixture of finely powdered iron oxide and cloudy oil, which will be described later. In addition, an inlet 8 for fluidizing gas may be provided on the side of the reaction column 1 in order to help fluidize the portion 4 of the fluidizing medium divided by the partition wall, and the position of the inlet 8 may be , number, shape, etc. are determined as appropriate, and the fluidized bed formed here is arranged so as to be continuously circulated between the fluidizing media 3 and 4. A charging port 9 is installed in the lower part of the fluidizing medium section 4, through which combustible materials such as heavy oil, pitch, granular coal, etc. are charged into the fluidizing medium 4, and an inlet 10 is provided. The above combustible materials are gasified by introducing oxygen or oxygen-rich gas from
The combustion heats the fluidizing medium to a temperature range of 800-1200 oo.

The position, number, shape, etc. of the charging port 9 and the inlet port 10 may be determined as appropriate, and the positional relationship between the charging port 9 and the inlet port 10 is not restricted to the arrangement shown in FIG. There is no problem even if it is on the top. At this time, high-temperature combustion gas can be introduced into the bag through the charging port 9 and the inlet 10, and the heat can be radiated to the temperature range above the fluidizing medium. In the reaction column 1 shown in FIG. , by appropriately determining the shape and the flow rate of the oxygen-rich gas or the flow rate of the hot combustion gas fed through it, the fluidizing medium in the reaction column 1 descends as a whole from the section 3, The fluidized medium enters the 4th part of the fluidized medium through the lower end of the partition, ascends as a whole through the same part, and then moves back to the 3rd part of the fluidized medium through the upper end of the partition, creating a continuous circulation. ,
The hot fluidizing medium heated in section 4 can carry a large amount of thermal energy into section 3. The upper part of the reaction tower 1 is filled with finely powdered iron oxide, of which 80% or more by weight has a particle size of 0.1 or less, and 10 to 10% by weight of this finely powdered iron oxide, which penetrates the side wall of the reaction column 1. A charging port 11 is provided for supplying coarse particles of the mixture with virgin oil adjusted to 50% to the upper part of the fluidizing medium 3 in the fluidized bed.

Therefore, the coarse mixture supplied from the bag inlet 11 is rapidly heated in the fluidized bed to reduce the particle size of the coarse mixture.
At the same time, the cloudy oil decomposes and generates reducing gas, and at the same time, the iron oxide after sintering is reduced by the carbon and reducing gas from the car oil, causing excessive reducing The gas leaves the top of the fluidized bed and rises. Here, the powder particles contained in the reducing gas that has risen into the space 12 of the reaction tower 1 are separated by passing through a collector 13, and then the gas is taken out from the discharge row 4. The collected powder particles are repeatedly charged into the fluidizing medium section 4 from the bottom of the bottle collector 13. As mentioned above, while the three reactions of reduction and gasification occur simultaneously, the coarse mixture gradually descends in the fluidized bed 3 of the fluidized medium divided by the partition wall in the reaction tower 1, The reduced iron becomes granular particles and collects at the bottom of the reaction tower 1.

A discharge pipe 15 is provided at the bottom of the reaction tower 1 to recover the neck granular reduced iron. Since the above simultaneous reactions of dawning, reduction, and gasification are all endothermic reactions, the fluidized bed 3 of the fluidizing medium
The reaction temperature within the reactor must be maintained in the range of 700-1100°C. During the above reaction, on the upper surface of the fluidized bed 3 of the fluidized medium, the weight ratio of the mixture aggregates and sintered bodies to the fluidized medium is 1/20 or less, and directly above the rectifier 5, the weight ratio of the granular reduced iron to the fluidized medium is 1/20 or less. The weight ratio to fluidizing medium is 1/10 or more.

Such a difference in weight ratio is achieved because the cross-sectional area of the lower part of the reaction tower gradually decreases downward, and the average flow velocity of the fluidizing gas increases as it goes downward. As described above, the granular reduced iron is discharged to the outside of the reaction tower 1 through the discharge pipe 15. At this time, if the granular reduced iron and the fluidization medium are not completely separated, for example, the granular reduced iron is discharged. A fluidizing gas inlet 16 is provided in the middle of the pipe 15, and the fluidizing medium mixed with the granular reduced iron and descending can be returned to the bottom of the reaction column 1 from the discharge pipe 15.

At this time, the weight ratio of the jaw granular reduced iron to the fluidizing medium immediately above the rectifier 5 is 1/10 or more. The discharge method that involves separation as described above is not limited to the above method, and other methods may be used as appropriate. This invention is based on the second
The apparatus is not limited to the embodiment shown in the figures, and other embodiments such as those exemplified below can also be adopted.

