Pulverized coal combustion method

Abstract: The method including the steps of separating pulverized coal mixture gas (2) ejected from a vertical type coal grinder containing a rotary type classifier (1) therein into thick mixture gas (4) and thin mixture gas (5) by means of a distributor (3), and injecting these thick and thin mixture gases respectively through separate burner injecting ports (6,7) into a same furnace (8) to make them burn, is improved so as to reduce both an unburnt fuel content in ash and a nitrogen oxide concentration in exhaust gas while maintaining excellent ignition characteristic. The improvements reside in that an air-to-fuel ratio of the thick mixture gas is chosen at 1 - 2, while an air-to-fuel ratio of the thin mixture gas is chosen at 3 - 6, and the range of a degree of pulverization of the pulverized coal is regulated at 100 mesh residue 1.5% or less. The degree of pulverization of the pulverized coal fed to ihe distributor is regulated either by adjusting a rotational speed of the rotary type classifier (65) or by adjusting the angles formed between classifying vanes (75) rotating about the axis of the rotary type classifier and the direction of rotation.

Description: Field of the Invention: The present invention relates to a method for combustion of pulverized coal, and more particularly to a method for combustion of pulverized coal including the steps of separating pulverized coal mixture gas ejected from a vertical type coal grinder containing a rotary type classifier therein into thick mixture gas and thin mixture gas by means of a distributor, and injecting these thick and thin mixture gases respectively through separate burner injection ports into a same furnace to make them burn. Description of the Prior Art: One example of an apparatus for carrying out the method for combustion of pulverized coal in the prior art is shown in a system diagram in Fig. 8. In this figure, reference numeral 01 designates a vertical type coal grinder containing a stationary type classifier therein, numeral 2 designates a pulverized coal pipe, numeral 3 designates a distributor, numeral 4 designates a thick mixture gas feed pipe, numeral 5 designates a thin mixture gas feed pipe, numeral 6 designates a thick mixture gas burner, numeral 7 designates a thin mixture gas burner, and numeral 8 designates a boiler furnace. Pulverized coal mixture gas consisting of coal pulverized finely by the vertical type coal grinder 01 and primary air for combustion is, after ejected from the coal grinder and introduced into the pulverized coal pipe 2, separated into thick mixture gas and thin mixture gas by the distributor 3. The thick mixture gas passes through the thick mixture gas feed pipe 4 and is injected from the thick mixture gas burner 6 into the boiler furnace 8 to burn. On the other hand, the thin mixture gas passes through the thin mixture gas feed pipe 5 and is injected from the thin mixture gas burner 7 into the boiler furnace 8 to burn. In such a pulverized coal combustion method in the prior art, by separating pulverized coal mixture gas into thick mixture gas and thin mixture gas and making them burn separately, an effect of suppressing production of nitrogen oxides (NO x ) in the course of combustion reaction is obtained, and therefore, in recent low NO x combustion apparatuses, mostly such method is employed. One example of a vertical type coal grinder 01 containing a stationary type classifier is shown in a longitudinal cross-section view in Fig. 9. In this figure, material to be ground such as lumped powder coal or the like charged through a feed pipe 10 is applied with load on a rotary table 20 by a grinding roller 30 and is thus ground into pulverized coal, and it is spattered towards the outer circumference of the same rotary table 20. On the other hand, hot air is sent from a hot air inlet port 40 at the below through a blow-up portion 50 into a mill. The above-mentioned pulverized coal spattered towards the outer circumference of the rotary table 20 is blown up to the above by this hot air, that is, by this carrier gas, passes through stationary vanes 80 and is fed into a stationary type classifier 60, where it is separated into fine powder and coarse powder. Then the fine powder is taken out through a pulverized coal pipe 110, while the coarse powder falls along the inner circumferential wall of the stationary type classifier 60 onto the rotary table 20 and is ground again. In the above-described pulverized coal combustion method in the prior art, in order to reduce unburnt loss of a boiler, it is desirable to make a degree of pulverized coal to be burnt as fine as possible. However, if a degree of pulverization is made excessively high, degradation of capability of a grinder and increase of power consumption would become remarkable, and moreover, problems such as generation of vibration would be involved. Therefore, in the pulverized coal combustion method making use of a vertical type coal grinder containing a stationary type classifier therein, it is a common practice to operate the machine with a degree of pulverization of 