CA1128895A - Process for recovering superfluous gas in coke dry quenching process and an apparatus therefor - Google Patents
Process for recovering superfluous gas in coke dry quenching process and an apparatus thereforInfo
- Publication number
- CA1128895A CA1128895A CA323,710A CA323710A CA1128895A CA 1128895 A CA1128895 A CA 1128895A CA 323710 A CA323710 A CA 323710A CA 1128895 A CA1128895 A CA 1128895A
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- Prior art keywords
- gas
- superfluous
- circulating
- cooling tower
- pressure
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
Abstract
Abstract of the Disclosure A superfluous circulating gas in the coke dry quenching installation, which is obtained by adjusting addition of a diluting gas to the circulating gas to cool the cooling tower for red heated coke discharged from the coke oven so that the composition of the superfluous gas is more than 4% of H2, more than 14% of CO, less than 1% of O2 and the caloritic value being more than 700 Kca?/Nm3, is branched from the circulating gas pipe and reused for supplementing the fuel gas from the coke oven.
Description
~ ~ ~ 8 ~ 5 The present invention relates to a process for recovering superfluous circulating gas in coke dry quenching process, more perticularly to a process for increasing the calory of the gas discharged from a cooling tower so as to be reused and recovering such a gas, and to an apparatus for recovering such a gas sa-fely and smoothly as a fuel gas, which is fed to suction main of coke oven and the like.
In general, in the coke dry quenching installation, the red heated coke is charged in a cooling tower and an inert gas at about 180C is blown into the tower from the lower portion to cool the red heated coke and the highly heated exhaust gas formed by heat exchanging with the red heated coke is introduced into a heat exchanger, such as a boiler using the exhaust heat to recover the sensible heat.
When the above described inert gas is being circulated after blowing into the cooling tower, hydrogen generated from the red heated coke and carbon monoxide generated by combustion of coke are mixed in the inert gas, so that it is necessary to restrain these gas components in a low concentration in order to reuse for the cooling by circulation and heretofore the concentration of hydrogen and carbon monoxide is diluted by using nitrogen or diluting ~combusting) air and the superfluous gas is discharged from an upper or lower bleeder into the atmosphere.
Upon diluting such a circulating gas, it is necessary to make the composition of the circulating gas not to explode and the diluting has been carried out for lowering the concentration of hydrogen and carbon monoxide in the superfluous gas. Therefore, the superfluous circulating gas discharged from the bleeder is small in the caloritic value
In general, in the coke dry quenching installation, the red heated coke is charged in a cooling tower and an inert gas at about 180C is blown into the tower from the lower portion to cool the red heated coke and the highly heated exhaust gas formed by heat exchanging with the red heated coke is introduced into a heat exchanger, such as a boiler using the exhaust heat to recover the sensible heat.
When the above described inert gas is being circulated after blowing into the cooling tower, hydrogen generated from the red heated coke and carbon monoxide generated by combustion of coke are mixed in the inert gas, so that it is necessary to restrain these gas components in a low concentration in order to reuse for the cooling by circulation and heretofore the concentration of hydrogen and carbon monoxide is diluted by using nitrogen or diluting ~combusting) air and the superfluous gas is discharged from an upper or lower bleeder into the atmosphere.
Upon diluting such a circulating gas, it is necessary to make the composition of the circulating gas not to explode and the diluting has been carried out for lowering the concentration of hydrogen and carbon monoxide in the superfluous gas. Therefore, the superfluous circulating gas discharged from the bleeder is small in the caloritic value
- 2 -8~5 and has not been reused and has been directly discharged into the atmosphere after combustion treatment or removing dusts.
In such an operation that a large amount of the diluting air and the like is used, the combustion of H2 and CO in the cir-culating gas (H2-~1/202~H2O, CO~l/202~CO2) occurs and the formed H2O and CO2 cause the reduction reaction (C+CO2~CO, C+H2O~CO+H2) at the upper portion of the cooling tower resulting into combus-tion of the red heated coke charged in the tower, so that the yield of coke disadvantageously is lowered.
lO. The present invention provides a process for recovering a superfluous circulating cooling gas discharged from a cooling tower in a coke dry quenching installation, which comprises adding a gas such as air and/or nitrogen to a cooling gas circulating in the coke dry quenching installation in such an amount that the composition of the circulating cooling gas is more than 4% of H2, more than 14% of CO, and less than 1% of 2~ and the caloritic value is more than 700 Xcal/Nm3 and discharging and recovering from the coke dry quenching installation an amount of the circula-ting cooling gas corresponding to the superfluous amount caused by addition of said at least one gas while adjusting the inner pres-sure of a prechamber portion in the cooling tower to a predeter-mined pressure by controlling the pressure of the circulating gas flow in a circulating gas pipe at an inlet position to the cooling tower for the circulating gas flow to a predetermined value.
The present invention will be explained in more detail.
For a better understanding of the invention, reference is taken to the accompanying drawing, wherein:
Fig. l is a schematic partially sectional view of an apparatus of coke dry quenching according to the present invention;
Fig. 2 is a view for showing relation of the amount of air fed into the circulating system to the amount of the superfluous gas and the caloritic value of the ~ 1 ~ 8 ~ 5 superfluous gas, and Fig. 3 is a diagrammatic view of the gas flow of the apparatus for recovering the superfluous gas in the coke dry quenching.
