KR100716682B1 - Coke dry quenching method and system - Google Patents

Abstract

By using a fire extinguishing tower composed of a cooling chamber and a prechamber on the upper side thereof, the coke is charged from above the prechamber, the air is blown into the prechamber, and / or the water or the steam is blown in to cool the sensible heat of the coke. In the coke dry fire extinguishing method of heat-exchanging an inert gas as a medium and heat-recovering the waste heat boiler in the form of steam, air and / or water or steam blown into the prechamber such that the heat input to the waste heat boiler becomes a target value. The amount of recovered steam is kept constant by adjusting the amount of, and the amount of flammable gas and oxygen in the circulating gas is kept to a minimum amount to prevent foreign matters from adhering to the sloped flow portion, thereby preventing heat damage of the boiler tube while reducing heat recovery efficiency. And increase the circulation gas aeration resistance and breakage of boiler tube wear To maximize the recovery of sensible heat.

Glowing coke, prechamber, cooling room, waste heat boiler, boiler tube, sloped flow

Description

Coke dry fire extinguishing method and apparatus {COKE DRY QUENCHING METHOD AND SYSTEM}

The present invention relates to a coke dry fire extinguishing method and a fire extinguishing device.

In cooling the red coke discharged from the coke oven, a coke dry fire extinguishing apparatus (so-called CDQ (Coke Dry Quencher)) is used to recover the sensible heat of the coke and save energy.

The dry fire extinguishing device has a cooling chamber for heat-exchanging sensible heat of the glowing coke with an inert gas as a medium, and a prechamber at the upper portion of the cooling chamber. The glowing coke is charged into the prechamber from above the prechamber. The prechamber is provided for the purpose of absorbing the time fluctuations of the red coke input and obtaining stability of the operation.

The coke is heat-exchanged with an inert gas in the cooling chamber, cooled to around 200 ° C, and then cut out by a predetermined amount. The inert gas heated to 900 ° C. after the heat exchange is discharged from the top of the cooling chamber to the ring duct, heat recovered to the waste heat boiler via the primary dust catcher, and fed back to the cooling chamber by a circulating blower.

Charged coke contains volatile or fine coke. Volatilization is highly combustible and there exists a possibility of abnormal combustion, if it contains in high ratio in circulating gas. Therefore, when the air is blown into the prechamber, the volatile matter and the fine powder coke remaining in the coke lump can be combusted.

Part of the surface layer of the red coke may be burned by the blown air. As a result, the amount of heat of the gas discharged from the cooling chamber can be increased by mixing the high temperature air and the combustion exhaust gas with the inert gas.

In addition, since the temperature of the coke reaching the cooling chamber via the prechamber is also raised, the amount of heat recovered as the inert gas in the cooling chamber is also increased. As a result, the steam recovery amount in the waste heat boiler can be increased.

By blowing air into the prechamber, the amount of heat recovery in the waste heat boiler can be increased in the operation of the dry fire extinguishing equipment in a steady state, and the supply amount of the red coke is lowered or the temperature of the red coke to be charged is lowered. Even when the coke temperature in a cooling chamber falls, it becomes possible to keep constant the heat recovery amount in a waste heat boiler. Japanese Patent Laid-Open No. 61-37893 discloses a method of blowing air into a prechamber.

In a dry fire extinguishing system, a gas containing water added in a prechamber is supplied to produce a gas containing a large amount of carbon monoxide and hydrogen gas by reaction with a red coke, and the gas is combined with a circulating gas in a digestion tower. One method is described in Japanese Patent Laid-Open No. 59-75981.

The carbon monoxide and hydrogen gas recovered as gas components in the circulating gas can be recovered as fuel gas after passing through the boiler, and can be recovered as steam by the boiler after adding air into the gas duct to burn carbon monoxide or hydrogen. have.

Steam generated in a waste heat boiler of a coke dry fire extinguishing facility is generally converted into electrical energy in a steam turbine generator and utilized. In order to operate this steam turbine generator stably at the highest efficiency point, it is important to keep the amount of steam generated in the waste heat boiler constant.

In addition, even when used as general steam, if the amount of generated steam fluctuates to the required amount, the steam is insufficient at the demand source when the amount of generated steam decreases, and the generated steam is dissipated unnecessarily when the amount of generated steam increases, so that the generated steam is effective. It is also necessary to maintain a constant steam generation for use.

Since air blown into the prechamber, water and steam blown into the prechamber, and air blown into the hot gas recovered from the digester, the amount of circulating gas circulated between the firebox and the waste heat boiler is increased. Therefore, it is necessary to disperse a part of circulating gas to the outside in order to keep the quantity of circulating gas constant.

When unburned gas, such as carbon monoxide and hydrogen, is contained in circulating gas, the energy which these unburned gas has cannot be collect | recovered effectively.

Therefore, it is preferable to convert unburned gas contained in circulating gas into heat energy by blowing in air and burning it, and to prevent unburned gas from being contained in circulating gas at least when the circulating gas passes through the waste heat boiler.

On the other hand, when oxygen is contained in circulating gas, it is unpreferable in the point that coke burns in a cooling chamber and it reduces cooling ability. Therefore, when blowing air into the circulating gas recovered from the digestion tower, it is necessary to consider that oxygen does not remain in a circulating gas by blowing excess oxygen.

By blowing air into the prechamber and burning some of the remaining volatiles, fine coke and lump coke, both the blown air and the coke in the prechamber rise in temperature. When the temperature in the prechamber is about 1400 ° C., the melted and vaporized as much as the ash contained in the coke, and the vaporized ash is mixed with the inert gas which is carried with the air to raise the cooling chamber.

The cooling chamber outlet temperature of the inert gas is around 900 ° C., and the vaporized ash agglomerates and adheres to the sloping flue portion in the upper portion of the cooling chamber. This deposit is called a clinker and has the problem of causing a blockage of the gas vent holes to increase the ventilation resistance of the gas and inhibit the circulation of the gas for high temperature coke cooling.

Therefore, even in the case where air is blown into the prechamber, it is necessary to control so that the prechamber internal temperature is always kept below a predetermined temperature.

In order to cope with the above-described problems, the waste heat boiler supply gas temperature is varied, but the upper limit of the use temperature specified by the material and structure of the boiler tube constituting the waste heat boiler is determined. As a cause, it is necessary to supply the waste heat boiler supply gas temperature below that temperature.

In addition, when the waste heat boiler feed gas temperature is lowered, the heat exchange efficiency in the boiler is lowered, leading to a decrease in the amount of steam generated. Therefore, it is necessary to perform control so that the waste heat boiler feed gas temperature is always kept within a certain range.

The high-temperature exhaust gas discharged from the fire extinguishing tower is supplied to the waste heat boiler via the sloped flow portion, but when the amount of the exhaust gas exceeds the upper limit flow rate, flotation and scattering of coke are generated from the sloped flow flow. Since it leads to troubles of abrasion failure of the boiler tube due to rapid increase or scattered coke, control at a constant flow rate or less is necessary.

In addition, in order to maximize energy saving by maximizing the amount of sensible heat recovered from the red coke in the cooling chamber at all times, it is important to increase the amount of inert gas supplied to the cooling chamber as much as possible, and from the above limitations of the upper limit of the amount of exhaust gas discharged from the digestion tower, It is necessary to constant control to the upper limit.

A coke dry fire extinguishing method for recovering sensible heat of red coke as a steam by using a coke dry fire extinguishing device, the first object of the present invention is to provide a fire extinguishing method for maintaining a constant amount of recovered steam at a required amount. The second object of the present invention is to provide a fire extinguishing method for maintaining a flammable gas component and an oxygen component in a circulating gas at a minimum value at all times. The third object of the present invention is to maintain the waste heat boiler feed gas temperature within a certain range at all times to prevent thermal damage of the boiler tube, and to prevent a decrease in the heat recovery efficiency of the boiler. Coke from the sloped flow, keeping the amount of exhaust gas discharged at a constant flow rate at all times At the same time to prevent abrasion damage to the circulation and increases the flow resistance of the gas tube boiler according to the injuries and scattering and to maximize the sensible heat recovered amount from the glowing coke in the cooling chamber to the fifth object.

In addition, the present invention seeks to improve safety by injecting air into the prechamber, and combustible gas and powdered coke combustion, and also to increase the amount of waste heat recovery. It is a sixth object to provide a dry fire extinguishing method and a fire extinguishing device.

(I) The gist of the present invention for achieving the first to fifth objects is as follows.

(1) By using the fire-extinguishing tower 1 which consists of the cooling chamber 2 and the prechamber 3 in the upper part, the red coke 9 is charged from the upper part of the prechamber, and air and / or to the prechamber 3 are carried out. In a coke dry fire extinguishing method, in which water or steam is blown, sensible heat of the red coke is heat-exchanged with an inert gas as a medium in the cooling chamber, and heat is recovered in the form of steam in a waste heat boiler (7). 7) When the amount of air and / or water or steam blown into the prechamber 3 is adjusted so that the amount of heat input to the target value is a target value, water or steam blown into the prechamber (hereinafter referred to as "PC water / steam 26"). Ratio of the adjustment amount of the air to the prechamber (hereinafter referred to as "PC air 24") is determined so as to keep the temperature in the prechamber constant. How to digest.

(2) By using the fire-extinguishing tower 1 which consists of the cooling chamber 2 and the prechamber 3 in the upper part, the red coke 9 is charged from the upper part of the prechamber, and air and / or the prechamber 3 are carried out. In a coke dry fire extinguishing method, in which water or steam is blown, sensible heat of the red coke is heat-exchanged with an inert gas as a medium in the cooling chamber, and heat is recovered in the form of steam in a waste heat boiler (7). 7) When the amount of air and / or water or steam blown into the prechamber 3 is adjusted so that the amount of heat input to the target value is a target value, the waste heat to the hot discharge gas 22 discharged from the digestion tower 1 The PC air 24 and / or the PC water and steam 26 are supplied so that air (hereinafter referred to as "SF air 25") is supplied to the boiler so that the heat input to the waste heat boiler becomes constant. While adjusting the amount of, adjust the amount of the SF air 25 Therefore, the ratio between the adjustment amount of the SF air 25 and the adjustment amount of the PC air 24 and / or the adjustment amount of the PC water and vapor 26 maintains the concentration of the combustible gas component and oxygen in the circulating gas at a constant level. Coke dry fire extinguishing method characterized in that it is determined to.

(3) Further, the SF air 25 is supplied to the high temperature discharge gas 22 discharged from the fire extinguishing tower 1 until the waste heat boiler, so that the amount of heat input to the waste heat boiler is constant. While adjusting the amounts of the PC air 24 and / or the PC water / vapor 26, the amount of the SF air 25 is adjusted to adjust the amount of adjustment of the SF air 25 and the PC air 24. The amount and / or ratio with the adjustment amount of PC water and vapor | steam (26) is set so that the density | concentration of the combustible gas component and oxygen in a circulating gas may be kept constant, The coke dry extinguishing method as described in said (1) characterized by the above-mentioned.

(4) The coke dry fire extinguishing method according to the above (1), (2) or (3), wherein the amount of steam generated by the waste heat boiler is adjusted to a target value instead of the heat input amount into the waste heat boiler.

(5) The coke dry fire extinguishing method according to the above (1), (2) or (3), wherein the temperature of the waste heat boiler inlet gas is adjusted to a target value instead of the heat input to the waste heat boiler.

(6) The above (1), (2), (3) or (5), wherein the heat input amount to the waste heat boiler or the waste heat boiler inlet gas temperature target value is modified so that the steam generation amount of the waste heat boiler becomes a target value. The coke dry fire extinguishing method described in.

(7) Adjustment of the quantity of the said PC air 24, PC water vapor 26, SF air 25 detects the fluctuation | variation of the discharge | emission of the coke 10 from the digestion tower 1, and detects the said The coke dry fire extinguishing method according to any one of the above items (1) to (6), wherein the amount of heat input to the waste heat boiler is adjusted so as to compensate for the change in the coke sensible heat recovery amount due to the change in the amount of coke discharged. .