200 mesh pass 80% or less. A general characteristic of a vertical type coal grinder containing a stationary type classifier therein is shown in Fig. 10. As shown in this figure, in the case where pulverization has been effected by the above-mentioned grinder up to a degree of pulverization of about 200 mesh pass 80%, in the pulverized coal are contained coarse particles of 100 mesh or larger by about 2.4%, and this is an inevitable phenomenon in view of a characteristic of a stationary type classifier. Now, the mixture gas of pulverized coal ground in the above-described manner is separated into thick mixture gas and thin mixture gas by means of a distributor. However, since the distributor utilizes a classifying effect based on inertial forces, in view of its operating characteristic, it is inevitable that a most part of the above-mentioned coarse particles of 100 mesh or larger would flow to the side of thick mixture gas. One example of the configuration of the above-described distributor is shown in Fig. 11. In this figure, pulverized coal mixture gas introduced into the distributor through a pulverized coal mixture gas inlet 3a is separated into thick mixture gas and thin mixture gas due to inertial forces, and they are ejected respectively through a thick mixture gas outlet 3b and a thin mixture gas outlet 3c. In the above-mentioned distributor, while coarse particles of 100 mesh or larger are contained by 2.5% in the pulverized coal at the inlet, 95% or more of them is ejected through the thick mixture gas outlet 3b. The thick mixture gas burner suppresses production of nitrogen oxides by burning pulverized coal within a low oxygen content atmosphere containing air less than a theoretical combustion air amount, but in the above-described thick mixture gas is contained a large amount of coarse particles of 100 mesh or larger, these coarse particles cannot fully burn out within the low oxygen content atmosphere, and a most part of them would remain as an unburnt content. Therefore, an unburnt ash component is high, and accompanying therewith there was a problem that unburnt loss of a boiler was high. A general relation between a degree of pulverization and an unburnt ash content is shown in Fig. 12. On the other hand, from a view point of effective utilization of coal burnt ash, often the necessity for suppressing an unburnt ash content to less than a regulated value would arise, and in such cases since operations for increasing a surplus air proportion are necessitated, there was a problem that production of nitrogen oxides could not be effectively suppressed. Relations between a surplus air proportion and an NO x content as well as an unburnt ash content in the above-described combustion method in the prior art are shown in Fig. 13. Furthermore, in Fig. 7 is shown by a dash line a relation between an unburnt ash content and an NO x content in the pulverised coal combustion method in the prior art. Among these contents, if one is reduced, then the other tends to increase, and so, in order to reduce both the unburnt ash content and the NO x content, any novel technique is necessary. In addition, the relations between a concentration ratio of the thick mixture gas to the thin mixture gas and an NO x content as well as an unburnt ash content have the tendencies as shown in Fig. 14, and if the concentration ratio is increased, the NO x content is lowered but the unburnt content is increased. Accordingly, in order to maintain both the NO x content and the unburnt ash content at proper values, it is necessary to arbitrarily and automatically control the aforementioned concentration ratio according to variations of a boiler load and a kind of coal, but in the pulverised coal combustion method in the prior art, such control was impossible. In the EP-A-0 225 157 there is described a method and apparatus for reducing NO x emissions from coal furnaces. This method includes the steps of separating the pulverised coal mixed with air into two streams, one fuel rich and one fuel lean. These streams are then introduced into the furnace via corresponding separate burners. In order to split the two streams the apparatus comprises a concentrator which includes a rotary classifier and is arranged between a conventional mill and the furnace. SUMMARY OF THE INVENTION: It is therefore one object of the present invention to provide a novel pulverized coal combustion method that is free from the above-mentioned shortcomings in the prior art. A more specific object of the present invention is to provide a pulverized coal combustion method in which an unburnt ash content and a concentration of nitrogen oxide in an exhaust gas are both low, and an ignition characteristic is excellent. According to one embodiment of the present invention, there is provided a pulverized coal combustion method including the steps of separating pulverized coal mixture gas ejected from a vertical type coal grinder containing a rotary type classifier therein into thick mixture gas and thin mixture gas by means of a distributor, and injecting these thick and thin mixture gases respectively through