Although the charging port 11 in FIG. 2 is shown as a single tube for simplicity, the number and shape of the tubes may be arbitrary, such as a plurality of tubes or tubes branched at a tip.

Although FIG. 3 is a cross-sectional view taken along line AA' in FIG. 2, it is not limited to this, and the reaction tower 1 may have a cross-section as shown in FIG. 4, for example, or as shown in FIG. It may also have an asymmetric longitudinal section.

The collector 13 for separating the powder and granules from the generated reducing gas in the space 12 may be installed outside the reaction tower 1 as shown in FIG. 5, and the separated powder and granules are returned. It is returned to the reaction column 1 through pipe 17. Reducing fluidizing gas inlet 7, 7',
7'', 8 and the inlet 10 for oxygen-containing gas or high-temperature combustion gas do not necessarily need to be opened in the side wall surface as shown in Fig. 2. The same applies to the combustible material charging port 9.Furthermore, the fluidizing medium may be of a dispersion type.
In order to help ensure stable and continuous circulation within the
A high flow rate of reducing gas can be introduced through the inlet tube 18 shown. The cross section of the reaction tower 1 divided by the partition walls 2 does not necessarily have to be symmetrical; for example, the section AA' in the reaction tower shown in FIG.
It may be something like the figure. The partition wall 2 in the reaction tower 1 is not limited to a flat plate shape as shown in FIGS. 2 to 7, but may be cylindrical, for example, like the partition wall 2 in FIGS. 8 and 9. At this time, the fluidized bed of the fluidizing medium is divided into a portion 3 inside the cylindrical partition wall and a portion 4 outside the partition wall. 9th
The figure shows a sectional view taken along line AA' of the reaction tower 1 in FIG. In this invention, when it is desired to separately take out the gases generated from both parts 3 and 4 of the fluidized bed divided by the partition wall 2 in the reaction tower 1, the partition wall 2 is It can be extended to the top of the tower.

At this time, an outlet 19 is installed near the upper surface of the fluidized bed 4, and the circulating fluidizing medium can be moved from the fluidized bed section 4 to the section 3 through the downcomer pipe 20 and the riser pipe 21. The form of this movement is arbitrary, but in the example shown in FIG. 10, the fluidizing gas is introduced into the riser pipe 21 via the inlet 22 and the rectifier 23. Further, the generated gas is discharged to the outside of the reaction tower 1 through the discharge port 24. When air is used as the oxygen-containing gas fed into the fluidized bed section 4 and it is desirable that the combustion gas after using the air be dissipated into the atmosphere, the gas generated from the upper surface of the fluidized bed section 4 Since it is unfavorable for thermal efficiency to contain combustible gas, in this case, an inlet 26 is installed near the top surface of the fluidized bed section 4, and air is introduced through this inlet to remove the combustible gas. Complete combustion can be achieved. At this time, the inlet 25 is not limited to the one shown in FIG. 10, but may be one that protrudes into the fluidized bed to achieve good dispersion. FIG. 11 shows a case where the partition wall is cylindrical, and from the fluidized bed portion 4 outside the cylindrical partition wall to the outlet 19.
, a path through which the fluidizing medium circulates to the fluidized bed section 3 through the downcomer pipe 20 and the riser pipe 21.

If it is necessary to take out the respective gases generated from the fluidized bed section 3 and section 4 separately, by providing a partition wall inside the reaction column 1 as a cross section as shown in FIG. The same purpose can be achieved as the device shown in FIG. Although FIG. 12 shows an example of a symmetrical partition wall for simplicity, the present invention is not necessarily limited to this, and for example, a completely symmetrical partition wall as shown in FIG. 13 may be used. 14th
The figure is a longitudinal cross-sectional view of the reaction tower 1 taken along the XX' cross section in the direction of the arrow in the example of FIG. This is to explain.