Re-ferring Fig. 1, the numeral 1 shows a backet elevating tower, the numeral 2 shows a backet and the numeral
In such an operation that a large amount of the diluting air and the like is used, the combustion of H2 and CO in the cir-culating gas (H2-~1/202~H2O, CO~l/202~CO2) occurs and the formed H2O and CO2 cause the reduction reaction (C+CO2~CO, C+H2O~CO+H2) at the upper portion of the cooling tower resulting into combus-tion of the red heated coke charged in the tower, so that the yield of coke disadvantageously is lowered.
lO. The present invention provides a process for recovering a superfluous circulating cooling gas discharged from a cooling tower in a coke dry quenching installation, which comprises adding a gas such as air and/or nitrogen to a cooling gas circulating in the coke dry quenching installation in such an amount that the composition of the circulating cooling gas is more than 4% of H2, more than 14% of CO, and less than 1% of 2~ and the caloritic value is more than 700 Xcal/Nm3 and discharging and recovering from the coke dry quenching installation an amount of the circula-ting cooling gas corresponding to the superfluous amount caused by addition of said at least one gas while adjusting the inner pres-sure of a prechamber portion in the cooling tower to a predeter-mined pressure by controlling the pressure of the circulating gas flow in a circulating gas pipe at an inlet position to the cooling tower for the circulating gas flow to a predetermined value.
The present invention will be explained in more detail.
For a better understanding of the invention, reference is taken to the accompanying drawing, wherein:
Fig. l is a schematic partially sectional view of an apparatus of coke dry quenching according to the present invention;
Fig. 2 is a view for showing relation of the amount of air fed into the circulating system to the amount of the superfluous gas and the caloritic value of the ~ 1 ~ 8 ~ 5 superfluous gas, and Fig. 3 is a diagrammatic view of the gas flow of the apparatus for recovering the superfluous gas in the coke dry quenching.
Re-ferring Fig. 1, the numeral 1 shows a backet elevating tower, the numeral 2 shows a backet and the numeral
3 shows a cooling tower, at the upper portion of which is provided a hopper 3a and said cooling tower is constituted with a prechamber 3b at the upper portion and a cooling chamber 3c at the lower portion. Below the cooling chamber 3c are provided a means 4 for taking out the coke, a dis-charing device 5 and a conveyor 6 in said order. At the upper end of the cooling chamber 3c of the cooling tower 3, that is, at the side wall at the lower end portion of the prechamber 3b is provided a circular smoke channel 7 and the smoke channel 7 is connected to a circulating passageway 8.
In the circulating passageway 8, a primary dust removing device 9, a boiler 10 using waste heat, a secondary dust removing device 11 and a blower 12 are provided and the end of said passageway is connected to the lower end of the cooling tower 3. At the upper end portion of the cooling tower 3, an upper bleeder 13 is provided and at the circulat-ing passageway positioning at the inlet side of the cooling tower 3, a lower bleeder 14 is provided.
Red heated coke taken out from a coke oven ~not - shown) is charged in the prechamber 3b from the hopper 3a through the backet 2, is cooled during falling down in the cooling chamber 3c and taken out at a constant speed from the above described means 4 at the lower portion of the cooling tower.
In the circulating passageway 8, a primary dust removing device 9, a boiler 10 using waste heat, a secondary dust removing device 11 and a blower 12 are provided and the end of said passageway is connected to the lower end of the cooling tower 3. At the upper end portion of the cooling tower 3, an upper bleeder 13 is provided and at the circulat-ing passageway positioning at the inlet side of the cooling tower 3, a lower bleeder 14 is provided.
Red heated coke taken out from a coke oven ~not - shown) is charged in the prechamber 3b from the hopper 3a through the backet 2, is cooled during falling down in the cooling chamber 3c and taken out at a constant speed from the above described means 4 at the lower portion of the cooling tower.
- 4 ~ ~ ~ 8 ~ 5 The circulating gas is circulated in the passageway 8 and the cooling tower by the blower 12 and the gas blown into the tower from the lower portion of the cooling chamber 3c is heat exchanged with the red heated coke while being raised in opposite to falling down of the coke to cool the coke. The gas raised temperature by the heat exchange is sucked into the above described circular channel 7 and reaches the circulating passageway 8 and reaches the waste heat boiler 10 through the primary dust removing device 9 to effect heat exchange and make vapor, and dusts are addition-ally removed by the secondary dust removing device 11 and then the gas is increased in the pressure by a blower 12 and again blown into the cooling tower 3.
In the above described circulating system, H2 and CO generated when the red heated coke is cooled, are mixed and increased in the circulating gas, so that in order to dilute said gas components, diluting gasses, such as combust-ing air and/or nitrogen are added thereto. Such an addition is conducted by a pipe 16 for blowing air through a regulating valve lS, which is provided at the circular channel 7 or a pipe 18 for blowing nitrogen through a regulating valve 17, which is connected to the circulating passageway 8 near the blower 12.
As the other diluting gas, there is air which penetrates into the cooling tower 3 when the backet 2" is mounted on and removed from the hopper 3a. However, a major part (about 60~ of the total air) of air is fed into the cooling tower 3 from the above described pipe 16, so that if the amount of this air is controlled, the composition of the circulating gas can be controlled.