separate burner injection ports into a same furnace to make them burn, improved in that an air-to-coal mass flow rate ratio of the thick mixture gas is chosen at 1 - 2, while an air-to-coal mass flow rate ratio of the thin mixture gas is chosen at 3 - 6, and the range of a degree of pulverisation of the pulverised coal is regulated at 100 mesh residue 1.5% or less. According to another embodiment of the present invention, there is provided the above-featured pulverized coal combustion method, wherein the degree of pulverization of the pulverized coal fed to the distributor is regulated by adjusting a rotational speed of the rotary type classifier. According to still another embodiment of the present invention, there is provided the first-featured pulverised coal combustion method, wherein the degree of pulverization of the pulverised coal fed to the distributor is regulated by adjusting the angles formed between classifying vanes rotating about the axis of the rotary type classifier and the direction of rotation. An operation characteristic of a vertical type coal grinder containing a rotary type classifier therein is shown in Fig. 5. As shown in this figure, in the case where pulverization has been effected in this coal grinder under the condition of 200 mesh pass 85%, coarse particles of 100 mesh or larger in the pulverized coal are reduced up to 0.1%. In combustion within a low oxygen content atmosphere, a possibility of coarse particles of 100 mesh or larger remaining as an unburnt content is high as shown in Fig. 13. On the other hand, in the case where coal burnt ash is used as a raw material of cement, generally it is necessary to make an unburnt content in the coal burnt ash 5% or less. While the amount of an unburnt content in the coal burnt ash is different depending upon a degree of pulverization, a kind of coal and the like, as shown in Fig. 20 by regulating a degree of pulverization at 100 mesh residue 1.5% or less, an unburnt content in the coal burnt ash can be always made to be 5% or less. Taking into the aforementioned fact into consideration, according to the present invention, the range of a degree of pulverization of the pulverized coal is regulated at 100 mesh residue 1.5% or less. Since the amount of coarse particles of 100 mesh or larger can be greatly reduced to as small as 100 mesh residue 1.5% or less by employing the grinding machine containing a rotary type classifier therein, unburnt loss of a boiler can be remarkably decreased as compared to the prior art. In addition, in the event that unburnt loss of the same order as that in the prior art is allowed, the machine can be operated at a lower surplus air proportion in Fig. 13 by the amount corresponding to the reduction of coarse particles of 100 mesh or larger, and hence a nitrogen oxide concentration in a boiler exhaust gas can be greatly reduced as compared to that in the prior art. In addition, by adjusting a rotational speed of a rotary type classifier and angles formed between classifying vanes and the direction of rotation, a degree of pulverization can be arbitrarily and automatically changed. Concentration ratios of the thick and thin mixture gases at the outlet when pulverized coal having different degrees pulverization has been fed to the distributor shown in Fig. 11, are shown in Fig. 15. In the case where a size of pulverized particle is small, since a classifying effect into thick and thin mixture gases due to a centrifugal force becomes small, the concentration ratio would become small as shown in this figure. Accordingly, by adjusting a rotational speed of the rotary type classifier and angles formed between classifying vanes and the direction of rotation, an NO x content and an unburnt content can be arbitrarily and automatically regulated. The present invention will become more apparent by reference to the following description of one preferred embodiment of the invention taken in conjunction with the accompanying drawings. DESCRIPTION OF THE DRAWINGS: In the accompanying drawings: Fig. 1 is a system diagram showing an apparatus for carrying out one preferred embodiment of the present invention; Fig. 2 is a longitudinal cross-section view of a vertical type coal grinder containing a rotary type classifier therein, which is available in the apparatus for carrying out the preferred embodiment of the present invention; Fig. 3 is a perspective view partly cut away of the same rotary type classifier; Fig. 4 is a transverse cross-section view taken along chain line IV-IV in Fig. 2 as viewed in the direction of arrows; Fig. 5 is a diagram showing a characteristic of a vertical type coal grinder containing a rotary type classifier therein; Fig. 6 is a diagram showing relations between a (combustion primary air/coal) ratio and an NO x content, a flame propagation speed and an unburnt ash content in the pulverized coal combustion method according to the aforementioned preferred embodiment; Fig. 7 is a diagram showing relations between an NO x content and an unburnt ash content as compared the case of the combustion method according to the aforementioned preferred embodiment