(8) The adjustment of the amount of the PC air 24, the PC water vapor 26, and the SF air 25 detects a fluctuation in the amount of circulating gas 37, and the coke sensible heat cycle by the detected circulating gas amount fluctuation. The coke dry fire extinguishing method according to any one of the above items (1) to (7), wherein the amount of heat input to the waste heat boiler (7) is adjusted to compensate for the change in quantity.

(9) The air [SF air 25] is supplied to the high temperature discharge gas 22 discharged | emitted from the digestion tower until it reaches the waste heat boiler 7, and the said PC air 24, PC water, The adjustment of the amount of the steam 26 detects a change in the amount of SF air, and compensates for the change in boiler heat input due to the detected change in the SF air amount, and adjusts the amount of heat input to the waste heat boiler to a target value. The coke dry fire extinguishing method according to any one of 1) or (4) to (8).

(10) A part of the gas discharged from the waste heat boiler 7 and supplied to the cooling chamber 2 is branched, and the branched gas (hereinafter referred to as "bypass gas 29") is joined to the waste heat boiler supply gas. The adjustment of the amount of the PC air 24, the PC water vapor 26, and the SF air 25 detects a change in the amount of the blown gas 21 supplied to the cooling chamber, and is supplied to the detected cooling chamber. The coke dry fire extinguishing method according to any one of the above (1) to (9), wherein the coke sensible heat recovery amount fluctuation due to the amount of the blown gas 21 is compensated for, and the heat input to the waste heat boiler is adjusted to be constant. .

(11) When the waste heat boiler feed gas temperature is detected and the detected waste heat boiler feed gas temperature exceeds a predetermined upper and lower limit, the circulating gas flow rate is increased or decreased to restore the boiler inlet temperature to the upper and lower limits. The coke dry fire extinguishing method according to any one of the above (1) to (10).

(12) Using the fire-extinguishing tower 1 which consists of the cooling chamber 2 and the prechamber 3 in the upper part, the red coke 9 is charged from the upper side of the prechamber, and the sensible heat which the red coke has is made into the said cooling chamber. Heat exchanges an inert gas as a medium in the inside, and supplies air (SF air 25) to the high-temperature discharge gas 22 discharged from the digestion tower 1 to the waste heat boiler 7, In the coke dry fire extinguishing method of heat recovery in the form of steam in a waste heat boiler (7), the carbon monoxide concentration or hydrogen concentration in the gas circulating in the waste heat boiler (7) or the circulating gas calorific value by these gas components becomes constant and also the oxygen concentration. Coke dry fire extinguishing method, characterized in that for adjusting the amount of the SF air to be below a certain concentration.

(13) Adjusting the amount of SF air 25 sets a target value to the carbon monoxide concentration in the gas circulating in the waste heat boiler, and sets an upper limit, a lower limit and a target value to the oxygen concentration in the gas so that the carbon monoxide concentration becomes the target value. When the air amount is adjusted and the oxygen concentration exceeds the upper limit, the adjustment of the SF air amount by the carbon monoxide concentration is stopped and the SF air amount is adjusted so that the oxygen concentration becomes the target value, and the oxygen concentration is lower than the target value or the lower limit value or the oxygen concentration is lowered. The coke dry fire extinguishing method according to the above (12), wherein when the carbon oxide concentration exceeds the target value or the lower limit and the carbon oxide concentration exceeds the target value, the adjustment of the SF air amount by the carbon monoxide concentration is resumed.

(14) The adjustment of the amount of the SF air 25 sets a target value to the hydrogen concentration in the gas circulating in the waste heat boiler, and sets an upper limit, a lower limit and a target value to the oxygen concentration in the gas so that the hydrogen concentration becomes the target value. When the air amount is adjusted and the oxygen concentration exceeds the upper limit, the adjustment of the SF air amount by the hydrogen concentration is stopped and the SF air amount is adjusted so that the oxygen concentration becomes the target value, and the oxygen concentration is lower than the target value or the lower limit value or the oxygen concentration is lowered. The coke dry fire extinguishing method according to the above (12), wherein when the hydrogen concentration exceeds the target value or the lower limit and the hydrogen concentration exceeds the target value, the adjustment of the SF air amount by the hydrogen concentration is resumed.

(15) The amount of SF air 25 is adjusted by adding the product of the carbon monoxide concentration in the gas circulating in the waste heat boiler to the calorific value of carbon monoxide and adding the product of the hydrogen concentration in the gas and the calorific value of hydrogen to generate the circulating gas calorific value. A target value is set, an upper limit value, a lower limit value, and a target value are set for the oxygen concentration in the gas, and the SF air amount is adjusted so that the circulating gas calorific value becomes the target value, and when the oxygen concentration exceeds the upper limit value, the SF air amount is determined by the circulating gas calorific value. When the adjustment is stopped and the SF air amount is adjusted so that the oxygen concentration becomes the target value, the oxygen concentration is lower than the target value or the lower limit value, or the oxygen concentration is lower than the target value or the lower limit value, and the circulating gas calorific value is higher than the target value. Resume adjustment of SF air volume by The coke dry fire extinguishing method as described in said (12).

(16) The adjustment of the amount of the SF air 25 detects a change in the discharge of the coke 10 from the fire extinguishing tower 1, and carbon monoxide in the gas circulating the waste heat boiler due to the change in the detected discharge of the coke. The coke dry fire extinguishing method according to any one of the above (12) to (15), wherein the concentration or hydrogen concentration or the circulating gas calorific value and the oxygen concentration are adjusted to prevent variations.

(17) The adjustment of the amount of SF air 25 detects a change in the amount of PC air 24 and / or the amount of PC water and steam 26, and the change in the amount of detected PC air and / or the amount of PC water and steam. Coke dry fire extinguishing method according to any one of (12) to (16), characterized in that the carbon monoxide concentration or hydrogen concentration in the gas circulating in the waste heat boiler is adjusted to prevent variations in the circulating gas calorific value and oxygen concentration. .

(18) Blowing air [PC air 24] into the prechamber 3 and / or blowing water or steam [PC water vapor 26], and the carbon monoxide concentration or hydrogen concentration or the circulating gas calorific value In the adjustment of the amount of SF air 25 by means of adjusting the amount of the SF air 25, the amount of the PC air 24 and / or the PC water / steam 26 is adjusted, and the PC air 24 and / Or the ratio between the amount of decrease in PC water / steam 26 and the amount of increase in SF air 25 is determined so that the amount of heat input to the waste heat boiler 7 becomes constant. The coke dry fire extinguishing method described in.

(19) The coke dry fire extinguishing method according to the above (18), wherein a ratio between the adjustment amount of the PC water and the vapor (26) and the adjustment amount of the PC air (24) is determined to keep the temperature in the prechamber constant.

(20) Using the fire-extinguishing tower 1 which consists of the cooling chamber 2 and the prechamber 3 in the upper part, the red coke 9 is charged from above the prechamber, and air is blown in to the prechamber 3. And / or blow water or steam to heat the sensible heat of the glowing coke in the cooling chamber as an inert gas as a medium, and the sensible heat of the hot gas discharged from the digestion tower 1 to be discharged from the waste heat boiler 7. In the coke dry fire extinguishing method of heat recovery in the form of steam, a part of the gas discharged from the waste heat boiler 7 and supplied to the cooling chamber is branched, and the branched gas (bypass gas 29) is supplied to the waste heat boiler supply gas. And adjusting the amount of the bypass gas (29) so that the amount of the hot exhaust gas (22) discharged from the digestion tower (1) becomes a target value.

(21) Instead of the amount of hot exhaust gas 22 discharged from the digestion tower 1, the bypass gas so that the boiler supply gas pressure measured from the extinguishing tower outlet until reaching the waste heat boiler inlet becomes a target value. The coke dry fire extinguishing method according to the above (20), wherein the amount of cobalt is adjusted.

(22) When the temperature in the prechamber is measured and a difference occurs between the measured temperature in the prechamber and the target value, the value of the ratio of the adjustment amount of the PC water / steam 26 and the adjustment amount of the PC air 24. The coke dry fire extinguishing method according to the above (1) or (19), wherein the temperature in the prechamber is adjusted to be a target value.

(23) a cooling tower (2) and a prechamber (3) at the upper portion of the digestion tower (1) for charging the red coke (9) from above the prechamber, and blowing air into the prechamber (3); And / or the sensible heat of the hot gas discharged from the digestion tower by heat-exchanging the blowing device 14, 16 for blowing water or steam and the sensible heat of the coke in the cooling chamber as an inert gas as a medium. In the coke dry fire extinguishing device having a waste heat boiler (7) heat recovery in the form, SF air blowing device (15) for supplying air (SF air 25) to the hot gas 22 discharged from the fire tower (2) And a bypass pipe 19 for branching a part of the gas discharged from the waste heat boiler to be supplied as an inert gas to the cooling chamber, and joining the branched gas (bypass gas 29) to the waste heat boiler supply gas. Into the fire extinguishing tower (1) Emitter discharged coke dry fire extinguishing system, characterized in that located in the waste-heat boiler (7) in the route to the introduction in the joining position of the bypass pipe (19) SF air intake port than the upstream side (the opposite boiler side).

(1) to (6) and (11) of the present invention relate to feedback control for maintaining a constant amount of waste heat boiler steam recovery.

Further, the above (7) to (10) of the present invention relates to feedforward control for maintaining a constant amount of waste heat boiler steam recovery against disturbance.

The above (12) to (15), (18) and (19) of the present invention relate to feedback control for making the content of the combustible component and oxygen in the circulating gas extremely small.

Moreover, said (16) and (17) of this invention are related with feedforward control for making the content of the combustible component and oxygen in a circulating gas very small against disturbance.

Further, the above (20) and (21) of the present invention relates to feedback control for maintaining a constant amount of hot gas discharged from the cooling chamber.

Further, the above (22) of the present invention relates to feedback control for keeping the temperature in the prechamber constant.

In addition, the above (23) of the present invention relates to a coke dry fire extinguishing device for avoiding damage due to local abnormal temperature rise of the sloped flow langer.

(II) In the present invention which achieves the sixth object, water or steam is blown together with air in the prechamber. The water gas reaction that occurs when the red coke is in contact with steam is an endothermic reaction, and hydrogen gas and carbon monoxide are generated. When water is blown in, the endothermic reaction by the said water gas reaction is added to the endothermic reaction when water evaporates.

Therefore, while the inside of the prechamber is heated by blowing air into the prechamber, an endothermic reaction occurs by blowing water or vapor into the prechamber, and as a result, the prechamber temperature can be kept below a certain temperature.

Specifically, by controlling the temperature in the prechamber to 1150 ° C. or lower, melting and vaporization of ash in the prechamber can be prevented, and adhesion of clinker to the gas circulation system can be prevented. .

The present invention is characterized by having a preferred method and apparatus for blowing water and air in blowing air and water into the prechamber. It is further characterized by having a preferred method and apparatus for measuring the temperature in the prechamber when controlling the temperature in the prechamber below a certain temperature by blowing water or vapor together with air in the prechamber.

That is, the summary of this invention which achieves the said 6th objective is as follows.

(24) A fire extinguishing tower (1) comprising a cooling chamber (2) and a prechamber (3) thereon, charged with red coke (9) from above the prechamber, and air (24) in the prechamber from the prechamber top. In the coke dry fire extinguishing method which blows water and blows water (26) and heat-exchanges the sensible heat which the said coke has in the cooling chamber with an inert gas as a medium in a cooling chamber, and heat-recovers it in vapor form. Coke dry fire extinguishing method characterized in that the water (26) is sprayed in a mist type, and mixed with the air of the mist type water to be blown into the prechamber.