~ 5 The present invention is the process wherein a gas having a high calory as fuel gas, that is a caloritic value of more than 700 ICcaQ/Nm3 is taken out from a gas recovering pipe 19, which is branched from a pipe for a lower bleeder 14. For obtaining such a high calory, the diluting gas is added and adjusted so that the composition of the circulating gas becomes less than 1% of O~, more than 4% of H~ and more than 14% (preferably, 20-23%) of CO, said % being by volume.
The gas pressure in the circulating system is regulated by taking out the circulating gas (recovering the superfluous gas) by controlling a pressure regulating device 20 and a regulating valve 21 of a gas recovering pipe 19, so that the inner pressure at the prechamber 3b portion becomes the desired pressure (usually 0-5 mm AqG). Of course, it is possible to adjust the circulating gas by discharging said gas from the upper and lower bleeders.
The reason why the gas recovering pipe 19 is provided at the lower bleeder 14 portion, is that the pressure of the ; gas is higher than the upper bleeder 13 and is stable, so that the discharging of the gas is easy, and the composition of the gas is constant and the necessary composition can be easily obtained and the composition of the circulating gas can be easily controlled. However, it is possible to recover the circulating gas from the upper bleeder 13.
Z5 Then, the present invention will be explained with - respect to an example but is not limited by this example.
Fig. 2 shows the relation of the amount of air entered into the circulating system to the amount of the superfluous gas and the caloritic value thereof, when in the installation of the specification as shown in the following Table 1, an amount of coke treated ~to be cooled) is 56 ton/hr. an amount of the circulating gas is 81,000 Nm3/hr. and air is used as the diluting gas. The following Table 2 shows the composition of the superfluous gas in this case.
Table 1 Item Specification Capacity of ~reating coke 52-56 ton/hr.
Temperature of charged coke 950-1,050C
(red heated coke) Temperature of discharged coke 200-250C
(cooled coke) Volume of prechamber about 120 m3 Volume of cooling chamber 250 m3 Gas temperature at inlet of boiler 750-800C
Gas temperature at inlet of 170-180C
cooling chamber Amount of circulating gas about 1,500 Nm3/ton per ton cf coke I'able 2 Gas composition (VoQ %) Air amount No. (Nm3/hr) H2 2 N~ CH4 CO C02 __ _ 1 1730 5.40 0.85 67.99 tr 21.16 4.60 2 1610 8.02 0.88 65.20 0.01 21.69 4.20 _ .
3 1450 11.56 O.Z4 6Z.04 O.OZ 2Z.54 3.60 4 1060 9.34 0.25 64.68 0.01 23.42 2.30 700 16.Z8 0.23 59.Z9 O.OZ Z3.18 1.00 As seen from Fig. 2, the amount of the superfluous gas is increased with increase of the total amount of air introduced into the circulating system, while the heat generating amount lowers but if the total amount of air is within the range of less than 2,200 Nm3/hr., the superfluous gas having the caloritic value of 700 KcaQ/Nm3 can be recovered. It is considered that an average amount of air penetrated into the cooling tower from the upper portion of said tower is about 800 Nm3/hr., so that in the practical operation, it is presumed that the total amount of air introduced into the circulating system is 800-2,200 Nm3/hr.
(the pure amount of the diluting air is 0-1,400 Nm3/hr.) and the adjustment is carried out so that the superfluous gas having a caloritic value of 1,050-700 ICcaQ/Nm3 is recovered.
In this example, it is presumed that the maximum value can be obtained when the total amount of air is about 2,500 Nm3/hr.
and it should be intended to obtain this maximum value in view of the heat recovery but when the amount of air is larger, the loss of coke due to combustion increases, so that such a value is not preferable. Furthermore, the caloritic value of the superfluous gas lowers. Accordingly, such a value is not practical. Moreover, it can be easily conceived from the result of this test that when nitrogen is used as the diluting gas, the loss of coke due to combustion more decreases, while the amount of CO generated becomes smaller, so that the caloritic value of the superfluous gas more or less lowers as compared with the above case where air is used, but if the amount of the diluting nitrogen is small, it is possible to recover the gas of more than 700 KcaQ/Nm3.
As mentioned above, according to the present invention, it is possible to recover the gas containing a large amount of hydrogen and carbon monoxide and a high calory as the superfluous gas and the present invention is advantageous in view of the cost of production of coke and since the superfluous gas is not discharged as it is, the combustion treatment is not necessary, so that the treating installation for the combustion is not necessary.
Furthermore, since the superfluous circulating gas having a high calory is obtained by decreasing the amount of the diluting gas, the gas amount is decreased and the loss of the red heated coke due to combustion can be reduced to improve the yield o-f coke.
Moreover, the present invention also relates to an apparatus for recovering the superfluous gas in the coke dry quenching installation and an explanation will be made with respect to the second aspect of the present invention.
When the superfluous gas is taken out from the above described circulating system and used for fuel gas, the taken out superfluous gas has been heretofore directly connected ; to a fuel gas pipe without controlling the superfluous gas flow. Therefore, there have been the following defects.
1) By taking out the superfluous gas from the circulating gas system, the pressure in the circulating gas system varies and the operation in the coke dry quenching installa-tion is unstable.