and the case of the combustion method in the prior art; Fig. 8 is a system diagram showing an apparatus for carrying out one example of a pulverized coal combustion method in the prior art; Fig. 9 is a longitudinal cross-section view showing one example of a vertical type coal grinder containing a stationary type classifier therein; Fig. 10 is a diagram showing a characteristic of a vertical type coal grinder containing a stationary type classifier therein; Fig. 11 is a cross-section view showing one example of the configuration of a distributor; Fig. 12 is a diagram showing a general relation between a degree of pulverization and an unburnt ash content; Fig. 13 is a diagram showing relations between a surplus air proportion, and an NO x content and an unburnt ash content in the combustion method in the prior art; Fig. 14 is a diagram showing relations between various concentration ratios of thick mixture gas to thin mixture gas, and an NO x content and an unburnt ash content in the above-described preferred embodiment of the present invention; Fig. 15 is a diagram showing a relation between a degree of pulverization of pulverized coal at the inlet of the distributor in the above-described preferred embodiment, and a concentration ratio of thick mixture gas to thin mixture gas at its two outlets; Fig. 16 is a diagram showing variation of a degree of pulverisation in the event that a rotational speed of the classifier is varied in the aforementioned preferred embodiment; Fig. 17 is a diagram showing relations between a rotational speed of the classifier, and an NO x content and an unburnt ash content in the same preferred embodiment; Fig. 18 is a diagram showing relations between an air-to-coal mass flow rate ratio of thick mixture gas, and an NO x content, an unburnt ash content and an air-to-coal mass flow rate ratio of thin mixture gas in the same preferred embodiment; Fig. 19 is a diagram showing a relation between a rotational speed of the classifier and an air-to-coal mass flow rate ratio of thick mixture gas; and Fig. 20 is a diagram showing a relation between a degree of pulverisation of pulverized coal and an unburnt ash content in a coal burnt ash. DESCRIPTION OF THE PREFERRED EMBODIMENT: Fig. 1 is a system diagramm of an apparatus for carrying out one preferred embodiment of the invention. In this figure, reference numeral 1 designates a vertical type coal grinder containing a rotary type classifier therein, numeral 2 designates a pulverized coal pipe, numeral 3 designates a distributor, numeral 4 designates a thick mixture gas feed pipe, numeral 5 designates a thin mixture gas feed pipe, numeral 6 designates a thick mixture gas burner, numeral 7 designates a thin mixture gas burner disposed contiguously to the thick mixture gas burner 6, and numeral 8 designates a boiler furnace. Coal pulverised by the vertical type coal grinder 1 is, after ejected from the same coal grinder 1 as pulverized coal mixture gas and introduced into the pulverized coal pipe 2, separated into thick mixture gas and thin mixture gas by means of the distributor 3. The thick mixture gas passes through the thick mixture gas feed pipe 4 and is ejected from the thick mixture gas burner 6 into the boiler furnace 8 to burn. On the other hand, the thin mixture gas passes through the thin mixture gas feed pipe 5 and is ejected from the thin mixture gas burner 7 into the boiler furnace 8 to burn. The above-mentioned operations are similar to those in the pulverized coal combustion method in the prior art. Fig. 2 is a longitudinal cross-section view showing a mechanism of the above-mentioned vertical type coal grinder 1 containing a rotary type classifier therein, Fig. 3 is a perspective view partly cut away of the rotary type classifier, and Fig. 4 is a transverse cross-section view taken along chain line IV-IV in Fig. 2. At first, with reference to Figs. 2 and 3, material to be ground such as lumped powder coal charged through a feed pipe 10 is applied with load on a rotary table 20 by a grinding roller 30 and pulverized into powder, and it is spattered towards the outer circumference of the rotary table 20. On the other hand, hot air is sent from a hot air inlet portion 40 from the lower part through a blow-up portion 50 into the inside of the grinder. The above-mentioned pulverized coal spattered towards the outer circumference of the rotary table 20 is carried into a rotary type classifier 65 at the upper part by the hot air, that is, by the carrier gas, and it is separated into coarse powder and fine powder. The fine powder is taken out through a pulverized coal pipe 110, while the coarse powder is spattered to the outside and falls so as to be ground again. In the above-mentioned rotary type classifier 65, a plurality of classifying vanes 75 are disposed so as to extend along generating lines of an inverse frustocone having a vertical axis and have their upper and lower ends fixedly secured to an upper support plate 80 and a lower support plate 90, respectively, and they are constructed so as to be rotated by the feed pipe 10 disposed along the above-mentioned axis, that