(25) Having two or more blowing holes 45 for injecting air and water into the prechamber in the circumferential direction of the prechamber, and arranging the prechamber circumferential directions θ between adjacent blowing holes within the following ranges. The coke dry fire extinguishing method as described in said (24) characterized by the above-mentioned.

0.5 × (360 / N) ≤ θ (°) ≤ 1.5 × (360 / N)

Is the prechamber circumferential angle between adjacent inlets, and N is the number of inlets.

(26) The above-mentioned (24) or (25), wherein the height direction position of the air intake port 45 for injecting air and water into the prechamber is higher than a predetermined coke stacking upper limit position in the prechamber. Described coke dry fire extinguishing method.

(27) When the upper end of the coke stacked in the prechamber exceeds the predetermined coke loading upper limit position, the blowing of air and water into the prechamber is stopped or the blowing amount is reduced, so that the upper end of the coke is the upper limit. The coke dry fire extinguishing method according to the above (26), wherein the blowing of water and air is resumed or the blowing amount is increased when the position or the predetermined predetermined position is lower.

(28) A fire extinguishing tower (1) comprising a cooling chamber (2) and a prechamber (3) thereon, charged with red coke (9) from above the prechamber, and blows air into the prechamber from the prechamber top. In addition, the coke dry extinguishing method which blows water or steam, heat-exchanges the sensible heat which the said coke has, and heat-exchanges it in the form of steam by using an inert gas as a medium in a cooling chamber, The surface of the coke directly under the prechamber exit. A coke dry fire extinguishing method, characterized in that the temperature is measured by a non-contact optical thermometer (18), and the operation management or control is performed as the temperature in the prechamber with the measured temperature.

(29) The blowing amount of the water or steam or the blowing amount of the prechamber blowing air such that air is blown from the upper portion of the prechamber into the prechamber while blowing water or steam, and the temperature in the prechamber is equal to or less than a predetermined temperature. The coke dry fire extinguishing method as described in said (28) characterized by adjusting one or both of them.

(30) A digestion tower (1) comprising a cooling chamber (2) for exchanging sensible heat of the glowing coke with an inert gas as a medium, and a prechamber (3) above the cooling chamber, and the heat of the inert gas in the form of steam. In the coke dry fire extinguishing device having a waste heat boiler (7) to recover the furnace, and having a blowing device (46) for blowing air and water into the prechamber above the prechamber, the blowing device (46) A coke dry fire extinguishing device, characterized in that the spray to form a mixture into the air and blow into the prechamber.

(31) The blowing device (46) has two water spray nozzles (42) arranged up and down in the air blowing pipe (47), and the water spray nozzle (42) has a wide angle in the horizontal direction and a vertical direction. The coke dry fire extinguishing device according to (30), wherein water is sprayed at a narrow angle.

(32) It has two or more injection holes 45 of the said blowing device 46 in the circumferential direction of a prechamber, and arrange | positions the prechamber circumferential direction angle (theta) between adjacent injection openings in the following ranges, The coke dry fire extinguishing device according to (30) or (31) described above.

0.5 × (360 / N) ≤ 0 (°) ≤ 1.5 × (360 / N)

Is the prechamber circumferential angle between adjacent inlets, and N is the number of inlets.

(33) The above (30), (31) or (32), wherein the height direction position of the intake port 45 of the blowing device 46 is higher than a predetermined coke stacking upper limit position in the prechamber. Coke dry fire extinguishing device described in.

(34) A fire extinguishing tower (1) comprising a cooling chamber (2) for exchanging sensible heat of the glowing coke with an inert gas as a medium, and a prechamber (3) above the cooling chamber, and the heat of the inert gas in the form of steam. In the coke dry fire extinguishing device having a waste heat boiler (7) to recover the furnace, and having a blowing device (46) for blowing air, water or steam into the prechamber above the prechamber, the coke of the coke immediately below the prechamber outlet Coke dry fire extinguishing device, characterized by having a non-contact optical thermometer (18) for measuring the surface temperature.

1 is a schematic diagram of a coke dry fire extinguishing device of the present invention.

Fig. 2 is a block diagram showing the outline of the control of the present invention. Fig. 2A is a block diagram of the invention of claim 1, Fig. 2B is a block diagram of the invention of claim 2, and Fig. 2C is a block diagram of the invention of claim 3. to be.

3 is another block diagram showing the outline of the control of the present invention. FIG. 3A is a block diagram of the invention of claim 6, and FIG. 3B is a block diagram of the invention of claim 7. FIG.

4 is another block diagram showing an outline of the control of the present invention. 4A is a block diagram of the invention of claim 12, FIG. 4B is a block diagram of the invention of claim 16, and FIG. 4C is a block diagram of the invention of claim 19; to be.

5 is a schematic diagram of another coke dry fire extinguishing device of the present invention.

Fig. 6 is a partial sectional view showing the air and water blowing device of the present invention.

7 is a perspective view showing the spraying situation of the water spray nozzle of the present invention.

8 is a view showing the spraying situation of the sprayed water of the present invention. FIG. 8A is a diagram showing the trajectory of sprayed water in the prechamber cross section, and FIG. 8B is a diagram showing the sprayed water spray range on the upper surface of the glowing coke.

Fig. 9 is a diagram showing the spray water spray range on the upper surface of the coke coke in the case of having a plurality of air inlets of the present invention. FIG. 9A is a diagram showing a case where two inlets are provided, and FIG. 9B is a diagram showing a case where three inlets are provided.

(I) Embodiment of this invention which achieves said 1st-5th objective is demonstrated based on FIG.

The fire-extinguishing tower 1 which cools the red coke is formed in the vertical shape, and is provided with the prechamber 3 and the cooling chamber 2 in the up-down direction. The prechamber 3 and the cooling chamber 2 are divided as gas flows by the sloughing flow portions 4 formed around the inner wall thereof.

The inert gas 9 having a temperature of about 980 ° C. is charged from above the prechamber 3, gradually moves downward, and is inert gas blown from the intake pipe 11 below the cooling chamber in the cooling chamber 2. It is cooled by (27). The temperature of the coke 10 at the time of discharge from the lower part of a cooling chamber is set to 200 degreeC vicinity.

The inert gas 27 blown in the cooling chamber performs heat exchange between the glowing coke while raising the inside of the cooling chamber, and the gas temperature rises to the ring duct 5 from the sloped flow portion 4 in the upper portion of the cooling chamber. Discharged. In addition, the inert gas is sent from the ring duct 5 to the waste heat boiler 7 via the primary dust catcher 6, and is heat-recovered by the waste heat boiler 7 to lower the temperature to around 180 ° C. It is blown back into the cooling chamber 2 via 8).

In the present invention, air is blown into the prechamber as needed. In addition, the air blown into a prechamber may be called "PC air 24" below. Oxygen in the blown air reacts with some of the remaining volatiles, fine coke and lump coke. The reaction is an exothermic reaction that mainly produces carbon monoxide, and the blown air, the product gas, and the coke are lowered in the prechamber while the temperature is increased to become the highest temperature in the lower part of the prechamber.

The blown air and the generated gas are mixed with the inert gas that has risen from the lower side in the lower part of the prechamber, and are discharged from the sleeping flow portion 4 to the ring duct 5.

In the present invention, water or steam is blown into the prechamber together with air as necessary. In addition, water or steam blown into a prechamber may be called "PC water / vapor 26" below.

The blown water absorbs heat when it evaporates to become steam, and the steam contacts with the red coke to generate hydrogen gas and carbon monoxide by water gas reaction and endothermic. Therefore, the temperature of the gas and the coke in the prechamber is lowered by blowing water or steam, and the temperature of the gas and the coke in the prechamber can be adjusted by adjusting the blowing amount of water or steam.

Hydrogen gas and carbon monoxide generated by the water gas reaction are lowered in the prechamber, mixed with the inert gas that has risen in the lower part of the prechamber, and discharged from the sleeping flow portion 4 to the ring duct 5.

In the present invention, air 25 is blown into the ring duct 5 or the gas discharge pipe 12 of the sloped flow portion 4 (SF) as necessary. In addition, this blown air may be called "SF air 25" below.

Carbon monoxide generated by the reaction of the PC air 24 and the red coke 9, carbon monoxide and hydrogen generated by the reaction of the PC water vapor 26 and the red coke 9 are discharged from the ring duct 5. It is then burned by contact with the SF air 25 to be changed to carbon dioxide and water and then to generate heat.

Corresponding to the blowing amount of the PC air 24, the blowing air of the combustible gas such as carbon monoxide generated by the PC air 24 is blown into the SF air 25, which is necessary and sufficient, so that the basis of the blowing of the PC air is based on. The steam energy recovery amount can be maximized. In addition, a sufficient amount of SF air required to combust the combustible gas generated by the water gas reaction between the PC water vapor 26 and the coke 9 in response to the amount of the PC water vapor 26 blown ( By simultaneously blowing 25), the amount of steam energy recovery based on PC water and steam injection can be maximized.

When oxygen or the like amount of oxygen necessary for burning the combustible gas contained in the exhaust gas 22 is supplied as the SF air 25, excess oxygen remains in the circulating gas 37 and is included in the blown gas 21 to cool it. It is blown into the chamber 2. Therefore, it is preferable that the quantity of SF air 25 supply only the quantity required to burn the combustible gas contained in exhaust gas 22. As shown in FIG.

In the present invention, a part of the gas discharged from the waste heat boiler 7 and supplied from the inert gas blowing pipe 11 to the cooling chamber is branched to the bypass pipe 19 as necessary, and the branched gas (hereinafter, “ Bypass gas 2 " is combined with the discharge gas 22 in the gas discharge pipe 12 to form the waste heat boiler supply gas 23.

The required amount of the blown gas 21 to the cooling chamber 2 is preferably blown in as much as possible in order to maximize the amount of sensible heat recovered from the red coke in the cooling chamber 2, while the fire tower 1 There is an upper limit on the amount of exhaust gas 22 discharged from the exhaust gas, so that the blown gas 21 into the cooling chamber 2 is maintained to maintain the exhaust gas 22 discharged from the digestion tower 1 near its upper limit. It is desirable to adjust the amount.

On the other hand, in order to prevent the gas temperature of the waste heat boiler supply gas 23 from excessively rising or for other purposes, the flow rate of the waste heat boiler supply gas 23 is more than the required amount of the blown gas 21. There is. In such a case, a part of the circulating gas 37 is bypassed to the bypass pipe 19 and joined with the discharge gas 22 so that the amount of the blown gas 21 is exhausted from the above-described fire extinguishing tower 1. The amount of the waste heat boiler supply gas 23 can be increased while maintaining the gas amount near the upper limit.

(1) to (6) and (11) of the present invention relate to feedback control for maintaining a constant amount of waste heat boiler steam recovery. Further, the above (7) to (10) of the present invention relates to feedforward control for maintaining a constant amount of waste heat boiler steam recovery against disturbance. In said (1)-(11) of this invention, PC air is blown in from the prechamber, or both PC air and PC water and steam are blown in.

Increasing the blowing amount of the PC air 24 increases the reaction with the red coke 9 in the prechamber, and consequently, the amount of vapor recovery is increased. Conversely, reducing the blow-in amount of the PC air 24 reduces the amount of vapor recovery. The relationship between the fluctuation value of the amount of PC air and the fluctuation value of the vapor recovery amount is mainly determined by the calorific value when oxygen and coke in PC air react to generate carbon monoxide, and a combustion component of a volatile component containing red coke is added. .

The relationship between the fluctuation value of the amount of PC air and the fluctuation value of the vapor recovery amount for each coke dry fire extinguishing device can be accurately determined based on actual operation data. Similarly, the relationship between the fluctuation value of the blow amount of the PC water and steam 26 and the fluctuation value of the vapor recovery amount can be accurately determined based on actual operation data. When control to keep the waste heat boiler vapor recovery amount constant by feedback control is carried out, normally, the waste heat boiler heat input amount is selected as a control amount.