In Fig. 14, the reduced iron in the form of granules produced by performing the three reactions of sintering, reduction, and gasification inside the fluidized bed section 3 divided by the partition walls 2 and 2' is mixed with a fluidizing medium. It collects at the bottom of the reaction tower 1 and has a classification function (inlet 16).
It is discharged to the outside from the bottom of the reaction tower through a discharge pipe 15 having a diameter. The fluidizing medium separated from the granular reduced iron immediately above the rectifier 5 passes around the lower end of the partition wall 2 and enters the lower part of the fluidized bed section 4, and the fluidizing medium is fed through the inlet 06, the rectifier 5, and the inlet 8. The combustible material moves upward in the fluidized bed section 4 in a fluidized state due to the action of It is heated by combustion and moves from the upper end of the partition wall 2' to the fluidized bed section 4' shown in FIG. FIG. 15 is a vertical cross-sectional view of the YY' cross section in FIG.
The fluidized bed section 3' and section 4' located further back will be explained. In FIG. 15, the fluidizing medium transferred above the fluidized bed section 4' moves downward in the fluidized bed section 4' in a weak fluidized state, goes around the lower end of the partition wall 2 at the bottom of the reaction column, and passes through the fluidized bed section 3'. It is moved upward in a fluidized state by the action of the fluidizing gas fed through the inlet 6, the rectifier 5 and the inlets 7, 7', 7'', and the It circulates stably and continuously by moving beyond the partition wall 2' in Fig. 12 to the upper surface of the fluidized bed section 3.In other words, by installing the partition wall in a single cylindrical body, the fluidizing medium is stabilized and circulated. In obtaining granular reduced iron by causing continuous circulation and supplying coarse particles of a mixture of finely powdered iron oxide and heavy oil to the upper part of one fluidized bed section divided by partition walls, It has the same effect as those in Figs. 2 to 11. As the reducing gas used in this invention, it is desirable to purify the reducing gas generated from the reaction tower 1 and recycle it. The system shown in Figure 16 is one of the methods for recycling the reducing gas.
This is an example.

In FIG. 16, a mixture of fine powdered iron oxide and heavy oil is supplied to the reaction tower 1 from a charging port 11,
7 and is discharged from the reaction tower. On the other hand, reducing gases generated by gasifying military oil and gasifying charged combustibles are mixed in the reaction tower 1 and sent from the outlet 14 through the conduit 28 to the cooling and refining tower 29 for cooling and cleaning. It will be thickened. The cooled gas enters a heat exchanger 311 through a conduit 30, then moisture is removed in a dehydration tower 32, and then a decarboxylation tower 33.
Carbon dioxide is removed. The reducing gas purified as described above is sent to the heat exchanger 31 and the heat exchanger 35 by the circulation blower 34 and heated, and then passes through the inlets 6, 7, 7', 7'' and 8 to the reaction column. 1. Oxygen-rich gas is fed through the inlet 10, but if the gas does not contain nitrogen, there is no need to release the produced gas out of the system. Since it is disadvantageous to circulate large amounts of nitrogen when using air as the oxygen-rich gas, the production of reducing gases using air is It is discharged outside the system through the conduit 26 in the figure, but at this time, air can also be introduced from the inlet 25 near the top of the reaction column 1. Even if air is not used, it is rich in oxygen. Even if the reducing gas generated by the gas needs to be taken out separately, it can be discharged out of the system through the conduit 26. This is done using fresh oil, but a heavy oil rough separation device 36 is installed in the loop, and the young oil containing particles is separated and reacts as a combustible substance that is gasified and burned by the oxygen-containing feed gas. It is fed through the inlet 9 at the bottom of the column 1. Fig. 16 shows an example of a method for effectively recycling and using the generated reducing gas using the operating method of the present invention. Other methods may be used as long as the resulting reducing gas is purified and sent to the lower part of the reaction tower as a reducing gas.Next, specific numerical values for experiments on fine powder iron oxide reduction will be shown.

Example A fluidization operation was carried out under the conditions shown in Table 1 using a heat-resistant metal reactor having an inner diameter of 10 arcs in the upper part of the fluidized bed as shown in FIG.

However, to compensate for heat loss, the outside was heated with an electric furnace.
Table 1 Examples of experimental values obtained by continuous operation under the above conditions are shown in Table 2.

As described in Table 2 and above, the fluidization operation method of the present invention has the following effects when reducing fine powdered iron oxide.

(i- Since three types of reactions, sintering and reduction of fine powdered iron oxide and gasification of military oil, occur simultaneously in the same reaction tower, granulation and sintering cannot be performed as in the conventional direct reduction iron manufacturing method. It is possible to efficiently reduce fine powdered iron oxide without requiring separate equipment for the gasification and reduction of young oil, and without the need for extensive pollution prevention equipment that accompany these devices.

(ii) Since gasification and combustion using oxygen can be performed as a method of supplying the thermal energy necessary for reduction and gasification reactions, it is possible to configure a complete closed system in which the generated gas is purified and recycled. is possible and therefore does not pose the risk of becoming a source of environmental pollution as with known direct reduction methods.

(iii) It is industrially advantageous because the thermal energy used to reduce the finely divided iron oxide can be reduced compared to existing direct reduction methods.