is, by a vertical drive shaft. The angles ϑ formed between the plurality of classifying vanes 75 and the direction of rotation can be changed by an appropriate mechanism not shown. As a result of rotation of the classifying vanes 75, pulverized coal in a carrier gas is classified into coarse powder and fine powder, and the principle of classification is based on the following two effects: (A) Balance of forces acting upon particles entered in a classifying vane assembly As shown in Fig. 4, a particle in the vane assembly is subjected to a fluid resistance force R in the centripetal direction and a centrifugal force F due to rotational motion of the vanes, and the respective forces are represented by the following formulae: R = 3πdµV₁, d: particle diameter [cm] µ: viscosity of gas [poise] V₁: gas velocity in the centripetal direction [cm/s] V₂: circumferential velocity of the vanes [cm/s] ρ₁, ρ₂: density of particle, gas [g/cm²] And when the classifier is being operated under a fixed condition, coarse particles fulfilling the relation of F > R are released to the outside of the classifier, whereas fine particles fulfilling the relation of F < R flow to the inside of the classifier, and thus the particles are classified into fine particles and coarse particles. (B) Reflected direction α of particles after collision against the vanes In Fig. 4 is also shown the state of a particle colliding against a vane, and when the reflected direction α of the particle after collision against the vane is directed to the outside with respect to a tangential line, the particle is liable to be released to the outside of the classifier, but on the contrary when the reflected direction α is directed to the inside, the particle is liable to flow into the classifier. When an air flow enters between the classifying vanes, a swirl flow is generated, but it is known that fine particles would make motion close to a swirl flow, while coarse particles would make motion close to a straight flow as deviated from the swirl flow. Consequently, fine particles are liable to have their reflected direction after collision against the vane directed to the inside, while coarse particles are liable to have their reflected direction to the outside, and so classification into fine particles and coarse particles can be carried out effectively. Fig. 5 is a diagram showing the results of test for a performance of the illustrated coal grinder. As shown in this figure, in the case where coal was ground by this grinder under a condition of 200 mesh pass 85%, coarse particles of 100 mesh or larger in the pulverized coal were only 0.1%. Furthermore, it was confirmed that this coal grinder could be operated at an extremely high degree of pulverization of 200 mesh pass 90% or more. At this time, coarse particles of 100 mesh or larger contained in the pulverized coal was 0%. Fig. 16 is a diagram showing variation of a degree of pulverization in the case where a rotational speed of the classifier is varied. As shown in this figure, by varying the rotational speed of the classifier, a degree of pulverization can be regulated easily over a wide range. Fig. 6 is a diagram showing relations between a (combustion primary air/coal) ratio and an NO x content, a flame propagation velocity and an unburnt ash content in the pulverized coal combustion method according to the illustrated embodiment. As shown in this figure, by burning a mixture gas flow having a (combustion primary air/coal) ratio C₀ after separating it into two, thick and thin, mixture gas flows having a concentration C₁ (producing a thick mixture gas flame having a high coal concentration) and a concentration C₂ (producing a thin mixture gas flame having a low coal concentration), an NO x concentration as a whole of the burner would become a weighted mean N m of respective NO x concentrations N₁ and N₂, and it would become lower than an NO x concentration N₀ when a mixture gas having a single concentration C₀ is burnt. On the other hand, stability of ignition upon pulverized coal combustion becomes good, as the difference between the flame propagation velocity V f of pulverized coal mixture gas and the injection flow velocity V a from a burner portion of pulverized coal mixture gas, that is, V f - V a becomes large. Since the above-mentioned thick mixture gas flame has a large flame propagation velocity V f as compared to the case of a mixture gas having a single concentration C₀, V f - V a becomes large, and so, stability of ignition is excellent. In Fig. 6, with respect to an unburnt ash content, the characteristic of the pulverized coal combustion method according to this preferred embodiment is indicated as compared to the method in the prior art. If degrees of pulverization within mixture gases having concentrations C₁ and C₂, respectively, are quite the same, unburnt ash contents produced from a thick mixture gas flame and a thin mixture gas flame in the case of combustion through the method in the prior art become U₁ and U₂, respectively, and an unburnt ash content as a whole of the burner would become U₀. However, due to the above described