WO2012017916A1

WO2012017916A1 - System for conversion of carbon dioxide into carbon monoxide in ironworks

Info

Publication number: WO2012017916A1
Application number: PCT/JP2011/067279
Authority: WO
Inventors: 肇名井; 八島　勇; 菅野　明弘; 陽介柴田; 雄一妹尾; 和也木下
Original assignee: 三井金属鉱業株式会社
Priority date: 2010-08-04
Filing date: 2011-07-28
Publication date: 2012-02-09
Also published as: JP2012036029A

Abstract

A conversion system of the present invention is characterized in that a metal oxide having oxygen ion conductivity and reversible oxygen deficiency is brought into contact directly with a blast furnace gas or a converter furnace gas while heating to reduce carbon dioxide in the blast furnace gas or the converter furnace gas through a stoichiometric reaction, thereby producing carbon monoxide, and that waste heat generated in an ironworks is utilized as a heat source for the heating. This conversion system is also characterized in that a metal oxide having oxygen ion conductivity and reversible oxygen deficiency is brought into contact with carbon dioxide separated from a blast furnace gas or a converter furnace gas while heating to reduce carbon dioxide through a stoichiometric reaction, thereby producing carbon monoxide, and that waste heat generated in an ironworks is utilized as a heat source for the heating.

Description

Carbon dioxide to carbon monoxide conversion system in steelworks.

The present invention relates to a system for converting carbon dioxide to carbon monoxide at a steelworks.

A lot of blast furnace gas and converter gas containing carbon dioxide are generated along with the operation of steelworks. Carbon dioxide is a greenhouse gas, and it is important from the viewpoint of preventing global warming to efficiently reuse carbon dioxide in the blast furnace gas and converter gas. From an economic point of view, it is desirable to recover from the blast furnace gas and reuse it without using an apparatus for separating carbon dioxide from the blast furnace gas. Furthermore, when carbon dioxide is reused, it is desirable from the viewpoint of improving energy efficiency to reuse the waste heat generated from the steelworks. From the above, it is desirable to establish a system for reusing blast furnace gas and waste heat generated from steelworks.

As a technology to recover and reuse carbon dioxide in the industry that generates carbon dioxide, for example, oxygen gas generated by decomposing carbon dioxide gas into carbon monoxide gas and oxygen gas using iron oxide in an oxygen deficient state Thus, a technique has been proposed in which the oxygen-deficient iron oxide is returned to the original iron oxide and only the carbon monoxide gas is recovered (see Patent Document 1).

In addition to the above technique, as a technique for reusing carbon dioxide discharged from an incinerator or the like, Patent Document 2 uses a solid reaction membrane having an oxygen ion conductor made of CeO ₂ and a catalyst. A method for separating carbon dioxide into carbon monoxide and oxygen has been proposed.

Japanese Patent Laid-Open No. 5-68853 JP 2001-322958 A

According to the technique described in Patent Document 1, carbon monoxide gas is certainly generated from carbon dioxide gas. However, iron oxide has low oxygen ion conductivity, and if the surface is oxidized, the oxygen deficiency will come into contact with carbon dioxide gas even if oxygen deficiency exists inside the oxide. I can't. Therefore, in order to increase the conversion efficiency from carbon dioxide gas to carbon monoxide gas, it is necessary to use a large amount of iron oxide having oxygen deficiency, which is economically disadvantageous. In addition, in this document, utilization of waste heat generated from a factory or the like is not proposed, and it has not been established as a total carbon monoxide gas generation system using waste heat and exhaust gas.

In the technique described in Patent Document 2, since a noble metal catalyst is used to decompose carbon dioxide into carbon monoxide and oxygen, a large amount of carbon dioxide is generated. The factory is extremely disadvantageous economically. Further, it is not clear whether exhaust gas can be directly supplied to the reactor, and it has not been established as a carbon monoxide gas generation system using waste heat and exhaust gas.

Therefore, an object of the present invention is to provide a system for converting carbon dioxide to carbon monoxide in an ironworks that can eliminate the various disadvantages of the prior art described above.

The present invention is a system for converting carbon dioxide to carbon monoxide at a steel mill,
A metal oxide having oxygen ion conductivity and having reversible oxygen vacancies and a blast furnace gas or converter gas are brought into direct contact under heating, and the stoichiometric amount of carbon dioxide in the blast furnace gas or converter gas. It provides a conversion system that generates carbon monoxide by reduction through stochastic reactions and uses waste heat generated from steelworks as a heat source for heating.

Further, the present invention is a system for converting carbon dioxide to carbon monoxide at a steel mill,
A metal oxide having oxygen ion conductivity and reversible oxygen deficiency is brought into contact with carbon dioxide separated from blast furnace gas or converter gas under heating, and this carbon dioxide is reduced by a stoichiometric reaction. Thus, the present invention provides a conversion system that generates carbon monoxide and uses waste heat generated from a steelworks as a heat source for heating.

Further, the present invention provides a metal oxide having oxygen ion conductivity and having reversible oxygen deficiency and a blast furnace gas or converter gas of an ironworks directly in contact with the blast furnace gas or the A method for producing carbon monoxide in which carbon dioxide in a converter gas is reduced by a stoichiometric reaction to produce carbon monoxide, and the carbon monoxide that uses waste heat generated from a steel works as a heat source for heating. A manufacturing method is provided.