[Brief explanation of the drawing]

FIG. 1 is an explanatory diagram of the prior art, FIG. 2 is an explanatory diagram of a vertical cross-sectional side view of a fluidization operation reaction tower in one embodiment of the present invention, and FIG. 3 is an AA' cross-sectional view of the reaction tower shown in FIG. 2. , FIG. 4 is another example of the cross-sectional view of the reaction tower, FIG. AA' of the reaction column shown in the figure
A sectional view, FIG. 7 is another example of the cross section of the reaction tower shown in FIG. AA′ cross-sectional view of the reaction tower shown in FIG. Fig. 11 is a partial explanatory view showing the upper part of the longitudinal side of the reaction tower, showing an example in which the partition wall is made cylindrical and extended to the upper part of the reaction tower in the same case as Fig. 10;
Figures 1 and 13 are drawings showing examples of almost perpendicular partition walls provided as cross sections inside the reaction tower, and Figures 14 and 15 show examples of reaction towers equipped with partition walls as shown in Figure 12. FIG. 16, which is a longitudinal side view, is a block diagram showing an example of a system for purifying the reducing gas generated from the reaction tower of the present invention and circulating it to the bottom of the reaction tower. 1...reactive, 2...partition, 3,4...
... Part of the fluidized bed divided by partition walls, 5.
... Rectifier, 6 ... Fluidization gas feed pipe,
7, 7', 7'', 7 river, 8...Fluidization gas inlet, 9...Combustible material charging inlet, 10...Oxygen-rich gas inlet , 11... Inlet of bag for coarse mixture, 12... Space, 13...
Collector, 14... Gas discharge port, 15... Discharge pipe, 16... Fluidization gas inlet, 17...
...Return pipe, 18...High speed reducing gas inflow pipe,
19... Outlet of fluidizing medium, 20...
Descending pipe, 21... Rising pipe, 22... Fluidizing gas inlet, 23... Rectifier, . 24...
...Gas outlet, 25...Air inlet, 26,
28, 30... Conduit, 27... Frame granular reduced iron, 29... Cooling refinement tower, 31, 35...
... Heat exchanger, 32 ... Dehydration tower, 33 ...
...Decarboxylation tower, 34...Blower, 36...
・Assembly separation device, 37...Pump, 41...
... Reaction tower, 42 ... Reheating tower, 43 ... Connection pipe, 44 ... Supply port, 45 ... Cyclone, 46 ... Gas blowing Included nozzle, 47...
Carbon material supply port, 48... Gas inlet for gas supply port, 49
, 51...Fluidized gas inlet, 50...
communication pipe. Figure 3...Figure 4Figure 6Figure 7Figure 9Figure 12Figure 13Figure 1Figure 2Figure 5Figure 8Figure 10Figure 1Figure 14Figure 15Figure 16

Claims (1)

[Claims] 1 A partition wall is provided in a cylindrical reaction tower having a lower bottom portion with a cross-sectional area gradually decreasing toward the bottom, and the average particle size is 0.1 to 0.1.
A fluidizing medium in the form of solid powder particles with a diameter of 1 mm is housed in the cylindrical body, and a cyclic gas rich in hydrogen and carbon monoxide is introduced into the lower part of the cylindrical body. The fluidizing medium is fluidized into a fluidized bed, and continuous circulation of the fluidizing medium is caused in the fluidized bed separated by the partition, and the fluidization medium is separated by the partition. By feeding oxygen or oxygen-rich gas and combustible material into one of the beds to cause gasification and combustion, or by feeding high temperature combustion gas, the fluidizing medium forming the fluidized bed is heated to 800 to heated to 1200° C. and circulated the high temperature fluidizing medium to the other side of the fluidized bed separated by the partition, and 80% by weight of the high temperature fluidizing medium in the fluidized bed portion was heated to 1200° C. This is fine powdered iron oxide with a particle size of 0.1 mm or less and 10 to 5% by weight for this fine powdered iron oxide.
The particle size of heavy oil adjusted to 0% is 2 to 20 mm.
700 to 110 in the fluidized bed section made of the above-mentioned high temperature fluidizing medium.
The coarse particles of the mixture are rapidly heated in a temperature range of 0°C, and the accompanying sintering and reduction of the fine powdered iron oxide and the gasification of the heavy oil are rapidly and simultaneously caused, and the granules are collected at the bottom of the reaction tower. The granular reduced iron is discharged from the bottom, and the fluidizing medium separated from the granular reduced iron at the bottom of the reaction tower is moved upward in a fluidized bed state and mixed into one fluidized bed separated by the partition wall. This method is characterized by continuously circulating the fluidizing medium in the fluidized bed and rapidly causing reactions of sintering, reduction, and gasification of the coarse mixture of finely powdered iron oxide and heavy oil. An operating method that simultaneously sinters and reduces a mixture of powdered iron oxide and heavy oil and gasifies heavy oil using a single reaction tower in which a fluidizing medium circulates.