The above-mentioned (1) of the present invention is made based on the above findings, and when the PC water / steam 26 is not blown so that the heat input amount into the waste heat boiler is a target value, the amount of PC air 24 is adjusted. By adjusting, when the PC water and the steam 26 are blown in, the amount of waste heat boiler steam is kept constant by adjusting the amount of the PC air 24 or the PC water and steam 26.

FIG. 2A shows a block diagram in the case where only the PC air 24 is adjusted. Specifically, when the heat input to the waste heat boiler shows a different value from the target value, the amount of heat generated is increased or decreased by varying the amount of PC air or varying the amount of PC air and the amount of water and steam of PC depending on the degree of the difference. Match the heat input to the waste heat boiler with the target value. More specifically, good control can be performed by optimizing each variable when performing PID control.

When the temperature in the prechamber 3 becomes too high, only the ash contained in the coke melts and vaporizes, and the ash that has been cooled and vaporized near the exit of the cooling chamber of the inert gas is agglomerated to form a sloped flow portion above the cooling chamber ( 4) is attached. Therefore, it is preferable that the temperature in the prechamber can be kept constant so that the temperature in the prechamber is not excessively increased even when the PC air 24 is increased in order to keep the vapor recovery amount constant in the above (1).

On the other hand, when the amount of PC water / vapor blowing is increased, the temperature in the prechamber can be lowered. The above (2) of the present invention has been made on the basis of this knowledge, and in the control for maintaining a constant steam recovery amount, the increase value of the PC air amount and the increase value of the PC water / vapor amount are performed at a constant ratio.

A block diagram is shown in Fig. 2B. The constant ratio is determined on the basis of an experiment or the like so that the degree of temperature rise in the prechamber due to the increase in the amount of PC air coincides with the degree of temperature drop in the prechamber due to the increase in the amount of PC water and steam. Thereby, feedback control for maintaining the heat input amount to a waste heat boiler can be performed uniformly, maintaining the temperature in a prechamber.

In the case where the PC air 24 or the PC water and vapor 26 are blown into the prechamber, the SF air 25 is blown in order to combust the combustible gas generated by these blowing gases. In order to control the amount of heat input to the waste heat boiler 7, in the above (1) and (2) of the present invention, if the amount of PC air, PC water, or steam is increased or decreased, the exhaust gas 22 discharged from the fire extinguishing tower is accompanied. The flammable gas component in the gas is also increased or decreased.

When the combustible gas increases, the increase is sent to the waste heat boiler in the unburned state in this state, and energy cannot be recovered sufficiently. In addition, when the combustible gas is reduced, the oxygen supplied from the SF air 25 becomes excess, the gas containing oxygen is supplied to the waste heat boiler, and finally is included in the blown gas 21 to be supplied to the cooling chamber.

In the above (3) of the present invention, the ratio of the adjustment amount of PC air and / or the adjustment amount of PC water and steam and the adjustment amount of SF air is to keep the concentration of the combustible gas component and oxygen in the waste heat boiler supply gas constant. Decide to keep.

Fig. 2C shows a block diagram in this case. The increase in the PC air 24 increases the carbon monoxide in the exhaust gas, and the amount of SF air 25 required to burn the increased carbon monoxide into carbon dioxide is almost comparable to the increase in the PC air 24.

Accurately, on the basis of the experimental results, it is possible to determine the ratio of the adjustment amount of the SF air 25 and the adjustment amount of the PC air 24 so as not to increase or decrease the combustible gas component and oxygen in the circulating gas 37. . The ratio between the adjustment amount of the SF air 25 and the adjustment amount of the PC water / vapor 26 can be obtained in the same manner.

In the above (3) of the present invention, the amount of the SF air 25 increases or decreases with the increase or decrease of the PC air 24 and / or the PC water / vapor 26. Since the combustion amount of the gas in the discharge pipe 12 also changes by increasing or decreasing the amount of SF air 25, the heat input amount to a waste heat boiler also increases or decreases.

Therefore, also in feedback control when the heat input amount of a waste heat boiler differs from a target value, the quantity of PC air 24 or PC air 24 or PC water / vapor 26 so that the heat input amount to a waste heat boiler becomes constant. When adjusting the amount of SF air 25 at the same time, the adjustment amount is sufficient to be smaller than the adjustment amount of PC air or the like in (1) and (2) of the present invention.

Regarding the adjustment of the amount of PC water and steam, in the case of increasing the PC water and steam 26 alone in the above (1) of the present invention, the heat input of the waste heat boiler decreases due to the increase, but in the above (3) of the present invention In addition, when adjusting the quantity of SF air 25, when the PC water and the steam 26 are increased, the waste heat boiler heat input amount increases with an increase, and a control parameter is decided in consideration of this point. Therefore, various variables at the time of performing PID control also become a value different from said (1) of this invention.

By simultaneously carrying out the above (1), (2) and (3) of the present invention, the temperature of the preheat chamber is kept constant so that the input of the waste heat boiler is maintained without increasing the combustible gas component and oxygen in the waste heat boiler feed gas. It becomes possible to perform feedback control to keep the amount of heat constant.

As described above, in feedback control for maintaining a constant steam recovery amount in the waste heat boiler 7, the waste heat boiler heat input amount is usually selected as a control amount, and the control is performed so that the heat input amount becomes constant. However, even if control is performed so that the heat input amount of the waste heat boiler becomes constant, the amount of steam generation of the waste heat boiler 7 may not necessarily be constant, but may fluctuate.

As a result of the investigation by the present inventors, the first reason that the amount of steam generation fluctuates is that unburned components and oxygen of the combustible gas remain in the boiler supply gas 23, and the unburned combustion components burn in the boiler, so It was found that steam was generated. The remaining oxygen may be considered to be a case where the air introduced as the SF air 25 does not complete combustion to the boiler inlet and when outside air penetrates into the boiler body.

The above-mentioned (4) of the present invention is made based on the above findings, and by adjusting the steam generation amount of the waste heat boiler to be a target value instead of the heat input amount to the waste heat boiler, it is possible to suppress the fluctuation of the steam generation amount and maintain a constant generation amount. It becomes possible. The performance value of the amount of steam generated can be measured by installing a flow meter such as an orifice in the main steam generated. It is also possible to estimate from the pure water supply to the waste heat boiler.

In said (5) of this invention, it adjusts so that waste heat boiler inlet gas temperature may become a target value instead of the heat input amount to a waste heat boiler. In fact, if the value of the boiler heat input value is to be obtained, the temperature, quantity and specific heat of the boiler inlet gas are required, and the measurement accuracy becomes complicated.

From this point of view, when the boiler inlet gas temperature control is performed as in the above (5) of the present invention, the control can be performed by measuring only the temperature. In addition, since the quantity and specific heat of the boiler inlet gas do not fluctuate greatly in a short time, by controlling the temperature constantly, the amount of heat input is constantly controlled in the short term.

Even if the feedback control is to be performed on the basis of the steam generation amount as described in the above (4) of the present invention, when the heat capacity of the boiler is large, a large time delay may be generated between the boiler heat input amount and the steam generation amount. It is accompanied by difficulty. On the other hand, the degree of deviation between the boiler heat input and the steam generation amount fluctuates in a very long cycle.

Therefore, the short-period feedback control for maintaining a constant steam generation amount is carried out using the waste heat boiler heat input amount as a control amount, and finds the relationship between the steam generation amount and the boiler heat input amount in a long cycle, and calculates the heat input amount at which the steam generation amount is a target value from the relationship. It is preferable to modify the waste heat boiler heat input quantity target value or waste heat boiler inlet gas temperature target value in short-term feedback control.

The above (6) of the present invention is made on the basis of this idea, and is characterized in that the heat input quantity target value or waste heat boiler inlet gas temperature target value is modified so that the steam generation amount of the waste heat boiler becomes a target value. Fig. 3A shows a block diagram in this case.

In the above (7) of the present invention, the feed forward control for detecting the fluctuation of the discharge of the coke 10 from the digestion tower 1, grasping the fluctuation of the detected coke discharge as disturbance, and maintaining a constant steam generation amount To do. As the coke discharge from the digestion tower 1 increases, the coke sensible heat recovery also increases with it. The increase value of the coke sensible heat recovery amount with the increase of coke discharge | emission can be calculated normally from a heat calculation, and can be correctly determined based on an experiment.

On the other hand, in order to offset the increase value of the coke sensible heat recovery amount, one kind or two or more kinds of the amounts of the PC air 24, the PC water / vapor 26, and the SF air 25 can be adjusted. The adjustment amount can be accurately determined based on heat calculations and experiments to keep the amount of heat supplied to the boiler constant.

Fig. 3B shows a block diagram when PC air is selected as the operation amount. This figure also shows a diagram of the feedback control.

The above (8) of the present invention focuses on the fluctuations in the amount of circulating gas as disturbance, and performs feedforward control for maintaining a constant amount of steam generation as in the above (7) of the present invention. In the case where the circulating gas is supplied to the cooling chamber without branching as it is, the value obtained by subtracting the amount of dissipating gas from the circulating gas amount is the amount of blown gas supplied to the cooling chamber as it is. When the amount of blown gas supplied to the cooling chamber is changed, the heat exchange efficiency in the cooling chamber is changed, and the amount of sensible heat from which the cooling gas is recovered from the red coke is changed.

The change in the sensible heat recovery amount is predicted in advance based on the heat calculation and the experiment, and the feed forward control is performed so that the amount of heat input to the waste heat boiler is made constant by supplementing the variance in the sensible heat recovery amount. One type or two or more types of water, steam 26, and SF air 25 are adjusted. Instead of detecting the amount of circulating gas, the amount of blown gas supplied to the cooling chamber may be directly detected and used.

In addition, (9) of the present invention focuses on the fluctuation of the SF air amount as disturbance, and performs feedforward control for maintaining the boiler heat input constant by adjusting PC air, PC water and steam.

In the above (10) of the present invention, in the case where the bypass tube (19) is arranged to flow the bypass gas (29), attention is paid to the fluctuations in the blown gas flow rate supplied to the cooling chamber as disturbance. As in (7), feed forward control is performed to keep the amount of steam generated constant.

When a part of the circulating gas is bypassed and supplied to the waste heat boiler, the amount of blown gas supplied to the cooling chamber is an amount obtained by subtracting the bypass gas amount and the dissipation gas amount from the circulating gas amount. When the amount of blown gas supplied to the cooling chamber is changed, the heat exchange efficiency in the cooling chamber is changed, and the amount of sensible heat recovered by the cooling gas from the red coke is changed. The change in the sensible heat recovery amount is predicted in advance based on the heat calculation and the experiment, and the feed forward control is performed so that the amount of heat input to the waste heat boiler is made constant by supplementing the variance in the sensible heat recovery amount. One type or two or more types of water, steam 26, and SF air 25 are adjusted.

Instead of directly detecting the amount of blown gas supplied to the cooling chamber, the amount of circulating gas and bypass gas may be detected and the amount of blown gas supplied to the cooling chamber may be calculated and used as the difference.

In the above (1) to (10) of the present invention, the feedback control and the feedforward control are performed while responding to the occurrence of various disturbances so as to maintain a constant amount of steam recovery in the waste heat boiler. In this process, there may be a case where the temperature of the waste heat boiler feed gas fluctuates.

On the other hand, even if the waste heat boiler heat input amount is kept constant, if the waste heat boiler supply gas temperature is outside the upper limit of the predetermined target range, there is a problem that causes the thermal damage of the waste heat boiler tube. In addition, if the lower limit of the target range, the problem of lowering the heat recovery efficiency in the waste heat boiler occurs.

Here, in a situation where the amount of generated steam of the waste heat boiler is kept constant, that is, the waste heat boiler heat input amount is kept constant, increasing the amount of circulating gas inevitably lowers the waste heat boiler supply gas temperature.