2) When the pressure at the outlet of the superfluous gas is positive and the pressure at the fuel gas pipe to which the superfluous gas is introduced, is negative, on the way of the gas pipe, there is a fear that a negative pressure ~ 2~8~5 zone is formed and air is sucked in. Accordingly, at the portions in the pipe where is poor in the sealing ability or is readily corroded, that is at the pressure raising blower or the dust removing device, it is necessary to adjust the pressure of the superfluous gas to become the positive pressure, but the conventional installation has a defect in this point.
3) Upon abnormal stop of the blower at the side of the coke dry quenching installation or the blower for raising pressure in order to transfer the superfluous gas, the conventional pipe has no stopping mechanism, so that there is the fear that the admixture of air or the reverse flow of gas occur.
4) In the case of the conventional apparatus, if there is a great difference in the caloritic value between the super-fluous gas and the fuel gas, the combustion of the fuel gas becomes unstable, becuase any means for previously mixing these gasses is not provided.
In the above described circulating system, H2 and CO generated when the red heated coke is cooled, are mixed and increased in the circulating gas, so that in order to dilute said gas components, diluting gasses, such as combust-ing air and/or nitrogen are added thereto. Such an addition is conducted by a pipe 16 for blowing air through a regulating valve lS, which is provided at the circular channel 7 or a pipe 18 for blowing nitrogen through a regulating valve 17, which is connected to the circulating passageway 8 near the blower 12.
As the other diluting gas, there is air which penetrates into the cooling tower 3 when the backet 2" is mounted on and removed from the hopper 3a. However, a major part (about 60~ of the total air) of air is fed into the cooling tower 3 from the above described pipe 16, so that if the amount of this air is controlled, the composition of the circulating gas can be controlled.
~ 5 The present invention is the process wherein a gas having a high calory as fuel gas, that is a caloritic value of more than 700 ICcaQ/Nm3 is taken out from a gas recovering pipe 19, which is branched from a pipe for a lower bleeder 14. For obtaining such a high calory, the diluting gas is added and adjusted so that the composition of the circulating gas becomes less than 1% of O~, more than 4% of H~ and more than 14% (preferably, 20-23%) of CO, said % being by volume.
The gas pressure in the circulating system is regulated by taking out the circulating gas (recovering the superfluous gas) by controlling a pressure regulating device 20 and a regulating valve 21 of a gas recovering pipe 19, so that the inner pressure at the prechamber 3b portion becomes the desired pressure (usually 0-5 mm AqG). Of course, it is possible to adjust the circulating gas by discharging said gas from the upper and lower bleeders.
The reason why the gas recovering pipe 19 is provided at the lower bleeder 14 portion, is that the pressure of the ; gas is higher than the upper bleeder 13 and is stable, so that the discharging of the gas is easy, and the composition of the gas is constant and the necessary composition can be easily obtained and the composition of the circulating gas can be easily controlled. However, it is possible to recover the circulating gas from the upper bleeder 13.
Z5 Then, the present invention will be explained with - respect to an example but is not limited by this example.
Fig. 2 shows the relation of the amount of air entered into the circulating system to the amount of the superfluous gas and the caloritic value thereof, when in the installation of the specification as shown in the following Table 1, an amount of coke treated ~to be cooled) is 56 ton/hr. an amount of the circulating gas is 81,000 Nm3/hr. and air is used as the diluting gas. The following Table 2 shows the composition of the superfluous gas in this case.
Table 1 Item Specification Capacity of ~reating coke 52-56 ton/hr.
Temperature of charged coke 950-1,050C
(red heated coke) Temperature of discharged coke 200-250C
(cooled coke) Volume of prechamber about 120 m3 Volume of cooling chamber 250 m3 Gas temperature at inlet of boiler 750-800C
Gas temperature at inlet of 170-180C
cooling chamber Amount of circulating gas about 1,500 Nm3/ton per ton cf coke I'able 2 Gas composition (VoQ %) Air amount No. (Nm3/hr) H2 2 N~ CH4 CO C02 __ _ 1 1730 5.40 0.85 67.99 tr 21.16 4.60 2 1610 8.02 0.88 65.20 0.01 21.69 4.20 _ .
3 1450 11.56 O.Z4 6Z.04 O.OZ 2Z.54 3.60 4 1060 9.34 0.25 64.68 0.01 23.42 2.30 700 16.Z8 0.23 59.Z9 O.OZ Z3.18 1.00 As seen from Fig. 2, the amount of the superfluous gas is increased with increase of the total amount of air introduced into the circulating system, while the heat generating amount lowers but if the total amount of air is within the range of less than 2,200 Nm3/hr., the superfluous gas having the caloritic value of 700 KcaQ/Nm3 can be recovered. It is considered that an average amount of air penetrated into the cooling tower from the upper portion of said tower is about 800 Nm3/hr., so that in the practical operation, it is presumed that the total amount of air introduced into the circulating system is 800-2,200 Nm3/hr.
(the pure amount of the diluting air is 0-1,400 Nm3/hr.) and the adjustment is carried out so that the superfluous gas having a caloritic value of 1,050-700 ICcaQ/Nm3 is recovered.