Further, the present invention is a method in which a metal oxide having oxygen ion conductivity and having a reversible oxygen deficiency is brought into direct contact with carbon dioxide separated from a blast furnace gas or converter gas of a steel mill under heating, A method for producing carbon monoxide in which carbon dioxide is reduced by a stoichiometric reaction to produce carbon monoxide, and a method for producing carbon monoxide using waste heat generated from a steel mill as a heat source for heating is provided. To do.

導入 By introducing the conversion system of the present invention into the steelworks, the amount of carbon dioxide emitted from the steelworks is reduced and the burden on the environment is reduced. In addition, carbon dioxide can be converted to carbon monoxide, which is a raw material such as C1 chemical material, and can be effectively reused. Furthermore, the energy efficiency of a steelworks can be improved by utilizing the waste heat generated from the steelworks.

FIG. 1 is a conceptual diagram of the conversion system of the present invention. FIG. 2 is a schematic diagram showing an apparatus suitably used in the conversion system of the present invention. FIG. 3 is a schematic diagram showing another apparatus suitably used in the conversion system of the present invention. FIG. 4 is a schematic view showing still another apparatus suitably used in the conversion system of the present invention. FIG. 5 is a schematic view showing an apparatus for generating carbon monoxide gas from blast furnace gas used in the examples. FIG. 6 is a schematic diagram showing an apparatus for synthesizing cerium oxide having oxygen deficiency used in the examples.

Hereinafter, the present invention will be described based on preferred embodiments with reference to the drawings. FIG. 1 schematically shows an integrated iron and steel works. In the steelworks, pig iron is produced in the blast furnace 1 using iron ore, coke and the like. The manufactured pig iron is supplied to the converter 2, and steel is produced in the converter 2. The coke used for the production of pig iron is produced by dry distillation of coal in the coke oven 3.

When producing pig iron in the blast furnace 1, blast furnace gas is generated. Further, when steel is produced in the converter 2, converter gas is generated. The main components of blast furnace gas are nitrogen, carbon monoxide and carbon dioxide. The blast furnace gas contains 52 to 53% by volume of nitrogen, 18 to 25% by volume of carbon monoxide, and 20 to 24% by volume of carbon dioxide. The main components of the converter gas are carbon monoxide and carbon dioxide. The converter gas contains 50 to 80% by volume of carbon monoxide and 15 to 17% by volume of carbon dioxide. Thus, both gases contain carbon dioxide as the main component. In the present invention, carbon dioxide contained in the blast furnace gas or converter gas is converted into a specific metal oxide (hereinafter, this metal oxide is referred to as “converter of carbon dioxide to carbon monoxide” or simply “ The carbon dioxide gas contained in these gases is converted into carbon monoxide gas by contacting with a heating agent. The reaction between the conversion agent and carbon dioxide gas is a stoichiometric reaction utilizing the reducing power of the conversion agent. That is, the conversion agent made of this metal oxide is not used as a catalyst, but as a reactant itself.

Specifically, in the present invention, as shown in FIG. 1, a blast furnace gas or a converter gas generated from an ironworks is directly supplied to the conversion device 4, and a conversion agent disposed in the conversion device 4 The carbon dioxide gas in the blast furnace gas or converter gas is converted into carbon monoxide gas by direct contact under heating. In this method, since the blast furnace gas or converter gas is directly supplied to the conversion device 4, it is not necessary to provide an apparatus for separating carbon dioxide from the blast furnace gas or converter gas, which is economically advantageous.

In addition to the above-described method, in the conversion system of the present invention, blast furnace gas or converter gas is supplied to the carbon dioxide separation and recovery device 5 to separate carbon dioxide, and this carbon dioxide gas is supplied to the conversion device 4. You may employ | adopt the method of making it contact with a conversion agent under a heating and converting carbon dioxide gas into carbon monoxide gas. In this case, when the carbon dioxide gas is composed of 100% by volume of carbon dioxide, it is ideal because it is not necessary to separate other gas in a subsequent process, but it may contain a small amount of other gas. When carbon dioxide gas contains other gas, it is preferable to use carbon dioxide gas containing 80% by volume or more of carbon dioxide. However, when the other gas is an oxygen-containing gas such as oxygen gas or water vapor, the ratio to the total amount of the supplied gas is preferably as small as possible. In the carbon dioxide separator 5, a known method used for separating carbon dioxide in the mixed gas, for example, an absorption method such as a chemical absorption method, a solid chemical absorption method, a physical absorption method, PSA (Pressure Swing Adsorption), Using TSA (Thermal Swing Adsorption), PTSA (Pressure and Temperature Swing Adsorption), etc., membrane separation method using polymer membrane, inorganic membrane, membrane-absorbing liquid hybrid, etc., cryogenic separation method, etc. Separate the carbon.

Even if any of the above-described methods is adopted, in the present invention, as the carbon dioxide gas source, only the blast furnace gas may be used, only the converter gas may be used, or the blast furnace gas and the converter are used. Both gases may be used.

As the conversion agent comprising the specific metal oxide, one having oxygen ion conductivity and having reversible oxygen vacancies is used. Since this conversion agent has a reversible oxygen deficiency, the conversion agent acquires the reducibility of carbon dioxide. A reversible defect | deletion is produced | generated when oxygen is forcibly extracted from a metal oxide by the process under strong reducing conditions. A reversible defect is a defect in which oxygen can be taken into a deficient site. For example, when the metal oxide is cerium oxide, which will be described later, in cerium oxide having a reversible defect, an unbalanced state of charge due to lack of oxygen is reduced to a part of tetravalent cerium to trivalent. To compensate. Trivalent cerium is unstable and easily returns to tetravalent. Therefore, by incorporating oxygen into the deficient site, trivalent cerium returns to tetravalent, and the charge balance is always kept at zero. By incorporating oxygen into the deficient site, the deficiency disappears, but oxygen deficiency is generated again by treatment under strong reducing conditions. “Reversible oxygen deficiency” is used in this sense.