Therefore, as described in the above (11) of the present invention, the temperature of the waste heat boiler supply gas 23 is detected, and the amount of the circulating gas 37 is adjusted so that the detected waste heat boiler supply gas temperature becomes a target range temperature. It is preferable. In order to increase the amount of circulating gas, the required amount of the circulating gas valve 38 is opened, and in order to reduce the amount of circulating gas, the required amount of the circulating gas valve 38 is closed.

The above (12) to (15), (18) and (19) of the present invention relate to feedback control for making the content of the combustible component and oxygen in the circulating gas extremely small. Moreover, said (16) and (17) of this invention are related with feedforward control for making the content of the combustible component and oxygen in a circulating gas very small against disturbance.

In the method of recovering all the sensible heat from the glowing coke in the waste heat boiler and dissipating the atmosphere when excess circulating gas is generated, it is preferable to make the combustible component in the circulating gas very small as described above.

On the other hand, when applying the combustible component control in the circulating gas of the present invention when the gas is recovered instead of dissipating a part of the circulating gas into the atmosphere, the target value of the carbon monoxide concentration, the hydrogen concentration or the circulating gas calorific value in the circulating gas is applied. By setting as the gas property to be recovered, a recovery gas having a stable calorific value can be obtained.

In the above (12) of the present invention, the air [SF air 25] is supplied to the high temperature discharge gas 22 discharged from the digestion tower until it reaches the waste heat boiler 7 to adjust this SF air amount. As a result, the carbon monoxide concentration or the hydrogen concentration in the gas 37 circulating in the waste heat boiler 7 or the circulating gas calorific value by these gas components is adjusted or the oxygen concentration is adjusted to be equal to or lower than the predetermined concentration.

Fig. 4A shows a block diagram in this case. The blowing of the PC air 24 and the PC water and vapor 26 is not essential here, but the SF air 25 is usually used as one of the purposes of burning the carbon monoxide generated by the blowing of the PC air 24. Since it is supplied, at least blowing of the PC air 24 is often performed simultaneously.

It is preferable to measure the gas component in the gas 37 which circulates the waste heat boiler 7 by sampling the gas after exiting the waste heat boiler 7. This is because the reaction between the unburned gas and the oxygen gas may continue after the inlet of the waste heat boiler. When an unburned combustible gas component is detected in the circulating gas 37, the SF air 25 which is necessary and sufficient to burn the combustible gas component is increased. When oxygen gas is detected in the circulating gas 37, the SF air 25 corresponding to the oxygen gas amount is reduced.

In the case where the combustible component and the oxygen coexist in the circulating gas, it is necessary to determine whether the control is performed using either the combustible gas component or the oxygen. In addition, if the process mainly produces carbon monoxide as the combustible gas component, the control can be carried out by focusing only on the carbon monoxide.

As in the above (13) of the present invention, the target value can be set to the carbon monoxide concentration in the gas circulating in the waste heat boiler, and the adjustment can be performed by setting the upper limit value and the target value to the oxygen concentration in the gas.

Normally, the SF air amount is adjusted so that the carbon monoxide concentration becomes the target value, and when the oxygen concentration exceeds the upper limit, the adjustment of the SF air amount by the carbon monoxide concentration is stopped to adjust the SF air amount so that the oxygen concentration becomes the target value, and the oxygen When the concentration is lower than the target or lower limit, or the oxygen concentration is lower than the target or lower limit and the carbon monoxide concentration is higher than the target value, the adjustment of the SF air amount by the carbon monoxide concentration is resumed.

By making such adjustments, it is possible to stably control the concentrations of carbon monoxide and oxygen in the circulating gas at a low level which is always below a constant value.

If it is a process in which hydrogen becomes a main component as a combustible gas component, it is preferable to focus only on hydrogen and to control it as said (14) of this invention.

In a process in which carbon monoxide and hydrogen coexist as a combustible gas component, the gas is multiplied by the product of the carbon monoxide concentration in the gas and the calorific value of carbon monoxide as described in (15) of the present invention, focusing on the calorific value when each combustible gas is burned. The product of the concentration of hydrogen and the calorific value of hydrogen is added to make the circulating gas calorific value and the target value is set to the calorific value.

On the other hand, an upper limit and a target value are set for the oxygen concentration in the gas. In general, the SF air amount is adjusted so that the circulating gas calorific value becomes the target value, and when the oxygen concentration exceeds the upper limit, the adjustment of the SF air amount by the circulating gas calorific value is stopped to adjust the SF air amount so that the oxygen concentration becomes the target value. When the oxygen concentration is lower than the target or lower limit, or the oxygen concentration is lower than the target or lower limit and the circulating gas calorific value exceeds the target value, the adjustment of the amount of SF air by the circulating gas calorific value is resumed.

By making such adjustments, the concentrations of carbon monoxide, hydrogen, circulating gas calorific value and oxygen in the circulating gas can always be controlled to a level below a constant value without problem. The target value of the carbon monoxide concentration or the hydrogen concentration or the circulating gas calorific value is preferably a value exceeding zero, and it is preferable to obtain and set the minimum point at which the oxygen concentration does not exceed the upper limit.

The above (16) of the present invention detects the fluctuations in the coke 10 emissions from the digestion tower, grasps the fluctuations in the detected coke emissions as disturbance, and checks the carbon monoxide concentration or hydrogen concentration and oxygen concentration in the gas circulating in the waste heat boiler. This is to perform feedforward control to prevent the variation of.

As the coke emissions from the digestion tower increase, the amount of combustible gas components in the circulating gas also increases. The increase in the combustible gas component accompanying the increase in coke emissions can be determined by calculations and experiments.

The increase in SF air for offsetting the increase in the amount of the combustible gas components is determined by the same calculations and experiments, and the feedforward control is carried out so that the amount of the combustible gas components and oxygen in the circulating gas does not change even if the coke emissions fluctuate. Control can be performed.

4B shows a block diagram in this case. This figure also describes the diagram of feedback control.

In the above (17) of the present invention, the variation in the amount of PC air 24 is recognized as disturbance, and feedforward control is performed as in the above (16) of the present invention to prevent the increase of the combustible gas component and oxygen in the circulating gas. By carrying out the invention (17) of the present invention at the same time as the invention (1) and (9) of the present invention, the concentration of the combustible gas component and the oxygen of the circulating gas is the same as that of the invention (3) of the present invention. The feedback control for making the steam recovery amount constant can be performed while keeping it constant.

In order to prevent an increase in the amount of combustible gas components and oxygen in the circulating gas, the amount of the SF air 25 is increased or decreased in the invention of (12) to (15) of the present invention. The amount of combustion in the gas fluctuates, causing variation in the amount of steam recovered in the waste heat boiler 7.

In the above (18) of the present invention, when adjusting the amount of the SF air 25 so that the carbon monoxide concentration, the hydrogen concentration, the circulating gas calorific value, and the oxygen concentration in the circulating gas are below a certain concentration, the amount of the SF air 25 is The amount of PC air 24 and / or PC water and steam 26 at the same time. The ratio of the increase amount of SF air 25 and the decrease amount of PC air 24 and / or PC water and steam 26 is set so that the heat input amount to waste heat boiler 7 becomes constant.

If the carbon monoxide concentration in the circulating gas is a high value exceeding the control value, the increase of SF air is a reaction to burn carbon monoxide or hydrogen, which acts to lower the carbon monoxide and hydrogen in the circulating gas, and the decrease of PC air, PC water and steam Since the amount of carbon monoxide generated in the prechamber is decreased, the carbon monoxide in the circulating gas is reduced.

On the other hand, an increase in SF air results in an increase in the amount of steam generated, while a decrease in PC air, PC water and steam results in a decrease in the amount of steam generated.

Therefore, it is possible to set the ratio between the increase amount of SF air and the decrease amount of PC air at a rate at which the vapor recovery amount does not fluctuate, thereby reducing the carbon monoxide concentration or hydrogen concentration in the circulating gas without changing the vapor recovery amount. It is possible.

Reducing the PC water and steam while increasing the SF air, the reduction of the PC water and steam also results in the reduction of hydrogen in the circulating gas, so that the concentration of hydrogen in the circulating gas can be further reduced without changing the vapor recovery amount.

When the oxygen concentration in the circulating gas is a high value exceeding the management value, the SF concentration is reduced to reduce the oxygen concentration in the circulating gas. In this case, since the combustion amount of combustible gas in a gas discharge pipe does not change, it does not affect the steam recovery amount. Therefore, in the control for lowering the oxygen concentration in the circulating gas, only the reduction of the SF air 25 is sufficient, and the PC air 24 does not need to simultaneously increase the PC water and the vapor 26 together.

In the above (19) of the present invention, when controlling the amount of the combustible gas component and oxygen in the circulating gas within a constant value, as in the above (18) of the present invention, the waste heat boiler steam recovery amount is constantly held, The temperature in the prechamber is also constantly held.

When adjusting the amount of the SF air so that the carbon monoxide concentration, the hydrogen concentration, the circulating gas calorific value, and the oxygen concentration in the circulating gas are below a certain concentration, the amount of SF air is adjusted and the amount of PC air and PC water and steam is adjusted. .

The ratio of the increase in SF air and the decrease in PC air and PC water and steam is determined so that the heat input to the waste heat boiler is constant. Further, in the above (18) of the present invention, the ratio between the adjustment amount of the PC air and the adjustment amount of the PC water and steam is determined so as to keep the temperature in the prechamber constant.

In the prechamber, an increase in the PC air results in an increase in the calorific value, and an increase in the PC water and steam results in a decrease in the calorific value. Therefore, by properly determining the ratio of the PC air increase value and the PC water and vapor increase value, the temperature in the prechamber can be constantly maintained. Fig. 4C shows a block diagram in this case.

The hot discharge gas discharged from the fire extinguishing tower is supplied to the waste heat boiler 7 via the sloped flow portion 4, but when the amount of the discharged gas exceeds the upper limit flow rate, the coke floats from the sloped flow portion 4 And the scattering phenomenon occurs, leading to a sudden increase in the circulation gas aeration resistance or trouble of abrasion failure of the boiler tube due to the scattering coke, so that control at a constant flow rate or less is necessary.

In addition, in order to maximize the amount of sensible heat recovered from the glowing coke in the cooling chamber 2 and to save energy, it is important to increase the amount of inert gas supplied to the cooling chamber 2 as much as possible. It is necessary to carry out constant control to the said upper limit from the upper limit constraint of the amount of discharge gas.

In the above (20) of the present invention, the bypass pipe 19 is installed in the path of the circulating gas, and the amount of the bypass gas 29 is adjusted so that the amount of the exhaust gas 22 becomes the target value. When the amount of the bypass gas 29 is increased, the amount of the blown gas 21 from the inert blown pipe 11 can be reduced while keeping the amount of the circulating gas 37 constant, resulting in discharge The amount of gas 22 can be reduced.

In the above (21) of the present invention, instead of the amount of the exhaust gas in the above (20) of the present invention, the boiler supply gas pressure measured during the time from the cooling chamber outlet to the waste heat boiler inlet is a target value. Adjust the amount of the bypass gas.

In the above (20) of the present invention, in order to determine the amount of hot gas discharged from the digestion tower, the amount of gas coming from the cooling chamber is obtained from the amount of circulating gas, the amount of dissipating gas, and the amount of bypass gas, and the amount of gas coming from one prechamber is determined by the amount of PC air, The boiler supply needs to be calculated based on the amount of PC water and steam, and the amount of gas increased by the reaction, and it is complicated and difficult to measure or estimate them. It is substituted by gas pressure.

The above (2) and (19) of the present invention determine the value of the ratio of the adjustment amount of the PC air and the adjustment amount of the PC water and steam in advance so that the temperature in the prechamber is kept constant.

By the way, since various operating conditions in a dry fire extinguishing device change, even if control is performed using the value of the said predetermined ratio, the performance temperature in a prechamber may differ from a target value.

In the above (22) of the present invention, when the temperature in the prechamber is measured and there is a difference between the temperature measured value and the target value in the prechamber, the value of the ratio of the adjustment amount of the PC air and the adjustment amount of the PC water and steam is determined. The temperature is adjusted to adjust the temperature in the prechamber to a target value.