In this example, it is presumed that the maximum value can be obtained when the total amount of air is about 2,500 Nm3/hr.
and it should be intended to obtain this maximum value in view of the heat recovery but when the amount of air is larger, the loss of coke due to combustion increases, so that such a value is not preferable. Furthermore, the caloritic value of the superfluous gas lowers. Accordingly, such a value is not practical. Moreover, it can be easily conceived from the result of this test that when nitrogen is used as the diluting gas, the loss of coke due to combustion more decreases, while the amount of CO generated becomes smaller, so that the caloritic value of the superfluous gas more or less lowers as compared with the above case where air is used, but if the amount of the diluting nitrogen is small, it is possible to recover the gas of more than 700 KcaQ/Nm3.
As mentioned above, according to the present invention, it is possible to recover the gas containing a large amount of hydrogen and carbon monoxide and a high calory as the superfluous gas and the present invention is advantageous in view of the cost of production of coke and since the superfluous gas is not discharged as it is, the combustion treatment is not necessary, so that the treating installation for the combustion is not necessary.
Furthermore, since the superfluous circulating gas having a high calory is obtained by decreasing the amount of the diluting gas, the gas amount is decreased and the loss of the red heated coke due to combustion can be reduced to improve the yield o-f coke.
Moreover, the present invention also relates to an apparatus for recovering the superfluous gas in the coke dry quenching installation and an explanation will be made with respect to the second aspect of the present invention.
When the superfluous gas is taken out from the above described circulating system and used for fuel gas, the taken out superfluous gas has been heretofore directly connected ; to a fuel gas pipe without controlling the superfluous gas flow. Therefore, there have been the following defects.
1) By taking out the superfluous gas from the circulating gas system, the pressure in the circulating gas system varies and the operation in the coke dry quenching installa-tion is unstable.
2) When the pressure at the outlet of the superfluous gas is positive and the pressure at the fuel gas pipe to which the superfluous gas is introduced, is negative, on the way of the gas pipe, there is a fear that a negative pressure ~ 2~8~5 zone is formed and air is sucked in. Accordingly, at the portions in the pipe where is poor in the sealing ability or is readily corroded, that is at the pressure raising blower or the dust removing device, it is necessary to adjust the pressure of the superfluous gas to become the positive pressure, but the conventional installation has a defect in this point.
3) Upon abnormal stop of the blower at the side of the coke dry quenching installation or the blower for raising pressure in order to transfer the superfluous gas, the conventional pipe has no stopping mechanism, so that there is the fear that the admixture of air or the reverse flow of gas occur.
4) In the case of the conventional apparatus, if there is a great difference in the caloritic value between the super-fluous gas and the fuel gas, the combustion of the fuel gas becomes unstable, becuase any means for previously mixing these gasses is not provided.
5) In usual, about 1 g/Nm3 of coke powders are contained in the superfluous gas but heretofore dusts are not removed, so that the coke powders enter into the fuel pipe as they are and a trouble, such as clogging of a burner at the use side occurs.
The object of the second aspect of the present invention is to obviate the defects of the above described prior arts and is to provide a novel apparatus for recovering the superfluous gas smoothly and safely.
The present invention consists in an apparatus wherein the prior arts have been improved with respect the following points.
~ 8 ~ ~
1) In order to take out the superfluous gas from the circulating system, the pipe for the superfluous gas is branched and a pressure regulating valve is provided at the branched pipe for taking out the super:Eluous gas to regulate the pressure at the opening for taking out the superfluous gas and to make the influence of the pressure variation to the circulating gas system smaller.
2) In the above described branched pipe for the superfluous gas, the pressure at the devices where the sealing ability is poor, such as a blower for raising pressure and a device for removing dust or the devices which are readily corroded, is regulated by providing a pressure regulator so that said pressure becomes positive pressure and it is prevented that air from the atmosphere enters into the superfluous gas to be recovered.
3) The connection to the coke dry quenching installation -and the -fuel gas pipe is cut so that air is not mixed into the fuel gas (suction main or dry main) upon abnormal stop of the blower for the circulating gas at the side of the coke dry quenching installation or the blower for raising pressure for transferring the superfluous gas. That is, on the way of the pipe for the superfluous gas, a plurality of stop valves are provided.
4) A mixing apparatus is omitted by introducing the super-fluous gas into the fuel gas pipe, such as the dry main, thesuction main and the like of the pipe for the coke oven gas without providing an apparatus for mixing the superfluous gas and the fuel gas. That is, in the pipe for the coke oven gas, the dry main or the suction main is provided at the upper stream side of the suction blower and the gas purifying installation, so that the superfluous gas and the fuel gas are fully mixed.
5) When the coke powders in the superfluous gas enter into the fuel gas without removing dusts, a trouble, such as clogging of burner may occur at the use side. For example, when the superfluous gas is connected to the dry main or the suction main of the fuel gas pipe, there is the fear that the admixing of coke powders causes trouble in the gas purifying installation. Accordingly, in order to prevent such a trouble, a dust removing apparatus is provided in the ~` superfluous gas pipe system according to the present inven-tion.
The invention will be explained` with respect to the apparatus of the present invention.
Referring to Fig. 3, the numeral 3 is a cooling tower and the tower 3 connects to the circulating passageways 8 and 8'. The numeral 13 is an upper bleeder, the numeral 12 is a blower for the circulating gas, the numeral 10 is a heat exchanger, such as a boiler, the numerals 9 and 11 are the primary and secondary dust removing devices and the numeral 8' is the superfluous gas pipe and connects to the lower portion of the cooling tower 3.