The conversion agent comprising the metal oxide used in the present invention has oxygen ion conductivity as described above. The oxygen ion conductivity may be developed at a temperature at which the production method of the present invention is performed. Since this conversion agent has oxygen ion conductivity, almost all of the reversible oxygen vacancies present in this conversion agent can be effectively utilized for the reaction with carbon dioxide. The reason is as follows. That is, since the production method of the present invention is a reaction between a solid metal oxide and a gaseous carbon dioxide gas, the reaction mainly proceeds on the solid surface. And the oxygen deficiency which exists in the surface of a metal oxide couple | bonds with the oxygen in a carbon dioxide, The oxygen deficiency in this surface lose | disappears, and a carbon dioxide is converted into carbon monoxide. In this case, since the metal oxide has oxygen ion conductivity, oxygen associated with oxygen vacancies existing on the surface of the metal oxide is in the state of oxygen ions (O ²⁻ ). The oxygen vacancies disappear inside the metal oxide, and reversible oxygen vacancies are generated again on the surface of the metal oxide. By repeating this, almost all of the reversible oxygen vacancies present in the conversion agent can contribute to the reaction with carbon dioxide. On the other hand, for example, the iron oxide having oxygen vacancies described in Patent Document 1 described in the background section does not have oxygen ion conductivity, so that oxygen vacancies remain in the oxide. Even so, when all the oxygen vacancies present on the surface of the oxide disappear, the reactivity with carbon dioxide is greatly reduced.

The conversion agent comprising the metal oxide used in the present invention has oxygen ion conductivity and has the following advantages. That is, in this conversion agent, the reversible oxygen deficiency present in the converter can also contribute to the reaction with carbon dioxide, so that the reactivity with carbon dioxide can be achieved without excessively increasing the specific surface area of this conversion agent. Is hard to decline. Therefore, this conversion agent has a degree of freedom that it can be formed into a desired shape such as a granular shape, a pellet shape, a plate shape, or a cylindrical shape. On the other hand, a metal oxide that does not have oxygen ion conductivity, for example, an iron oxide having an oxygen vacancy described in Patent Document 1 described in the background section, has an oxygen vacancy existing therein. Since it hardly contributes to the reaction with carbon dioxide, it is necessary to increase the specific surface area of the oxide in order to effectively utilize the oxygen deficiency. In other words, it is indispensable to use in the state of fine powder, and due to this, the handleability and the degree of freedom in designing the conversion agent are low.

As described above, the conversion agent comprising the metal oxide used in the present invention is essential to have oxygen ion conductivity and to have reversible oxygen deficiency. As the oxide, for example, cerium oxide; a metal oxide having a fluorite structure represented by stabilized zirconia (substantially transformed into a cubic fluorite type at a temperature used for reaction with carbon dioxide). And an oxide having the fluorite structure substituted with a metal element that improves oxygen ion conductivity and oxygen deficiency; bismuth oxide and bismuth oxide with oxygen ion conductivity and oxygen deficiency those obtained by substituting a metal element that improves; general formula ABO ₃ (a and B is a metal element) oxide and oxygen a site and B site of the ABO ₃ has a perovskite structure represented by Those obtained by substituting a metal element that improves on conductivity and oxygen deficiency; oxide and the A ₂ B formula A ₂ B ₂ O ₅ (A and B represents a metal element) having a brownmillerite type structure represented by A metal element that improves oxygen ion conductivity and oxygen deficiency at the A site and B site of ₂ O ₅ ; general formula Ln ₁₀ Si ₆ O ₂₇ (Ln is La, Pr, Nd, Sm, Gd or Dy A rare earth silicate represented by: an oxide having a moznaite structure such as La ₂ Mo ₂ O ₉ ; a general formula Nd ₂ Ln ₂ O ₃ F ₆ (Ln is Y, Ce, Eu, Sm or Gd) Rare earth metal oxyfluoride represented by In particular, it is preferable to use cerium oxide from the viewpoints of high oxygen ion conductivity and reversible oxygen vacancies, and economical efficiency.

When cerium oxide is used as the conversion agent used in the present invention, the cerium oxide includes CeO _2-x (wherein Ce has a tetravalent and trivalent mixed valence, and x is 0.5 And a reversible oxygen deficiency and a fluorite-type crystal structure are preferably used. This cerium oxide is produced by firing a cerium-containing salt or a hydrate thereof in an oxidizing atmosphere such as air to produce cerium oxide (CeO ₂ ) having a fluorite-type structure, and then strongly reducing the cerium oxide. And reversible oxygen deficiency. Regarding the firing conditions, the temperature is preferably 500 to 1400 ° C., more preferably 600 to 1300 ° C., and the time is preferably 1 to 20 hours, more preferably 1 to 5 hours. In strong reduction, a hydrogen-containing atmosphere having a hydrogen concentration of not less than the lower explosion limit, preferably not less than 20% by volume, is used as the reducing atmosphere. Of course, the hydrogen concentration may be 100% by volume. The temperature is preferably 700 to 1100 ° C., more preferably 800 to 1050 ° C., and the time is preferably 1 to 3 hours, more preferably 1 to 2 hours. Details of such cerium oxide are described, for example, in WO2010 / 004963 relating to the earlier application of the present applicant.