Thereby, even if there exists a fluctuation | variation in the operation factor of an apparatus, for example, the temperature in a prechamber can always be matched with target value.

When the SF air 25 is introduced into the gas discharge pipe 12 to combust the combustible gas component, the temperature of the exhaust gas 22 increases by the heat of combustion. In particular, in the case where the bypass gas flows by providing the bypass pipe 19, the temperature of the original exhaust gas 22 is high before the gas discharge pipe 12 and the bypass pipe 19 join.

Therefore, when SF air is introduced into the ring duct 5 and the slitting flow portion 4 before joining the bypass pipe 19 to combust the combustible gas component, the temperature rise of the exhaust gas 22 is also large. As a result, damage due to a local abnormal temperature rise of the bricks of the sloped flow portion may occur.

In the above (23) of the present invention, the SF gas 25 is introduced after the exhaust gas 22 joins the low temperature bypass gas 29 and the gas temperature is lowered. Even if the combustible gas burns, the temperature of the exhaust gas does not increase so much that it is possible to prevent damage due to abnormal local temperature rise of the brick.

Although the invention of said (1)-(23) of this invention can be acquired by implementing each independently, since the effect of each invention can be acquired in total by carrying out combining several invention, it is more preferable.

[First Embodiment]

The present invention was applied to the coke dry fire extinguishing device shown in FIG. The cooling chamber 2 of the dry fire extinguishing device has a volume of 600 m 3 and the prechamber 3 has a volume of 300 m 3. The red coke 9 with an average temperature of 980 ° C. was cooled to an average discharge of 170 tons / H.

PC air is blown in from the upper part of the prechamber into the space 31 formed of the coke upper surface 30 and the prechamber. The PC water and vapor 26 for adjusting the temperature in the prechamber are mixed with the PC air 24 in the piping of the air blowing device 14, and the mixed gas is blown into the prechamber.

SF air 25 is blown into the gas discharge pipe 12 to burn the combustible components in the exhaust gas 22 from the digestion tower 1 to raise the temperature of the exhaust gas and to control the components in the circulating gas 37. Was installed.

In addition, a bypass pipe 19 for branching a part of the inert gas supplied from the circulation blower 8 to the cooling chamber 2 and joining the discharged gas was provided. In addition, the concentration meter of oxygen, carbon monoxide, and hydrogen of a circulating gas component is measured from the sample pipe 37 arrange | positioned at the boiler outlet.

Here, the combination of (1) to (3), (6) to (8), (10) to (13), (16), (18) to (20), (22) and (23) of the present invention The control system and the apparatus were configured to set the target value of the steam generation amount 35 of the waste heat boiler 7 to 130 ton / H, the target carbon monoxide concentration target value of 0.3% and the upper limit value of the oxygen concentration of 0.3 in the circulating gas 37. %, The said lower limit value and the said target value are made into 0.1%, the prechamber internal temperature target value is 1000 degreeC, the upper limit of the temperature of the waste heat boiler supply gas 23 is set to 980 degreeC, and the said lower limit is set to 950 degreeC, and the digestion tower (1 Continuous control over a long period of time with a target value of the amount of the exhaust gas 22 discharged from the above) was 264000 Nm 3 / H.

As a result, in average operating conditions of circulating gas amount 298000 Nm3 / H, PC air amount 10000 Nm3 / H, SF air amount 30000 Nm3 / H, bypass gas amount 10000 Nm3 / H, and PC quantity 1.5 ton / H, The generation amount 35 can obtain a performance of 130 tons / H. In addition, the fluctuation | variation of the steam generation amount 35 was able to control the 1-hour average value in the range of ± 1.5 ton / H.

In addition, even when the set value of the discharge amount was changed from 170 ton / H to 120 ton / H, the steam generation amount 35 could be controlled within the range of 130 ton / H ± 1.5 ton / H.

In addition, the carbon monoxide concentration in the circulating gas 37 was 0.3% on average, and the oxygen concentration could be 0.1% or less. This result is shown in Table 1 in the comparison with a prior art. In addition, it is possible to obtain a temperature result of 1000 ° C in the prechamber, a temperature result of 965 ° C of the waste heat boiler supply gas 23, and a 264000 Nm3 / H amount of exhaust gas 22, resulting in adhesion of foreign matter to the sloped flow portion. No heat damage of the waste heat boiler tube, no deterioration of the heat recovery efficiency of the waste heat boiler, no increase in circulating gas ventilation resistance due to coke rise and scattering from the sloughing flow, and no wear damage of the waste heat boiler tube. It could be avoided and stable operation could be achieved because no local abnormal temperature rise occurred in the sloped flow-floor brick.

In addition, the temperature performance of the discharge coke 10 was 180 ° C., thereby maximizing the amount of sensible heat recovery from the red coke in the above stable operating conditions.

TABLE 1

Table 1 Comparison of Control Effects

 Item  Prior art  Invention  (1) Steam generation amount ① Average value ② Fluctuation value   103.0 tons / H ± 5.0 tons / H   103.0 tons / H ± 1.5 tons / H  (2) Circulating gas component ① Carbon monoxide concentration ② Oxygen concentration   2.0% ≤ 0.1%   0.3% ≤ 0.1%

(II) An embodiment of the present invention which achieves the sixth object will be described with reference to Figs.

As shown in Fig. 5, the fire extinguishing tower 1 for cooling the red coke is formed vertically, and includes a prechamber 3 and a cooling chamber 2 in the vertical direction. The prechamber 3 and the cooling chamber 2 are divided as gas flow flows by the sloughing flow portion 4 formed around the inner wall thereof.

The inert gas 9 having a temperature of about 980 ° C. is charged from the upper side of the prechamber 3 and gradually moves downward, and the inert gas blown from the intake pipe 11 below the cooling chamber in the cooling chamber 2. It is cooled by (27). The temperature of the coke 10 when discharged from the lower part of the cooling chamber is around 210 ° C.

The inert gas 27 blown in the cooling chamber rises in the cooling chamber, and heat exchange is performed between the glowing coke, and the gas temperature rises and is discharged to the ring duct 5 from the sloped flow portion 4 at the upper portion of the cooling chamber. do. In addition, the inert gas is transferred from the ring duct 5 to the waste heat boiler 7 via the primary dust catcher 6, and is recovered by the waste heat boiler 7 to reduce the temperature to around 180 ° C., followed by a circulating blower 8. ) Is blown back into the cooling chamber (2).

In the present invention, air 24 is blown into the prechamber from the air blowing device 14 in the upper portion of the prechamber. Oxygen in the blown air reacts with some of the remaining volatiles, fine coke and lump coke. The reaction is mainly an exothermic reaction that produces carbon monoxide, and the blown air, the product gas, and the coke descend into the prechamber while the temperature rises to become the highest temperature in the lower part of the prechamber.

The blown air and the generated gas are mixed with the inert gas that has risen from below in the lower part of the prechamber and are discharged from the slipping flow portion 4 to the ring duct 5. In the ring duct 5 or the gas discharge pipe 12, the air 25 may be blown from the air blowing pipe 15. As a result, carbon monoxide generated in the prechamber is burned to form carbon dioxide.

In the present invention, water 26 is further blown into the prechamber from the upper part of the prechamber by the water blowing device 16. Steam may be blown in from the water blowing device 16 together with water. The blown water absorbs heat when it evaporates to become steam, and the steam is in contact with the red coke to generate hydrogen gas and carbon monoxide by water gas reaction and endothermic.

Therefore, the temperature of the gas and the coke in the prechamber is lowered by blowing water or steam, and the temperature of the gas and the coke in the prechamber can be adjusted by adjusting the blowing amount of water or steam.

Hydrogen gas and carbon monoxide generated by the water gas reaction are lowered in the prechamber, mixed with the inert gas that has risen in the lower part of the prechamber, and discharged from the sleeping flow portion 4 to the ring duct 5. When air 25 is blown into the ring duct 5 or the gas discharge pipe 12, the air 25 burns hydrogen gas and carbon monoxide to water and carbon dioxide. At the same time, the amount of heat of the waste heat boiler supply gas 23 increases due to the combustion heat of the combustion.

As a result of blowing water or steam into the prechamber, as described above, the amount of heat supplied by the waste heat boiler supply gas 23 at the boiler inlet side increases. Therefore, in the case of the present invention which blows in water or steam, it is also possible to reduce the amount of air blown into the prechamber while ensuring the amount of heat required for the waste heat boiler.

That is, by controlling one or both of the air blowing amount into the prechamber and the water or steam blowing amount into the prechamber, the maximum temperature inside the prechamber and the gas amount and gas temperature of the waste heat boiler feed gas 23 are simultaneously optimized. It is possible to adjust on condition of.

If the amount of heat obtained by the inert gas is high by cooling the red coke, and the amount of heat supplied to the waste heat boiler can be secured sufficiently, the amount of blown in of the prechamber blown air 24 is adjusted without supplying water or steam from the prechamber. The temperature in the prechamber can be lowered only by lowering it.

Although ash was considered to melt at 1400 degreeC or more conventionally in coke powder, it turned out that many tests have softened and melted at about 1200 degreeC. In particular, in the case of a multicomponent system, the softening temperature tends to be lowered, and it has been found that a temperature of 1150 ° C. may be a major criterion in operation considering the temperature unevenness in the cross section of the prechamber having a radius of about 10 m. In addition, management at low temperatures in consideration of safety is effective in terms of long-term stable operation.

The above (24) and (30) of the present invention, when blowing the air (24) in the prechamber and at the same time blows water (26), sprays the water (26) blown into the prechamber into a mist form, the mist It is a coke dry fire extinguishing method and apparatus characterized in that the water of the mold is mixed with the air 24 to be blown into the prechamber. While blowing air and water into the prechamber, steam may also be blown.

The water 24 blown into the prechamber needs to be uniformly sprayed on the surface of the upper portion of the red coke layer 30 filled in the prechamber. If unevenly sprayed, the red coke in the place where water is sprayed in large quantities is excessively cooled, while the temperature of the red coke in the place where water is not sprayed is not sufficiently lowered, which is inappropriate. However, when water is sprayed on the red coke close to the brick of the prechamber side wall for the purpose of uniformly spraying the water, the water is scattered by the bricks and damages the bricks.

As in the present invention, the water blown into the prechamber is made into a fog type to prevent the water sprayed on the red coke from scattering into the bricks, and the fog type water is mixed with the air blown into the prechamber. By blowing in, the mist-like water can be spread evenly and uniformly, and the spray can be uniformly sprayed on the surface of the coke in the prechamber.

However, even mist-type water does not mean mist that does not contain any droplets. If water is mist-type enough to be obtained from a flat spray nozzle that is commonly used, small droplets may be included therein. .

In the present invention (31), as shown in Fig. 6, the blowing device 46, which sprays water into a mist, mixes it with air and blows it into the prechamber, is placed up and down in the air blowing pipe 47. Water spray nozzles 42a and 42b, wherein the water spray nozzles spray water at a wide angle in the horizontal direction and at a narrow angle in the vertical direction as shown in FIG. In Fig. 7, reference numeral 43 denotes the trajectory of the spray water, and 44 denotes the spray water spray range.

Of the two water spray nozzles arranged up and down, the nozzles 42a disposed upward adjust the spraying speed and the spraying angle so that the water reaches a far distance, and is mainly applied to the surface of the red coke far from the blowing device in the prechamber. Spray water. The nozzle 42b disposed downward adjusts the spraying speed and the spraying angle so that the reach of the water is near, and sprays water mainly on the surface of the red coke near the blowing device in the prechamber.

Thus, by arranging two upper and lower intake openings, as shown in Fig. 8A, water can be uniformly sprayed from the side close to the blowing device in the prechamber.

In the gas flow in the coke layer of the prechamber, more gas flows near the prechamber wall compared to the prechamber center. This is because the passage path to the sloped flow is shorter near the prechamber wall and the ventilation resistance in the coke layer is small.