At the vicinity of the cooling tower 3 which positions at the return side of the circulating passageways 8 and 8', a pipe 19 for taking out the superfluous gas is branched from the superfluous gas pipe 8 t and another end of the pipe 19 is connected to a fuel gas pipe, such as a suction main 29 or a dry main of the coke oven. In the superfluous gas pipe 19, a pressure regulating valve 21 is provided for adjusting the pressure of the opening for taking out the superfluous gas and this pressure regulating valve also is provided at the side o-f the suction main 29 for the same purpose. At the vicinity of the upper stream of this pressure regulating valve 21, a stop valve 22 which shuts the circuit upon abnormal time, is provided. In the superfluous gas pipe 19, a discharging valve 23 is provided, so that said discharging valve operates in syncronism with the above described stop valve 22 and upon abnormal time of the installation, the valve is opened to discharge the superfluous gas into the atmosphere. In addition, the superfluous gas pipe 19 is provided with a blower 24 for transferring the superfluous gas and a dust removing device 25, such as venturi scraber. At the upper stream side of the blower 24 and at the lower stream of the venturi scraber, pressure regulating valves 26 and 27 are provided and, for example, even when the pressure in the suction main 29 is negative, the pressure is adjusted so that the pipe to the above described dust removing device 25 becomes positive.
Furthermore, preparing for the abnormal time of the cooling tower 3 and the like, a stop valve 28 is provided at the side of the suction main 29.
In such an apparatus, the pressure for taking out the above described sup0rfluous gas is adjusted to be about 150-200 mmH2O by using the pressure regulating valve 21.
The flow amount, when the treating amount of No. l-No. 3 cooling towers 3 is 40-50 t/hr.-tower is 1,000-1,500 Nm3/tower and the total amount of the three towers is 3,000-4,500 Nm3, the temperature is 150-180C, the caloritic value is 700-1,000 KcaQ/Nm3 and these superfluous gasses flow together and then are purified (1 g/Nm3-~50 mg/Nm3) at the dust removing device 25, after which the pressure of the superfluous gas is adjusted by the pressure regulating valve 27 and flowed into the suction main 29. The caloritic value of coke oven gas is about 4,~00 KcaQ/Nm3, while the caloritic value of the superfluous gas is 700-1,000 KcaQ/Nm3 and both the values are comparatively greatly different, but since the superfluous gas flows into the suction main, both the gasses are fully mixed and further an amount of ~he superfluous gas is smaller than an amount of the coke oven gas, so that the combustion at the use side does not become unstable owing to variation of the caloritic value of the superfluous gas.
As mentioned above, the superfluous gas consisting mainly of the combustive components can be safely and smoothly recovered into the fuel gas pipe according to the apparatus : 15 of the present invention and the present invention is excellent in view of the savlng energy.
' .~
- 1~ -
The object of the second aspect of the present invention is to obviate the defects of the above described prior arts and is to provide a novel apparatus for recovering the superfluous gas smoothly and safely.
The present invention consists in an apparatus wherein the prior arts have been improved with respect the following points.
~ 8 ~ ~
1) In order to take out the superfluous gas from the circulating system, the pipe for the superfluous gas is branched and a pressure regulating valve is provided at the branched pipe for taking out the super:Eluous gas to regulate the pressure at the opening for taking out the superfluous gas and to make the influence of the pressure variation to the circulating gas system smaller.
2) In the above described branched pipe for the superfluous gas, the pressure at the devices where the sealing ability is poor, such as a blower for raising pressure and a device for removing dust or the devices which are readily corroded, is regulated by providing a pressure regulator so that said pressure becomes positive pressure and it is prevented that air from the atmosphere enters into the superfluous gas to be recovered.
3) The connection to the coke dry quenching installation -and the -fuel gas pipe is cut so that air is not mixed into the fuel gas (suction main or dry main) upon abnormal stop of the blower for the circulating gas at the side of the coke dry quenching installation or the blower for raising pressure for transferring the superfluous gas. That is, on the way of the pipe for the superfluous gas, a plurality of stop valves are provided.
4) A mixing apparatus is omitted by introducing the super-fluous gas into the fuel gas pipe, such as the dry main, thesuction main and the like of the pipe for the coke oven gas without providing an apparatus for mixing the superfluous gas and the fuel gas. That is, in the pipe for the coke oven gas, the dry main or the suction main is provided at the upper stream side of the suction blower and the gas purifying installation, so that the superfluous gas and the fuel gas are fully mixed.
5) When the coke powders in the superfluous gas enter into the fuel gas without removing dusts, a trouble, such as clogging of burner may occur at the use side. For example, when the superfluous gas is connected to the dry main or the suction main of the fuel gas pipe, there is the fear that the admixing of coke powders causes trouble in the gas purifying installation. Accordingly, in order to prevent such a trouble, a dust removing apparatus is provided in the ~` superfluous gas pipe system according to the present inven-tion.
The invention will be explained` with respect to the apparatus of the present invention.
Referring to Fig. 3, the numeral 3 is a cooling tower and the tower 3 connects to the circulating passageways 8 and 8'. The numeral 13 is an upper bleeder, the numeral 12 is a blower for the circulating gas, the numeral 10 is a heat exchanger, such as a boiler, the numerals 9 and 11 are the primary and secondary dust removing devices and the numeral 8' is the superfluous gas pipe and connects to the lower portion of the cooling tower 3.