Further, the cerium oxide is represented by CeO _2-x (wherein Ce has a trivalent and mixed valence of less than trivalent, and x represents a number of 0.5 to 0.7), and is reversible Those having a typical oxygen deficiency and having a superlattice structure similar to fluorite are also preferably used. Fluorite-like is a state in which the oxygen vacancies that initially exist at random are changed into ordered oxygen vacancies as oxygen escapes from the crystals of fluorite-type structures such as ordinary cerium oxide. Strictly speaking, it refers to a state that cannot be called a fluorite structure. Examples thereof include a magnetoplumbite type structure represented by PbFe ₁₂ O ₁₉ and a structure such as YBa ₂ Cu ₃ O _6.9 exhibiting superconductivity. The superlattice is a crystal lattice whose periodic structure is longer than the basic unit lattice by superimposing a plurality of types of crystal lattices. It can be confirmed, for example, by X-ray structural analysis that cerium oxide has a superlattice structure similar to fluorite. Cerium oxide having such a structure can be obtained by using an oxygen-containing cerium salt or a hydrate thereof as a precursor and directly reducing it. The reduction treatment is performed in a strong reducing atmosphere in which the concentration of a reducing gas such as hydrogen gas, acetylene gas, or carbon monoxide gas is high and heat treatment is performed at a high temperature. The reducing gas concentration is preferably not less than the lower limit of explosion to 100% by volume, more preferably 20% to 100% by volume. The treatment temperature is preferably 500 ° C. or higher, more preferably 700 ° C. to 1200 ° C., and still more preferably 1000 ° C. to 1050 ° C. The strongly reducing atmosphere is generally atmospheric pressure, but pressure conditions may be used instead. During the reduction treatment, a reducing gas atmosphere is maintained throughout the reaction system, and the reaction system is not exposed to the oxygen-containing gas atmosphere. The details of such cerium oxide are described in, for example, WO2008 / 140004 related to the applicant's previous application.

Further, the cerium oxide is represented by Ce ₂ O _3-x (wherein x represents a number of 0 or more and less than 1), has a reversible oxygen deficiency, and has a trigonal crystal structure. Those are also preferably used. Here, when x in the formula is 0, cerium has a trivalent valence, and when x is a number other than 0, cerium is a mixed valence that is trivalent and less than trivalent. Have This cerium oxide can be obtained by baking an acid-containing cerium salt or a hydrate thereof in a reducing atmosphere, for example, in a hydrogen atmosphere. For example, if the firing temperature is 1000 ° C., the firing temperature and firing time are 2 hours or longer, and if the firing temperature is higher than 1050 ° C., firing is performed for 1 hour or longer. Further, the cerium oxide is obtained by baking the cerium oxide containing acid in an air atmosphere at, for example, 600 ° C. for 1 hour or more, and converting the obtained cerium oxide having a fluorite-type crystal structure in a reducing atmosphere, for example, in a hydrogen atmosphere. For example, it can be obtained by firing at 1200 ° C. for 1 hour or longer.

In the present invention, the reaction between the conversion agent used and the blast furnace gas or converter gas is performed under heating. The heating temperature is set to, for example, 450 to 1000 ° C., particularly 450 to 800 ° C., particularly 500 to 750 ° C., to increase the conversion efficiency from carbon dioxide to carbon monoxide and to the action of carbon monoxide once generated. From the viewpoint of effectively preventing the conversion agent from being reduced and carbon dioxide from being regenerated. The amount of the conversion agent and the carbon dioxide gas in the blast furnace gas or the converter gas is such that the reaction of the conversion system is a stoichiometric reaction. In particular, it is preferable to supply carbon dioxide separated from blast furnace gas, converter gas, or blast furnace gas or converter gas so as to be 3 equivalents or more. For example, when the conversion agent is cerium oxide represented by CeO _2-x (x is as defined above), x / 2 mol of CO ₂ is equivalent to x / 2 mol of CO _2. To react. The above reaction conditions are similarly applied when carbon dioxide separated from blast furnace gas or converter gas is used as the carbon dioxide gas source.

In the present invention, waste heat generated from a steel mill is used as a heat source used for the heating. By using the waste heat generated from the steelworks as a heat source, the energy efficiency of the steelworks can be increased. In the present invention, specifically, the conversion device as a reaction system is heated by the following method (i) or (ii).

(I) Since the blast furnace 1 is usually heated to 1000 to 2000 ° C. and the converter 2 is usually heated to 1500 to 1800 ° C., the blast furnace gas and the converter gas are necessary for producing carbon monoxide from carbon dioxide. Have heat to be. Accordingly, the heat of the blast furnace gas or converter gas is used as a heat source, and the blast furnace gas or converter gas is blown into the converter 4 to heat the converter 4 as a reaction system. At this time, the blast furnace gas or the converter gas may be adjusted within the range of the heating temperature by a known means. When blast furnace gas or converter gas is used as a heat source, it is not necessary to use other heat sources, but other heat sources generated from the steelworks may be used as necessary.

(Ii) In steelworks, for example, blast furnaces, converters, coke ovens, etc. are heated to high temperatures, and a large amount of waste heat is generated. Using the generated waste heat, a heat medium such as water vapor, oil, and molten metal such as lead and sodium is heated, and the converter is heated by the heated heat medium. The heating temperature is adjusted so as to be within the range of the heating temperature.