Therefore, even in the space 31 in the upper part of the prechamber, there is a large amount of gas flowing toward the prechamber wall, whereby the sprayed water is further diffused in the circumferential direction to the entire surface of the upper coke layer 30. Spray water will spread widely.

Moreover, the blowing device of this invention can be arrange | positioned 2 or more in the circumferential direction different position in a prechamber. In this case, the range which should be covered by one blowing device should cover not only the distance for the diameter of the prechamber but from the vicinity of the blowing device to the center of the prechamber.

Since the water spray nozzle sprays water at a wide angle in the horizontal direction, water can be sprayed onto the surface of the red coke in the entire width of the prechamber extending to the left and right of the intake opening as shown in Fig. 8B. . On the other hand, the water spray nozzle sprays water in a substantially horizontal direction.

In this case, even if the spray angle in the vertical direction of the water spray nozzle is narrow, the water can be sprayed by sufficiently covering the half width of the prechamber which is the charge range of the nozzle.

Since the water spray nozzle 42 is disposed in the air intake pipe 47, the mist-like water is transported by a high-speed air flow, and the mist-like water can reach the far side from the blowing device 46 in the prechamber. .

In the above (25) and (32) of the present invention, the blowing holes 45 of the blowing device 46 for blowing air and water into the prechamber 3 have two or more places in the circumferential direction of the prechamber, The prechamber circumferential angle θ between the inlets is arranged within the following range.

0.5 × (360 / N) ≤ θ (°) ≤ 1.5 × (360 / N)

Is the prechamber circumferential angle between adjacent inlets, and N is the number of inlets. For example, 90 degrees ≤ 0 ≤ 270 degrees when the number of the inlets is two, and 60 degrees ≤ θ ≤ 180 degrees when the number of the inlets is three.

When θ is in the above-described angle range, the water inlets 45 are not overlapped, and water can be uniformly sprayed on the surface of the upper portion of the glowing coke layer 30 in the prechamber.

Fig. 9A is a diagram showing the case where the number N of the intake holes 45 is 2 and the angle θ is 180 °, and in Fig. 9B, N is 3 and θ is 120 °. The figure which shows the spray water spray range 44 in the case.

Air and water or vapor blown into the prechamber is suitably blown into the upper portion 30 of the glowing coke layer in the prechamber or into a space 31 consisting of the surface of the glowing coke layer and the prechamber. When air, water, or steam is blown into the red coke layer 32, the reaction proceeds only in the coke in which these gases are blown, resulting in uneven dispersion of the gas, resulting in uneven temperature distribution and reactivity in the prechamber cross section. Because.

In addition, air and water or steam bounced back from the coke layer are locally applied to the wall stones near the intake port, causing damage to the bricks by local cooling.

While the discharge of the coke 10 discharged from the inside of the cooling chamber is small in time, the coke 9 charged into the prechamber is charged in large quantities at one time, and then charging may be interrupted. Therefore, the surface position of the red coke layer upper part 30 in a prechamber changes every time.

As a height direction position of the air intake 45 of the air and water blown in from the upper part of the prechamber of this invention, as above (26) and (33) of this invention, it is upwards rather than the predetermined coke loading upper limit position in a prechamber. Is preferable.

Thereby, even if the coke loading amount in a prechamber changes with time, the air intake 45 of air and water can always be located in the upper part of a red coke layer.

When the charging speed of the red coke temporarily exceeds the coke discharge rate from the cooling chamber, the upper end of the red coke in the prechamber may exceed the coke stacking upper limit position.

In such a case, when the upper end portion of the coke loaded in the prechamber is larger than the predetermined coke stacking upper limit position as in the above (27) of the present invention, the blowing of air and water into the prechamber is stopped or the blowing amount is reduced. When the upper end of the coke falls below the upper limit position or a predetermined designated position, it is preferable to resume the blowing of water and air or to increase the blowing amount.

By performing such control, it is possible to avoid the problem that air and water are directly blown into the red coke layer and the dispersion of the gas is nonuniform. As a detection method of the coke upper end position in a prechamber, the calculation method from the coke input amount and coke discharge | emission based on the correction of a prechamber level meter can be employ | adopted.

When controlling the temperature in the prechamber below a predetermined temperature by blowing water or steam together with air in the prechamber, it is necessary to measure the temperature in the prechamber. The measured prechamber temperature is transferred to the blowing control device 17, and the blowing control device 17 controls the blowing amount of water or steam 16 or air 24 so that the prechamber temperature becomes a target temperature. do.

As a method for measuring the temperature in the prechamber, a method of measuring the atmospheric temperature or coke temperature near the inner side of the inner cylinder brick by inserting a thermometer through the wall from the outside to the prechamber portion, the inner cylinder temperature or the atmospheric temperature using a thermometer inserted in the inner cylinder brick And a method of measuring the temperature of the brick near the lower part of the prechamber with a thermocouple thermometer.

However, in all these methods, it is necessary to install a thermometer such as a thermocouple through a brick or a lower part of the prechamber, and the life of the thermometer is short, and it is necessary to replace it each time the thermometer deteriorates.

In the sloped flow portion 4 located in the middle of the fire extinguishing tower, a ring duct 5 for discharging the high heat gas having recovered the sensible heat is provided. When the ring duct 5 is observed from the side of the sloped flow part, the red coke can be directly observed through the opening of the ring duct 5.

The inventors measured the temperature of the glowing coke just below the prechamber observed through the opening of the ring duct 5 with the non-contact optical thermometer 18, and as a result, the temperature of the measured red coke was measured as the prechamber temperature. It has been found that it can be used for temperature control in the chamber, so that the temperature in the prechamber can be kept constant with sufficient precision.

The above (28), (29) and (34) of the present invention are made based on the above findings. That is, as in (34) of the present invention, a non-contact optical thermometer (18) for measuring the surface temperature of the coke immediately below the prechamber outlet is arranged, and as in (28) of the present invention, the thermometer The furnace temperature is measured, and operation management or control is performed as the temperature in the prechamber with the measurement temperature.

Further, as in (29) of the present invention, air is blown from the upper part of the prechamber into the prechamber using the surface temperature of the coke immediately below the prechamber outlet measured by the non-contact optical thermometer 18, Water or steam is blown in, and either or both of the blowing amount of the water or steam or the blowing amount of the prechamber blow air are adjusted so that the temperature in the prechamber is equal to or less than a predetermined temperature.

Unlike the thermocouple thermometers used in the past, the durability of the thermometer is greatly improved, and the frequency of replacing the thermometer is overwhelmingly reduced. Regarding the countermeasure in the case of a defective thermometer, it is enough to repair and replace the optical thermometer 18 installed in the space of the sloped flow portion 4, unlike the thermocouple thermometer installed through the brick, so that the load of the repair inspection is reduced. It can greatly reduce. As the non-contact optical thermometer 18, a radiation thermometer, a dichroic fine meter, or the like can be adopted.

Since air 24 blown into the prechamber and water or steam 26 blown into the prechamber are present, the amount of circulating gas 37 circulating between the digestion tower 1 and the waste heat boiler 7 increases. . Therefore, a part of the circulating gas must be dissipated to the outside as the dissipating gas 33 for the purpose of keeping the amount of the circulating gas constant.

When unburned gas, such as carbon monoxide and hydrogen, is contained in circulating gas, the energy which these unburned gas has cannot be collect | recovered effectively. Therefore, it is preferable to convert unburned gas contained in circulating gas into heat energy by blowing in air and burning it, and to prevent unburned gas from being contained in circulating gas at least when the circulating gas passes through the waste heat boiler.

As illustrated in FIG. 5, the air blown 25 may be recovered from the fire extinguishing tower 1 and blown from the air blower 14 in the gas directed toward the waste heat boiler 7. As a result, all of the carbon monoxide and hydrogen generated by reacting the coke with air, water and steam blown into the prechamber are burned by the air 25 blown into the circulating gas to generate carbon dioxide or water, thereby generating a waste heat boiler. By (7), energy can be effectively recovered as steam.

Second Embodiment

The present invention was applied to the coke dry fire extinguishing device shown in FIG. The cooling chamber 2 of the dry fire extinguishing device has a volume of 600 m 3 and the prechamber 3 has a volume of 300 m 3. The red coke 9 with an average temperature of 980 ° C. was cooled to an average discharge of 170 tons / H.

As the blowing device 46 for simultaneously injecting air and water into the prechamber, two were arranged in the prechamber using the one shown in FIG. The two blowing devices were arranged at θ = 180 ° in the circumferential direction. As a temperature measuring means in the prechamber, a radiation thermometer is provided at two places of the slitting flow section to measure the temperature of the glowing coke observed through the ring duct in a non-contact manner, and the prechamber has an average temperature of these two temperature measurement results. It was set as the temperature inside. Two radiation thermometers were installed at positions of 90 ° and 270 ° with the boiler side at 0 ° in the circumferential direction of the ring duct.

The upper limit of the coke loading amount in the prechamber was 120 tons, and the loading designated value was 110 tons. The blowing device 42 was installed 1 m above the coke surface in the coke stacking upper limit.

The target temperature in the prechamber is 1000 deg. C, and the amount of the prechamber blown air 24 is in the range of 5000 to 30000 Nm3 / h depending on the fluctuation of the coke discharge in order to keep the amount of steam generated in the waste heat boiler 7 constant. And the amount of prechamber blown water 26 was varied in the range of 0.5 to 2.5 t / h to maintain the temperature in the prechamber at a target.

As a result, the performance of the prechamber temperature was controlled in the range of 1000 ± 20 ° C., and no foreign matter adhered to the sloped flow portion. In addition, no damage of the bricks due to the scattering of water to the prechamber bricks was observed, and no damage of the bricks due to local cooling of the prechamber bricks was also observed. The non-contact thermometer using the radiation thermometer was stably operated for a long time.

According to this invention, it becomes possible to hold | maintain a fixed quantity constant amount of steam of a waste heat boiler in a coke dry type fire extinguishing apparatus. In addition, it becomes possible to maintain the concentration of the combustible gas component and oxygen in the circulating gas of the waste heat boiler at a value below a fixed value.

In addition, by maintaining the temperature of the prechamber portion at a constant value, it is possible to prevent foreign matter from adhering to the slipping flow portion. In addition, it is possible to maintain the waste heat boiler inlet gas temperature in a certain range to prevent thermal breakage of the boiler tube and to prevent a decrease in heat recovery efficiency in the boiler.

In addition, the amount of exhaust gas discharged from the fire extinguishing tower is maintained at a constant flow rate to prevent the rise of coke from the sloughing flow, increase the resistance of the circulating gas to air due to scattering, and to prevent wear and tear of the boiler tube, while at the same time glowing in the cooling chamber. It is possible to maximize the recovery of sensible heat from the coke.

In addition, in the coke dry fire extinguishing method and the fire extinguishing device, the water sprayed into the prechamber can be prevented from scattering on the coke by spraying the water injected into the prechamber, and the mist-free water is freed. By mixing and blowing in the air blown into a chamber, it becomes possible to spread | diffuse mist-like water uniformly and to spread | spread uniformly on the surface of the red coke in a prechamber.

Furthermore, the present invention further improves the durability of the thermometer by measuring the temperature of the glowing coke observed through the opening of the ring duct with a non-contact optical thermometer, so that the frequency of replacing the thermometer can be overwhelmingly reduced. Therefore, the present invention can significantly reduce the load of the repair inspection also in response to the failure of the thermometer.