At the vicinity of the cooling tower 3 which positions at the return side of the circulating passageways 8 and 8', a pipe 19 for taking out the superfluous gas is branched from the superfluous gas pipe 8 t and another end of the pipe 19 is connected to a fuel gas pipe, such as a suction main 29 or a dry main of the coke oven. In the superfluous gas pipe 19, a pressure regulating valve 21 is provided for adjusting the pressure of the opening for taking out the superfluous gas and this pressure regulating valve also is provided at the side o-f the suction main 29 for the same purpose. At the vicinity of the upper stream of this pressure regulating valve 21, a stop valve 22 which shuts the circuit upon abnormal time, is provided. In the superfluous gas pipe 19, a discharging valve 23 is provided, so that said discharging valve operates in syncronism with the above described stop valve 22 and upon abnormal time of the installation, the valve is opened to discharge the superfluous gas into the atmosphere. In addition, the superfluous gas pipe 19 is provided with a blower 24 for transferring the superfluous gas and a dust removing device 25, such as venturi scraber. At the upper stream side of the blower 24 and at the lower stream of the venturi scraber, pressure regulating valves 26 and 27 are provided and, for example, even when the pressure in the suction main 29 is negative, the pressure is adjusted so that the pipe to the above described dust removing device 25 becomes positive.
Furthermore, preparing for the abnormal time of the cooling tower 3 and the like, a stop valve 28 is provided at the side of the suction main 29.
In such an apparatus, the pressure for taking out the above described sup0rfluous gas is adjusted to be about 150-200 mmH2O by using the pressure regulating valve 21.
The flow amount, when the treating amount of No. l-No. 3 cooling towers 3 is 40-50 t/hr.-tower is 1,000-1,500 Nm3/tower and the total amount of the three towers is 3,000-4,500 Nm3, the temperature is 150-180C, the caloritic value is 700-1,000 KcaQ/Nm3 and these superfluous gasses flow together and then are purified (1 g/Nm3-~50 mg/Nm3) at the dust removing device 25, after which the pressure of the superfluous gas is adjusted by the pressure regulating valve 27 and flowed into the suction main 29. The caloritic value of coke oven gas is about 4,~00 KcaQ/Nm3, while the caloritic value of the superfluous gas is 700-1,000 KcaQ/Nm3 and both the values are comparatively greatly different, but since the superfluous gas flows into the suction main, both the gasses are fully mixed and further an amount of ~he superfluous gas is smaller than an amount of the coke oven gas, so that the combustion at the use side does not become unstable owing to variation of the caloritic value of the superfluous gas.
As mentioned above, the superfluous gas consisting mainly of the combustive components can be safely and smoothly recovered into the fuel gas pipe according to the apparatus : 15 of the present invention and the present invention is excellent in view of the savlng energy.
' .~
- 1~ -
Claims (5)
1. A process for recovering a superfluous circulating gas discharged from a cooling tower in a coke dry quenching installation, which comprises adjusting addition of diluting gas for cooling gas blown into the cooling tower, so that the composition of the circulating gas to be used for cooling is more than 4% of H2, more than 14% of CO, less than 1% of O2 and the caloritic value being more than 700 Kcal/Nm3 and re-covering the circulating gas corresponding to the superfluous amount caused by the addition of the diluting gas while ad-justing the inner pressure of a prechamber portion in the cooling tower to a predetermined pressure by controlling the pressure of the circulating gas flow in a circulating gas pipe at an inlet position to the cooling tower for the circulating gas flow to a predetermined value.
2. The process as claimed in claim 1, wherein said diluting gas is air and nitrogen.
3. The process as claimed in claim 1, wherein the inner pressure of the prechamber of the cooling tower is 0-5 mmAqG.
4. An apparatus for recovering the superfluous gas in a coke dry quenching installation where in a cooling tower, a heat exchanger and dust removing devices are connected by a circulating gas pipe to form a closed circuit, which comprises a superfluous gas pipe branched from the vicinity of an inlet of the cooling tower of the circulating gas pipe, another end of said superfluous gas pipe being connected to a fuel gas pipe, said superfluous gas pipe being provided with pressure regulating valves, stop valves, a valve for discharging the superfluous gas operating in synchronism with the above described stop valve, a pressure raising blower and a dust removing device between the portion branches from the circulating gas pipe and the connection to the fuel gas pipe.
5. A process for recovering a superfluous circulating cooling gas discharged from a cooling tower in a coke dry quenching installation, which comprises adding at least one of the gases selected from the group consisting of air and nitrogen to a cooling gas circulating in the coke dry quenching installation in such an amount that the composition of the circulating cooling gas is more than 4% of H2, more than 14%
of CO, and less than 1% of O2, and the caloritic value is more than 700 Kcal/Nm3 and discharging and recovering from the coke dry quenching installation an amount of the circulating cooling gas corresponding to the superfluous amount caused by addition of said at least one gas while adjusting the inner pressure of a prechamber portion in the cooling tower to a predetermined pressure by controlling the pressure of the circulating gas flow in a circulating gas pipe at an inlet position to the cooling tower for the circulating gas flow to a predetermined value.