The conversion agent can be contacted with carbon dioxide gas in various forms. For example, if the conversion device 4 is of a batch type, the powdered conversion agent can be allowed to stand (or filled) to perform the reaction, and the conversion agent can be granulated, pelletized, It is also possible to use a product molded into a lump shape, a plate shape, a honeycomb shape, a Raschig ring shape, a Bersaddle shape, or the like by leaving (or filling). On the other hand, if the conversion device 4 is a continuous type, a reaction surface that converts carbon dioxide into carbon monoxide with a dense film such as a cylinder, plate, or disk, and a regeneration surface that generates oxygen deficiency with a reducing gas. Any structure that is isolated from each other may be used.

The conversion agent in the conversion device 4 is oxidized by contact with carbon dioxide in the conversion device 4, and the conversion performance gradually decreases due to the oxidation. Therefore, it is preferable to regenerate and reuse the oxidized conversion agent by strong reduction. The regeneration of the conversion agent is achieved by causing oxygen deficiency by strong reduction under a high-temperature, high-concentration hydrogen gas atmosphere. However, it is not economically advantageous to use high-concentration hydrogen gas to strongly reduce the conversion agent. Therefore, it is desirable to use an economically advantageous reducing gas instead of high-concentration hydrogen gas. From this viewpoint, as a result of repeated studies, the inventors have surprisingly found that the conversion agent can be efficiently used by using the coke oven gas discharged from the coke oven as the reducing gas instead of the high concentration hydrogen gas. It was found that it can be regenerated. The main components of the coke oven gas are hydrogen and methane, and the coke oven gas contains about 50 to 60% by volume of hydrogen and about 25 to 30% by volume of methane. That is, the coke oven gas contains a sufficient amount of hydrogen necessary for the strong reduction of the conversion agent. In addition, the coke oven gas hardly contains water vapor, oxygen, or the like, which is a substance that inhibits the strong reduction of the conversion agent. Accordingly, the coke oven gas is suitable for generating oxygen deficiency in the conversion agent that has lost oxygen deficiency. Therefore, in the present invention, the coke oven gas generated from the coke oven 3 is supplied to the conversion device 4, and the coke oven gas and the conversion agent are brought into direct contact under heating to regenerate the conversion agent having oxygen deficiency. It is preferable.

As described above, the coke oven gas generated from the coke oven 3 is supplied to the conversion device 4 and brought into direct contact with the conversion agent. That is, it is not necessary to separate the hydrogen gas in the coke oven gas. The ability to directly use coke oven gas is economically advantageous because it eliminates the need to provide equipment and equipment for treating coke oven gas.

The reaction between the conversion agent and the coke oven gas is performed under heating. The heating temperature is preferably set to 700 to 1200 ° C., particularly 800 to 1200 ° C., particularly 900 to 1200 ° C., from the viewpoint of increasing the reduction efficiency by the hydrogen gas contained in the coke oven gas.

As the heat source used for heating, it is advantageous to use waste heat generated from the steelworks. By using the waste heat generated from the steelworks as a heat source, the energy efficiency of the steelworks can be further enhanced. In the present invention, the conversion device 4 as a reaction system can be heated by the following method (a) or (b).

(A) The coke oven is usually heated to 1200-1300 ° C. Thus, the coke oven gas discharged from the coke oven has the heat required to strongly reduce the oxidized conversion agent. Therefore, the heat of the coke oven gas is used as a heat source, and the coke oven gas is blown into the converter 4 to heat the converter 4 as a reaction system. At this time, the temperature of the coke oven gas may be adjusted within the range of the heating temperature by a known means. When coke oven gas is used as a heat source, it is not necessary to use other heat sources, but other heat sources may be used as necessary.

(B) In steelworks, for example, blast furnaces, converters, coke ovens, etc. are heated to high temperatures, and a large amount of waste heat is generated. Using the generated waste heat, a heat medium such as water vapor, oil, and molten metal such as lead and sodium is heated, and the converter is heated by the heated heat medium. The heating temperature is adjusted so as to be within the range of the heating temperature.

The production of carbon monoxide from carbon dioxide using a conversion agent and (b) regeneration of the conversion agent that has lost oxygen deficiency by coke oven gas may be performed simultaneously or separately. Also good. Hereinafter, the

conversion apparatuses

10, 20, and 30 that can simultaneously perform (A) and (B) will be described. In the description of

converters

10, 20, and 30, blast furnace gas, converter gas, or carbon dioxide separated from blast furnace gas or converter gas can be used as a raw material for generating carbon monoxide. Hereinafter, the case where blast furnace gas is used will be described.

FIG. 2 schematically shows a carbon monoxide converter suitably used in the present invention. The conversion device 10 shown in the figure is a continuous type and has a double-pipe structure. Specifically, the conversion device 10 shown in FIG. 1 includes an outer tube 11 and an inner tube 12 disposed in the outer tube 11. A heating device 13 using a heat medium heated by waste heat as a heat source is disposed in the inner tube 12. The inner tube 12 contains the conversion agent. In this apparatus, blast furnace gas is circulated in the space between the outer tube 11 and the inner tube 12. While the blast furnace gas circulates in this space, carbon dioxide in the blast furnace gas reacts with the conversion agent contained in the inner pipe 12 to generate carbon monoxide.

In the converter 10 shown in FIG. 2, in addition to circulating the blast furnace gas in the space between the outer tube 11 and the inner tube 12, the coke oven gas is circulated in the inner tube 12. . As a result, oxygen is extracted from the conversion agent oxidized by contact with the carbon dioxide gas in the blast furnace gas, and lost oxygen deficiency is generated again.