distributor characteristics, in the case where combustion was made practically through the method in the prior art, an unburnt ash content produced from a thick mixture gas flame increased to U₁′, and accompanying this increase, an unburnt ash content as a whole of the burner increased to U m . Whereas, according to this preferred embodiment, since coarse particles of 100 mesh or larger contained in the pulverized coal mixture gas having a concentration C₁ in the prior art are reduced and even operation under a condition of 200 mesh pass 85% can be performed, unburnt ash contents produced from a thick mixture gas flame and a thin mixture gas flame can be reduced to L₁ and L₂, respectively, and so, an unburnt ash content produced from a whole burner can be reduced to L₀. Fig. 7 is a diagram showing relations between an NO x content and an unburnt ash content as comparing the case of the combustion method according to this preferred embodiment and the case of the combustion method in the prior art. In this figure, a dash line curve indicates a characteristic of a pulverized coal combustion method in the prior art, while a solid line curve indicates a characteristic in the case of the method according to this preferred embodiment. It is seen from this figure that by employing the pulverized coal combustion method according to this preferred embodiment, an unburnt ash content with respect to a same NO x content value is reduced to one half as compared to the method in the prior art. In Fig. 18 are shown relations between an air-to-coal mass flow rate ratio of thick mixture gas and an unburnt ash content. From this figure, it is seen that in the case where an air-to-coal mass flow rate ratio of thick mixture gas is smaller than 1, an unburnt ash content increases abruptly, and that in the case where the same air-to-coal mass flow rate ratio is 2 or larger, an NO x content increases abruptly. Accordingly, it is preferable to regulate an air-to-coal mass flow rate ratio of thick mixture gas at the range of 1 - 2. At this time, an air-to-coal mass flow rate ratio of thin mixture gas is about 3 - 6. Exemplifying conditions of a rotary type classifier in which an air-to-coal mass flow rate ratio of thick mixture gas can be chosen in the range of 1 - 2, they are as follows. That is, Fig. 19 shows the mode of variation of an air-to-coal mass flow rate ratio of thick mixture when a rotational speed of a classifier is varied. From this figure, it is seen that by varying a rotational speed of a classifier in the range of 30 - 180 rpm and varying the angles ϑ (See Fig. 4) formed between the classifying vanes and the direction of rotation in the range of 30° - 60°, an air-to-coal mass flow rate ratio of thick mixture gas can be regulated in the range of 1 - 2. At this time, an air-to-coal mass flow rate ratio of thin mixture gas becomes about 3 - 6 as shown in Fig. 18. By regulating a rotational speed of a classifier as shown in Fig. 17 on the basis of the relations shown in Figs. 18 and 19, it has become possible to automatically control an NO x content and an unburnt ash content. As described in detail above, by employing the pulverized coal combustion method according to the present invention, an unburnt ash content as well as a concentration of nitrogen oxides in an exhaust gas can be remarkably reduced, and also, ideal pulverized coal combustion having an excellent ignition stability can be realized.

Claims: A pulverized coal combustion method including the steps of separating pulverized coal mixture gas ejected from a vertical type coal grinder containing a rotary type classifier therein into thick mixture gas and thin mixture gas by means of a distributor, and injecting these thick and thin mixture gases respectively through separate burner injection ports into a same furnace to make them burn; characterized in that an air-to-coal mass flow rate ratio of said thick mixture gas is chosen at 1 - 2, while an air-to-coal mass flow rate ratio of said thin mixture gas is chosen at 3 - 6, and the range of a degree of pulverization of the pulverized coal is regulated at 100 mesh residue 1.5% or less. A pulverized coal combustion method as claimed in Claim 1, characterized in that the degree of pulverization of the pulverized coal fed to the distributor is regulated by adjusting a rotational speed of the rotary type classifier. A pulverized coal combustion method as claimed in Claim 1, characterized in that the degree of pulverization of the pulverized coal fed to the distributor is regulated by adjusting the angles formed between classifying vanes rotating about the axis of the rotary type classifier and the direction of rotation.

Inventors: KANEKO SHOZO NAGASAKI SHIPYARD, KINOSHITA MASAAKI NAGASAKI SHI, KANEKO, SHOZO, NAGASAKI SHIPYARD & ENG. WORKS, KINOSHITA, MASAAKI, NAGASAKI SHIPYARD & ENG. WORKS, Kaneko, Shozo, Nagasaki Shipyard &amp; Eng. Works, Kinoshita, Masaaki, Nagasaki Shipyard &amp; Eng. Works
Applicants: MITSUBISHI HEAVY IND LTD, MITSUBISHI JUKOGYO KABUSHIKI KAISHA
Application year: 1990
Main classification: F23K1
IPC codes: F23C99, F23K1, B07B7, B02C23