of CO, and less than 1% of O2, and the caloritic value is more than 700 Kcal/Nm3 and discharging and recovering from the coke dry quenching installation an amount of the circulating cooling gas corresponding to the superfluous amount caused by addition of said at least one gas while adjusting the inner pressure of a prechamber portion in the cooling tower to a predetermined pressure by controlling the pressure of the circulating gas flow in a circulating gas pipe at an inlet position to the cooling tower for the circulating gas flow to a predetermined value.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32,044/78 | 1978-03-20 | ||
| JP3204478A JPS54124002A (en) | 1978-03-20 | 1978-03-20 | Recovery of excess circulating gas in dry type coke extingoishing method |
| JP177,249/78 | 1978-12-27 | ||
| JP17724978U JPS5720573Y2 (en) | 1978-12-27 | 1978-12-27 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1128895A true CA1128895A (en) | 1982-08-03 |
Family
ID=26370564
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA323,710A Expired CA1128895A (en) | 1978-03-20 | 1979-03-19 | Process for recovering superfluous gas in coke dry quenching process and an apparatus therefor |
Country Status (4)
| Country | Link |
|---|---|
| CA (1) | CA1128895A (en) |
| DE (1) | DE2910936A1 (en) |
| FR (1) | FR2420564A1 (en) |
| GB (1) | GB2018965B (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3004175A1 (en) * | 1980-02-05 | 1981-08-06 | Hartung, Kuhn & Co Maschinenfabrik GmbH, 4000 Düsseldorf | Hot coke transport system - with cage for coke cap in quenching tower and transfer carriage to cooling shafts |
| DE3010286C2 (en) * | 1980-03-18 | 1983-12-29 | Gosudarstvennoe konstruktorskoe bjuro koksochimičeskogo mašinostroenija, Slavjansk, Donezkaja oblast' | Device for dry extinguishing of coke |
| FR2481711A1 (en) * | 1980-04-30 | 1981-11-06 | G K | Coke dry-quenching plant - has great manoeuvrability of lifts and thus needs fewer auxiliary machines |
| FR2502635A1 (en) * | 1981-03-24 | 1982-10-01 | Uk Uglekhimichesky Instit | Dry quenching coke with concurrent prodn. of reducing gas - in two-stage process using steam as coolant in final stage |
| DE3329163C2 (en) * | 1983-08-12 | 1985-08-01 | Didier Engineering Gmbh, 4300 Essen | Process for using the sensible heat of coke in a coking plant |
| DE3535977A1 (en) * | 1985-09-17 | 1987-04-09 | Thyssen Industrie | COCK DRY COOLING DEVICE |
| DE3612922A1 (en) * | 1986-04-17 | 1987-10-22 | Thyssen Industrie | COCK DRY COOLING DEVICE |
| DE10128021C1 (en) * | 2001-06-08 | 2002-10-10 | Montan Tech Gmbh | Dry cooling coke comprises using cooling gas that is introduced into cooling shaft containing coke |
| JP5631073B2 (en) * | 2010-06-27 | 2014-11-26 | スチールプランテック株式会社 | Coke dry fire extinguishing equipment and operation method thereof |
| CN102829639A (en) * | 2012-08-16 | 2012-12-19 | 圣火科技(河南)有限责任公司 | Generating device utilizing waste heat of dry quenched liquid dregs |
| CN116179226A (en) * | 2023-03-07 | 2023-05-30 | 山东钢铁股份有限公司 | Dry quenching method for reducing coke burning loss |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE375785C (en) * | 1921-01-03 | 1923-05-18 | Sulzer Akt Ges Geb | Process for cooling glowing coke |
| GB256727A (en) * | 1925-05-25 | 1926-08-19 | Woodall Duckham 1920 Ltd | Improvements relating to the dry-quenching or dry cooling of coke |
| FR876670A (en) * | 1940-11-12 | 1942-11-12 | Forni Ed Impianti Ind Ingg De Bartolomeis Spa | Method and apparatus for the dry quenching of coke in continuous distillation furnaces |
| US2581409A (en) * | 1948-08-17 | 1952-01-08 | Koppers Co Inc | Method of dry quenching coke |
| DE1085495B (en) * | 1954-10-19 | 1960-07-21 | Still Fa Carl | Method of dry cooling coke |
| GB1020234A (en) * | 1961-10-17 | 1966-02-16 | Yawata Iron & Steel Co | Method of emergency operation of an oxygen top-blowing converter |
| AT361892B (en) * | 1975-06-13 | 1981-04-10 | Waagner Biro Ag | METHOD AND DEVICE FOR COOLING HOT SHEET GOODS, ESPECIALLY FOR DRYING AND DELETING HOT COOK |
-
1979
- 1979-03-16 FR FR797906731A patent/FR2420564A1/en active Granted
- 1979-03-19 CA CA323,710A patent/CA1128895A/en not_active Expired
- 1979-03-20 DE DE19792910936 patent/DE2910936A1/en active Granted
- 1979-03-20 GB GB7909650A patent/GB2018965B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| GB2018965A (en) | 1979-10-24 |
| FR2420564A1 (en) | 1979-10-19 |
| DE2910936A1 (en) | 1979-10-04 |
| DE2910936C2 (en) | 1988-08-11 |
| GB2018965B (en) | 1982-10-20 |
| FR2420564B1 (en) | 1982-03-05 |
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