In the converter 10 shown in FIG. 2, when blast furnace gas, converter gas, or coke oven gas is used as a heat source, high-temperature blast furnace gas, converter gas, or coke oven gas is circulated in each of the above spaces. Here, the high temperature means having sufficient heat energy to generate carbon monoxide from carbon dioxide and sufficient to strongly reduce the conversion agent that has lost oxygen deficiency (hereinafter referred to as high temperature). Sometimes used in this sense.) At this time, it is not necessary to use the heating device 13, but it may be used as necessary. When a heat medium heated by waste heat is used as the heat source, the converter 10 is heated by a heating device 13 that is disposed inside the inner tube 12 and uses the heat medium as a heat source. Further, instead of installing a heating device inside the inner tube 12, a heating device may be arranged around the outer tube 11 to heat the conversion device 10. However, in general, since the temperature at which oxygen is forcibly extracted from the oxidized conversion agent is higher than the temperature at which the reaction between carbon dioxide gas and the conversion agent occurs, when using a heating device as a heat source, Arranging the heating device 13 inside the inner tube 12 is advantageous in terms of ease of forced extraction of oxygen.

In the converter 10 shown in FIG. 2, the flow direction of the blast furnace gas and the flow direction of the coke oven gas are the same direction, but instead, the flow direction of the blast furnace gas and the flow direction of the coke oven gas are opposite directions. It may be. As a modification of the conversion device 10 shown in FIG. 2, the coke oven gas may be circulated in the space between the outer tube 11 and the inner tube 12, and the blast furnace gas may be circulated in the inner tube 12. it can.

Moreover, in the converter 10 shown in FIG. 2, although blast furnace gas is distribute | circulated as a carbon dioxide source, in addition to blast furnace gas, converter gas, the mixed gas of blast furnace gas and converter gas, or blast furnace gas or Carbon dioxide gas separated from the converter gas can be circulated (the same applies to FIGS. 3 and 4 described below).

The conversion apparatus 20 shown in FIG. 3 includes two batch-

type reaction apparatuses

21 and 22. Furthermore, the conversion device 20 includes a switching valve 23. The switching valve 23 has

input parts

23a and 23b connected to a blast furnace gas source and a coke oven gas source, respectively. Furthermore, the switching valve 23 has

output parts

23c and 23d connected to the

reaction devices

21 and 22, respectively. The conversion agent 24 can be arranged in each of the reaction apparatuses 21 and 22. A heating device 25 is disposed around each of the

reaction devices

21 and 22.

3, the blast furnace gas or the coke oven gas is alternatively and simultaneously supplied to each of the reaction apparatuses 21 and 22 via the switching valve 23. In addition to this, the type of gas supplied to each of the

reactors

21 and 22 can be switched by switching the switching valve 23.

When the converter 20 shown in FIG. 3 is operated, first, the switching valve 23 is set to the position shown in FIG. 3, the blast furnace gas is supplied to the second reactor 22, and the coke oven gas is supplied to the first reactor. 21 to be supplied. In this way, in the first reaction device 21, the conversion agent 24 placed inside is strongly reduced, oxygen is forcibly extracted, and a reversible oxygen deficiency is generated in the conversion agent 24. . On the other hand, in the second reactor 22, carbon monoxide is generated by the reaction between carbon dioxide in the blast furnace gas and the conversion agent 24, and the number of oxygen vacancies in the conversion agent 24 gradually decreases. When the amount of carbon monoxide produced in the second reactor 22 decreases, the switching valve 23 is switched so that the blast furnace gas is supplied to the first reactor 21 and the coke oven gas is supplied to the second reactor 22. To be. Since the conversion agent 24 that is stationary in the first reactor 21 has high activity that is not in contact with the carbon dioxide gas in the blast furnace gas, by contacting it with the carbon dioxide gas in the blast furnace gas, The amount of carbon monoxide produced starts to increase. On the other hand, in the second reactor 22, the conversion agent 24 whose activity is reduced due to a decrease in the number of oxygen vacancies is strongly reduced, oxygen is forcibly extracted, and a reversible oxygen vacancy is generated again in the conversion agent 24. .

3, when blast furnace gas, converter gas, or coke oven gas is used as a heat source, high-temperature blast furnace gas, converter gas, or coke oven gas is supplied to each of the reactors described above. At this time, although it is not necessary to use the heating apparatus 25, you may use it as needed. When a heat medium heated by waste heat is used as a heat source, each of the

reaction devices

21 and 22 is heated using a heating device 25 that uses the heat medium as a heat source. The heating temperatures of the first reactor 21 and the second reactor 22 may be set to the same or different temperatures. Generally, since the temperature at which oxygen is forcibly extracted from the oxidized conversion agent 24 is higher than the temperature at which the reaction between carbon dioxide gas and the conversion agent 24 occurs, the reactor for supplying coke oven gas is used. Is preferably set higher than the heating temperature of the reactor that produces carbon monoxide.

In this way, the reaction between the carbon dioxide gas in the blast furnace gas and the conversion agent 24 is alternately performed by the first reaction device 21 and the second reaction device 22, so that the conversion agent 24 is regenerated and monoxide is regenerated. Carbon can be produced semi-continuously. In addition, in the converter 20 shown in FIG. 3, although two batch type reactors were used, it may replace with this and may use three or more reactors.

The conversion device 30 shown in FIG. 4 has a structure in which plate-like bodies 31 including the conversion agent and plate-like separators 32 are alternately stacked. A plurality of convex portions 33 and concave portions 34 extending in one direction are alternately arranged on each surface of each separator 32. As a result, a space is formed between the plate-like body 31 and the pair of separators that are opposed to each other with the gas formed by the concave portions 34. Moreover, although not shown in figure, the converter 30 is provided with the heating apparatus arrange | positioned around the stack structure.