Claims (34)

Using a fire extinguishing tower composed of a cooling chamber and a prechamber on top of it, the red coke is charged from above the prechamber, the air is blown into the prechamber, and the water or steam is blown into the hot exhaust gas discharged from the fire extinguishing tower. In the coke dry fire-extinguishing method of supplying air, it heat-exchanges the sensible heat which the said glowing coke has in an inert gas as a medium in the said cooling chamber, and heat-recovers in the form of steam with a waste heat boiler. The amount of air and water or steam blown into the prechamber is adjusted so that the amount of heat input to the furnace is a target value, and the amount of air supplied to the waste heat boiler (hereinafter referred to as "SF air") At the time of adjustment, the adjustment amount and the amount of water or steam (hereinafter referred to as "PC water and steam") blown into the prechamber The ratio of the adjustment amount of the air blown into the chamber (hereinafter referred to as "PC air") is determined to keep the temperature in the prechamber constant, and the adjustment amount of SF air, the adjustment amount of PC air, and the adjustment amount of PC water and steam The ratio of to is determined to keep the concentrations of the combustible gas components and oxygen in the circulating gas constant, and to modify the target value of heat input to the waste heat boiler so that the steam generation amount of the waste heat boiler becomes a target value. . delete delete The coke dry fire extinguishing method according to claim 1, wherein the steam generation amount of the waste heat boiler is adjusted to a target value instead of the heat input amount into the waste heat boiler. The coke dry fire extinguishing method according to claim 1, wherein the waste heat boiler inlet gas temperature is adjusted to a target value instead of the heat input to the waste heat boiler. delete The adjustment of the amount of PC air, PC water, steam, SF air according to any one of claims 1, 4, or 5, detects a change in the amount of coke discharge from the digestion tower, and detects the detected amount. A coke dry fire extinguishing method, characterized in that the amount of heat input to a waste heat boiler is adjusted so as to compensate for a change in coke sensible heat recovery due to a change in coke discharge. The adjustment of the amount of the PC air, the PC water, the steam, and the SF air detects fluctuations in the amount of circulating gas, and coke due to the detected fluctuations in the amount of circulating gas. A coke dry fire extinguishing method, characterized in that the amount of heat input to a waste heat boiler is adjusted to compensate for variations in the sensible heat recovery amount. The air (SF air) of any one of Claims 1, 4 or 5 is supplied to the high temperature exhaust gas discharged from the digestion tower until it reaches the waste heat boiler, and the PC air, PC Coke dry fire extinguishing method characterized in that the adjustment of the amount of water and steam is detected by the SF air volume change to compensate for the fluctuation of the boiler heat input due to the detected SF air volume change to adjust the heat input to the waste heat boiler to a target value. . A part of the gas discharged from the said waste heat boiler and supplied to a cooling chamber is branched, and the said branched gas (henceforth a "bypass gas") in any one of Claims 1-4. Is combined with the waste heat boiler feed gas, and the adjustment of the amount of the PC air, the PC water, the steam, and the SF air detects a change in the amount of blown gas supplied to the cooling chamber, and is caused by a change in the amount of blown gas supplied to the detected cooling chamber. A coke dry fire extinguishing method, characterized in that the amount of heat input to a waste heat boiler is adjusted to compensate for the fluctuation of the coke sensible heat recovery amount. The circulating gas flow rate according to any one of claims 1, 4, and 5, wherein the waste heat boiler feed gas temperature is detected, and the detected waste heat boiler feed gas temperature exceeds a predetermined upper and lower limit. Coke dry fire extinguishing method, characterized in that for increasing and decreasing the boiler inlet temperature within the upper and lower limits. The amount of said SF air is adjusted so that carbon monoxide concentration or hydrogen concentration in the gas which circulates through the said waste heat boiler, or circulating gas calorific value by these gas components becomes constant, and oxygen concentration may become below a fixed concentration. Coke dry fire extinguishing method, characterized in that. 13. The method of claim 12, wherein the adjustment of the amount of SF air sets a target value for the carbon monoxide concentration in the gas circulating in the waste heat boiler, and sets an upper limit, a lower limit, and a target value for the oxygen concentration in the gas so that the carbon monoxide concentration becomes the target value. When the amount of SF air is adjusted, and when the oxygen concentration exceeds the upper limit, the adjustment of the amount of SF air by the carbon monoxide concentration is stopped to adjust the amount of SF air so that the oxygen concentration becomes the target value, and the oxygen concentration is the target value or the lower limit value. And adjusting the amount of SF air by the carbon monoxide concentration when the oxygen concentration is lower than the target value or the lower limit and the carbon oxide concentration is higher than the target value. 13. The method of claim 12, wherein the adjustment of the amount of SF air sets a target value for the hydrogen concentration in the gas circulating in the waste heat boiler, and sets an upper limit, a lower limit, and a target value for the oxygen concentration in the gas so that the hydrogen concentration becomes the target value. When the amount of SF air is adjusted and the oxygen concentration exceeds the upper limit, the adjustment of the amount of SF air by the hydrogen concentration is stopped to adjust the amount of SF air so that the oxygen concentration becomes the target value, and the oxygen concentration is the target value or the lower limit value. When the oxygen concentration is lower than the target value or the lower limit, and the hydrogen concentration is higher than the target value, the adjustment of the amount of SF air by the hydrogen concentration is resumed. The method according to claim 12, wherein the adjustment of the amount of SF air is a circulating gas calorific value by adding the product of the concentration of carbon monoxide in the gas circulating waste heat boiler and the calorific value of carbon monoxide by the product of the hydrogen concentration in the gas and the calorific value of hydrogen. The target value is set at, the upper limit value, the lower limit value and the target value are set to the oxygen concentration in the gas, the amount of SF air is adjusted so that the circulating gas calorific value becomes the target value, and when the oxygen concentration is the upper limit value, By adjusting the amount of SF air so that the oxygen concentration becomes the target value, the oxygen concentration is lower than the target value or the lower limit, or the oxygen concentration is lower than the target value or the lower limit, and the circulating gas calorific value is the target value. When exceeding, adjust the amount of SF air by the amount of circulating gas generated. The coke dry fire extinguishing method characterized by the resumption. The method according to any one of claims 12 to 15, wherein the adjustment of the amount of SF air detects a change in the amount of coke discharge from the digestion tower, and circulates the waste heat boiler by the change in the amount of detected coke discharge. Coke dry fire extinguishing method characterized in that the adjustment to prevent the fluctuation of carbon monoxide concentration or hydrogen concentration in the gas or the circulating gas heating value and oxygen concentration. 16. The waste heat according to any one of claims 12 to 15, wherein the adjustment of the amount of SF air detects a change in the amount of PC air or a amount of PC water and steam, and the waste heat caused by a change in the detected amount of PC air or amount of PC water and steam. A coke dry fire extinguishing method, characterized in that the carbon monoxide concentration or hydrogen concentration in the gas circulating the boiler is adjusted to prevent variations in the circulating gas calorific value and oxygen concentration. The method according to any one of claims 12 to 15, wherein air (PC air) is blown into the prechamber, or water or steam (PC water and steam) is blown to the carbon monoxide concentration or hydrogen concentration or the circulating gas calorific value. In adjusting the amount of SF air by adjusting the amount of SF air and the amount of PC air or PC water and steam at the same time, the ratio of the decrease of PC air or PC water and steam to the increase of SF air is a waste heat boiler. Coke dry fire extinguishing method characterized in that the heat input of the furnace is determined to be constant. The coke dry fire extinguishing method according to claim 18, wherein the ratio of the adjustment amount of PC water and steam to the adjustment amount of PC air is determined so as to keep the temperature in the prechamber constant. The hot exhaust gas of claim 1, wherein a part of the gas discharged from the waste heat boiler and supplied to the cooling chamber is branched to join the branched gas (bypass gas) to the waste heat boiler supply gas, and discharged from the digester. Coke dry fire extinguishing method characterized in that for adjusting the amount of the bypass gas so that the amount of the target value. The amount of the bypass gas according to claim 20, wherein instead of the amount of hot exhaust gas discharged from the digestion tower, the amount of the bypass gas is adjusted so that the boiler feed gas pressure measured from the digester outlet to the waste heat boiler inlet is a target value. Coke dry fire extinguishing method characterized in that. 2. The method according to claim 1, wherein when the temperature in the prechamber is measured and there is a difference between the measured temperature in the prechamber and a target value, the value of the ratio of the adjustment amount of the PC water and steam and the adjustment amount of the PC air is corrected. Coke dry fire extinguishing method characterized in that the temperature in the chamber is adjusted to a target value. A fire extinguishing tower comprising a cooling chamber and a prechamber on the upper side thereof, and charging the coke from above the prechamber; a blowing device for blowing air into the prechamber; or blowing water or steam; and the sensible heat of the coke. In a coke dry fire extinguishing device having a waste heat boiler in which a heat exchange of an inert gas as a medium in the cooling chamber and heat recovery of sensible heat of hot gas discharged from a fire extinguishing tower in the form of steam, The SF air blowing device for supplying SF air) and a part of the gas discharged from the waste heat boiler and supplied to the cooling chamber as an inert gas, and joining the branched gas (bypass gas) to the waste heat boiler supply gas. With a pass pipe, from which the hot gas is discharged from the digester tower and introduced into the waste heat boiler. A coke dry fire extinguishing device, characterized in that the confluence position of the bypass pipe is located upstream (the boiler side) from the SF air inlet. The coke dry fire extinguishing method according to claim 1, wherein the water blown into the prechamber is sprayed into a mist, and the water of the mist is mixed with the air blown into the prechamber. 25. The method according to claim 24, wherein the prechamber has two or more air inlets for blowing air and water into the prechamber in the circumferential direction of the prechamber, and the prechamber circumferential angle? Between the adjacent air inlets is arranged within the following range. Coke dry fire extinguishing method characterized in that. 0.5 × (360 / N) ≤ θ (°) ≤ 1.5 × (360 / N) Where θ is the prechamber circumferential angle between adjacent inlets, and N is the number of inlets. The coke dry fire extinguishing method according to claim 24 or 25, wherein the height direction position of the air inlet for blowing air and water into the prechamber is higher than a predetermined coke load upper limit position in the prechamber. 27. The method according to claim 26, wherein when the upper end of the coke stacked in the prechamber exceeds the predetermined upper limit of the coke stacking position, the blowing of air and water into the prechamber is stopped and the blowing amount is further reduced. The coke dry fire extinguishing method characterized by resuming the blowing of water and air, or increasing the blowing amount when it is less than an upper limit position or predetermined predetermined position. delete delete The cooling chamber which heat-exchanges the sensible heat which a red heat coke has with an inert gas as a medium, the digestion tower which consists of the prechamber of the upper part of the said cooling chamber, and the waste heat boiler which collect | recovers the heat of an inert gas in the form of steam, The upper part of the said prechamber In the coke dry fire extinguishing device having a blowing device for blowing air and water into the prechamber, the blowing device sprays the water in a mist form, mixed with air and blown into the prechamber, and at that time the blowing device A coke dry fire extinguishing device having two water spray nozzles disposed up and down in an air blowing pipe, wherein the water spray nozzle sprays water at a wide angle in a horizontal direction and at a narrow angle in a vertical direction. delete 31. The coke according to claim 30, wherein the blower opening has two or more blowholes in the circumferential direction of the prechamber, and the prechamber circumferential angle? Between the adjacent blowholes is arranged within the following range. Dry fire extinguishing device. 0.5 × (360 / N) ≤ θ (°) ≤ 1.5 × (360 / N) Where θ is the prechamber circumferential angle between adjacent inlets, and N is the number of inlets. The coke dry fire extinguishing device according to claim 30 or 32, wherein the height direction position of the blower opening of the blower is higher than a predetermined coke stacking upper limit position in the prechamber. The cooling chamber which heat-exchanges the sensible heat which a red heat coke has with an inert gas as a medium, the digestion tower which consists of the prechamber of the upper part of the said cooling chamber, and the waste heat boiler which collect | recovers the heat of an inert gas in the form of steam, The upper part of the said prechamber In the coke dry fire extinguishing device having a blowing device for blowing air and water or steam in the prechamber, a coke dry fire extinguishing device having a non-contact optical thermometer for measuring the surface temperature of the coke immediately below the prechamber outlet .

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