When the conversion device 30 shown in FIG. 4 is operated, the concave portion 34a located on the opposing surface between the one separator 32a and the plate-like body 31 in the two separators 32a and 32b facing each other with the plate-like body 31 interposed therebetween. Circulate blast furnace gas. While the blast furnace gas circulates in the recess 34a, the carbon dioxide gas in the blast furnace gas reacts with the conversion agent contained in the plate 31 to generate carbon monoxide. In addition to this, the coke oven gas is configured to circulate through the recess 34b located on the opposing surface of the other separator 32b and the plate-like body 31. As a result, oxygen is extracted from the conversion agent oxidized by contact with the carbon dioxide gas in the blast furnace gas, and lost oxygen deficiency is generated again. In this way, when the conversion device 30 is used, after the conversion agent is brought into contact with carbon dioxide gas in the blast furnace gas to generate carbon monoxide, as in the conversion device 10 shown in FIG. 2 described above. The conversion agent oxidized by contact with carbon dioxide gas can be brought into contact with hydrogen in coke oven gas to perform strong reduction to regenerate the conversion agent.

In each separator 32 of the conversion device 30 shown in FIG. 4, the extending direction of the convex portion 33 and the concave portion 34 formed on one surface and the other surface is shifted by 90 degrees. However, the extending direction of the convex portion 33 and the concave strip portion 34 formed on each surface of the separator 32 is not limited to this. For example, the extending direction of the convex part 33 and the concave line part 34 formed on each surface of the separator 32 may intersect at an angle other than 90 degrees, or the same direction. When the extending direction of the convex part 33 and the concave line part 34 formed on each surface of the separator 32 is the same direction, the direction of the gas flowing through the concave line part 34 on one surface side of the separator 32 and the other The direction of the gas flowing through the groove 34 on the surface side may be the same direction or the opposite direction.

In the converter 30 shown in FIG. 4, when blast furnace gas, converter gas, or coke oven gas is used as a heat source, high temperature blast furnace gas or converter gas is supplied to the recess 34 a and high temperature coke oven gas is supplied. It supplies to the concave part 34b. When a heating medium heated by waste heat is used as a heat source, a converter 30 (not shown) using a heated heating medium disposed around the stack structure is used to convert the converter 30. Heat.

Note that, regarding the conversion devices 30 and 40 shown in FIG. 3 and FIG. 4, the explanation about the conversion device 20 shown in FIG.

Hereinafter, the present invention will be described in more detail with reference to examples. However, the scope of the present invention is not limited to such examples.

Production of cerium oxide having reversible oxygen vacancies (a) Synthesis of cerium oxide without oxygen vacancies 100 g of cerium carbonate was left standing in a heating furnace, and baked by heating while circulating air. Heating was started from room temperature, heated at a rate of temperature increase of 10 ° C./min, reached 1000 ° C., and this temperature was maintained for 1 hour. Then, it naturally left to cool. The air flow rate was 1000 SCCM. Thus, a porous body of cerium oxide having no oxygen deficiency was obtained. Measurement by XRD confirmed that this cerium oxide was represented by CeO ₂ and had a fluorite-type crystal structure. This cerium oxide was pulverized by a ball mill.
(B) Synthesis of cerium oxide having oxygen vacancies The cerium oxide (50 g) obtained in (a) above is left in an atmosphere-controlled heating furnace and heated while flowing 100% by volume of hydrogen gas. Reduction was performed. Heating was started from room temperature, heated at a rate of temperature increase of 10 ° C./min, and after reaching 1000 ° C., this temperature was maintained for 1 hour. Then, it naturally left to cool. The circulation amount of hydrogen gas was 1000 SCCM. In this way, cerium oxide having reversible oxygen deficiency was obtained. As a result of measurement by XRD, it was confirmed that this cerium oxide has a fluorite-type crystal structure. As a result of elemental analysis, this cerium oxide was represented by Ce (IV, III) O _1.75 .

(2) Production of carbon monoxide gas from blast furnace gas An experiment was conducted using the model blast furnace gas and the apparatus shown in FIG. The composition of the model blast furnace gas was 53% by volume of nitrogen gas, 21% by volume of carbon dioxide gas, 24% by volume of carbon monoxide gas, and 2% by volume of hydrogen gas. The tubular furnace shown in FIG. 5 was installed in a glove box with a nitrogen gas atmosphere. In the tubular furnace, 8.5 g of cerium oxide powder having reversible oxygen vacancies obtained in the preceding item (1) is placed. First, the valve V5 was closed, all other valves were opened, and the inside of the tubular furnace was vacuumed. In this state, the valve V1 was closed and the tubular furnace was heated to 750 ° C. Next, after the valves V2 and V3 were closed, the suction in the tubular furnace was stopped. The valve V4 was closed and the model blast furnace gas was supplied into the tubular furnace. The supply was continued until the pressure in the tubular furnace reached atmospheric pressure. The valve V1 was closed and left for 1 hour. At this time, the stoichiometric ratio of carbon dioxide gas in the model blast furnace gas to cerium oxide having reversible oxygen deficiency was set to 1: 1 (that is, 1 equivalent as described above). Thereafter, the valve V2 was opened, and nitrogen gas was supplied into the tubular furnace until the gas recovery bag was slightly expanded. Next, the valve V2 was closed and the gas recovery bag was heat sealed and separated from the tube. In this state, the temperature of the tubular furnace was lowered and cooled to room temperature. After completion of cooling, the valve V1 was opened and nitrogen gas was supplied into the tubular furnace. The supply was continued until the pressure in the tubular furnace reached atmospheric pressure. Finally, the valves V3 and V5 were opened, and carbon monoxide in the tubular furnace was extruded with nitrogen gas. The gas after reaction collected in the gas collection bag was qualitatively and quantitatively analyzed using gas chromatography. As a result, the conversion rate from carbon dioxide to carbon monoxide was 50%. This conversion rate is defined by the following equation.

(3) Regeneration of cerium oxide with coke oven gas An experiment was conducted using the model coke oven gas and the apparatus shown in FIG. The composition of the model coke oven gas is 56% by volume of hydrogen gas, 30% by volume of methane gas, 3% by volume of acetylene, 6% by volume of carbon monoxide gas, 2.5% by volume of carbon dioxide gas, and 2% of nitrogen gas. 0.5% by volume. The tubular furnace shown in FIG. 6 was installed in a glove box with a nitrogen gas atmosphere. In the tubular furnace, 8.5 g of cerium oxide powder having lost oxygen deficiency produced in the preceding item (2) is left standing. First, bubble V2 was opened, then bubble V1 was opened, and strong reduction was performed by heating while circulating the model coke oven gas. Starting from room temperature, heating was performed to reach 1000 ° C. in 3 hours. After reaching 1000 ° C., this temperature was maintained for 2 hours. Thereafter, the model coke oven gas was allowed to cool naturally to room temperature while circulating. The flow rate of model coke oven gas was 500 SCCM. In this way, cerium oxide having oxygen deficiency was regenerated. As a result of measurement by XRD, it was confirmed that this cerium oxide has a fluorite-type crystal structure. As a result of elemental analysis, this cerium oxide was represented by Ce (IV, III) O _1.75 . Thereafter, the obtained cerium oxide was subjected to the same operation as in the previous item (2), and the conversion rate of this cerium oxide from carbon dioxide to carbon monoxide was calculated. The conversion rate was 50%.

Claims

A system for converting carbon dioxide to carbon monoxide at a steelworks,
A metal oxide having oxygen ion conductivity and having reversible oxygen vacancies is directly brought into contact with a blast furnace gas or converter gas under heating, and the carbon dioxide in the blast furnace gas or converter gas is chemically treated. A conversion system that produces carbon monoxide by reduction through a stoichiometric reaction, and uses waste heat generated from steelworks as a heat source for heating.
A system for converting carbon dioxide to carbon monoxide at a steelworks,
A metal oxide having oxygen ion conductivity and reversible oxygen deficiency is brought into contact with carbon dioxide separated from blast furnace gas or converter gas under heating, and this carbon dioxide is reduced by a stoichiometric reaction. Conversion system that produces carbon monoxide and uses waste heat generated from steelworks as a heat source for heating.
The metal oxide oxidized by contact with carbon dioxide contained in the blast furnace gas or converter gas is brought into direct contact with the coke oven gas generated from the ironworks under heating, and is strongly reduced by hydrogen in the coke oven gas. The conversion system according to claim 1 or 2, wherein the metal oxide is regenerated and waste heat generated from the steelworks is used as a heat source for heating.
The conversion system according to claim 1, wherein the heat of the blast furnace gas or the converter gas is used as a heat source, and the reaction system is directly heated by blowing the blast furnace gas or the converter gas into the reaction system.
The conversion system according to claim 3, wherein the heat of the coke oven gas is used as a heat source, and the reaction system is directly heated by blowing the coke oven gas into the reaction system.
The conversion system according to any one of claims 1 to 3, wherein the heat medium is heated using waste heat generated from the steel works, and the reaction system is heated using the heated heat medium.
The conversion system according to any one of claims 1 to 6, wherein the metal oxide is made of cerium oxide having reversible oxygen vacancies.
The metal oxide is represented by CeO 2-x (wherein Ce has a tetravalent and trivalent mixed valence, and x represents a positive number less than 0.5) and is reversible. The conversion system according to claim 7, comprising cerium oxide having an oxygen deficiency and a fluorite-type crystal structure.
The metal oxide is represented by CeO 2-x (wherein Ce has trivalent and mixed valences less than trivalent, x represents a number of 0.5 to 0.7), The conversion system according to claim 7, comprising cerium oxide having a reversible oxygen deficiency and a superlattice structure similar to fluorite.
The metal oxide is represented by Ce 2 O 3-x (x represents a number of 0 or more and less than 1), has a reversible oxygen deficiency, and has a trigonal crystal structure. The conversion system according to claim 7, comprising:
A metal oxide having oxygen ion conductivity and having reversible oxygen vacancies is directly brought into contact with a blast furnace gas or a converter gas of a steel mill under heating, and the blast furnace gas or the dioxide gas in the converter gas is contacted. A method for producing carbon monoxide in which carbon monoxide is produced by reducing carbon by a stoichiometric reaction, and the waste heat generated from an ironworks is used as a heat source for heating.
A metal oxide having oxygen ion conductivity and having reversible oxygen deficiency is brought into direct contact with carbon dioxide separated from the blast furnace gas or converter gas of a steel mill under heating, and this carbon dioxide is stoichiometrically. A method for producing carbon monoxide, which generates carbon monoxide by reduction by a stochastic reaction, and uses waste heat generated from a steel mill as a heat source for heating.