CA1245595A - Method for dry cooling coke using the sensible heat formed during dry cooling - Google Patents
Method for dry cooling coke using the sensible heat formed during dry coolingInfo
- Publication number
- CA1245595A CA1245595A CA000471353A CA471353A CA1245595A CA 1245595 A CA1245595 A CA 1245595A CA 000471353 A CA000471353 A CA 000471353A CA 471353 A CA471353 A CA 471353A CA 1245595 A CA1245595 A CA 1245595A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- coke
- cooler
- circulating gas
- dry
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
ABSTRACT OF THE DISCLOSURE
The invention relates to a method for dry cooling coke using the sensible heat which is formed during the dry cooling. According to the invention, a combustible gas which is used as a circulating gas, after leaving the waste gas steam boiler and before entering the coke cooling chamber, is cooled down approximately to coolant temperature in a combined washer cooler thus removing dust therefrom. Further-more, the circulating waste gas leaving the said washer cooler is passed through a cooling unit such as a heat pump like unit before entering the coke-cooling chamber. Adjustment of the calorific value of the combustible gas is effected by feeding nitrogen or cleaned flue gas into the cold circulating gas ahead of the coke dry cooler and/or by feeding air into the hot circulating gas after the dry cooler. Ahead of the dry cooler, excess cold circulating gas is withdrawn and is mixed with the under-grate-firing gas fed to the coke ovens.
The excess circulating gas may be withdrawn between the dry cooler and the preheating unit, it may be passed through a waste gas boiler, and mixed with the gas leaving the said preheating unit. The operating temperature may be adjusted by feeding the cooled gas into the duct running from the dry cooler to the said preheating unit.
The invention relates to a method for dry cooling coke using the sensible heat which is formed during the dry cooling. According to the invention, a combustible gas which is used as a circulating gas, after leaving the waste gas steam boiler and before entering the coke cooling chamber, is cooled down approximately to coolant temperature in a combined washer cooler thus removing dust therefrom. Further-more, the circulating waste gas leaving the said washer cooler is passed through a cooling unit such as a heat pump like unit before entering the coke-cooling chamber. Adjustment of the calorific value of the combustible gas is effected by feeding nitrogen or cleaned flue gas into the cold circulating gas ahead of the coke dry cooler and/or by feeding air into the hot circulating gas after the dry cooler. Ahead of the dry cooler, excess cold circulating gas is withdrawn and is mixed with the under-grate-firing gas fed to the coke ovens.
The excess circulating gas may be withdrawn between the dry cooler and the preheating unit, it may be passed through a waste gas boiler, and mixed with the gas leaving the said preheating unit. The operating temperature may be adjusted by feeding the cooled gas into the duct running from the dry cooler to the said preheating unit.
Description
~2~ssgs The invention relates to a method for utilizing the sensible heat which is formed during the dry cooling of coke by means of a gas, in which, for preheating the coal used in producing the coke, a circulating gas is passed through a waste heat boiler or the like heat consumption device and, after being freed from dust, is then returned to the coke cooling chamber, any excess gas being removed from the circuit.
In the case of known installations for cooling coke, operating in conjunction with a steam producing device, the cooling gas, after cooling in the steam boiler, is returned to - the cooling chamber at a temperature of about 150C. In order to cool the coke down to about 200C, a correspondingly large volume of cooling gas and a correspondingly large cooling chamber are needed. Since the latter is lined with refractory material, a considerable investment is required.
It is also known to preheat the coal used to produce the coke in the coke oven by means of flue gas or blast furnace gas as a carrier gas which has withdrawn the sensible heat from the coke in a coke dry cooling unit. The use of a blast furnace gas as a carrier gas is known from German Patent 27 33 365. According to this method, which is mainly suitable for steel plant coke ovens where blast furnace gas is available, the cooled gas is returned to the circuit after the coal has been heated.
In all circulating processes, the volume of circu-lating gas is increased by gasification (coke burn up) and subsequent coke degasification, and a certain amount of circulating gas must therefore be removed continuously~ In the method disclosed in British Patent 1,334,373, a flue gas is used as the carrier gas. Because of the residual oxygen content in all flue gases, the increase in gas and the loss of coke by burn up is greater than with combustible gases, and the volume of circulating gas to be carried away is also greater. This gas enriched with pollutants is released to the atmosphere, and thus requires expensive conditioning equipment, such as after burners, dust removers and possibly desul-phurizing e~uipment.
It is the aim of the present invention to provide conditions for the low cost implementation of a method for the dry cooling of coke in which the carrier gas flows in a closed circuit between the step of dry cooling of coke and that of preheating coke, any excess of circulating gas being discarded without causing pollution.
According to the invention, this aim is achieved by cooling down the circulating gas leaving the waste gas steam ~oiler, before said gas enters the coke cooling chamber, in a combined washer cooler, approximately to the cooling tempera-ture thus removing the dust from said circulating gas.
This rnakes it possible to reduce considerably the size of the coke cooling chamber. The circulating gas is not freed from dust as usual, by means of a dry separator, but with a co~bined wet washer cooler, where the said circulating gas is not only cleaned, but is cooled down to a temperature close to that of the coolant used. Since the circulating gas which is returned to the coke cooling chamber has, according to the invention, a substantially lower temperature, for example below 20C., the volume of circulating gas can be reduced considerably, and the coke cooling chamber itself may also be considerably smaller. Because of the smaller volume of circulating gas, a smaller blower using less power may be ~Z~5~5 used. The arrangement according to the invention therefore results in a considerable reduction of the investment and of the operating costs.
Moreover, by using an additional cooling unit, or a heat pump like unit, it is possible to provide additional cooling for the circulating gas leaving the washer cooler, before said gas enters the coke cooling chamber. This again reduces the volume of circulating gas and, at the same time, allows part of the water vapour to be removed from the circu-lating gas by condensation~ The resulting nearly dry gasbehaves like the circulating gas which is used in a normal dry coke cooling process and eliminates additional coke burn onO This allows the method according to the invention to be still more economical.
In accordance with a preferred ernbodiment of the invention, the clrculating gas between the coke dry cooler and the coal preheater is a combustible gas. The calorific value of the cornbustible gas is adjusted by feeding nitrogen or clean flue gas into the cold circulating gas ahead of the coke dry cooler, and/or by feeding air into the hot circulating gas after the coke dry cooler. Any excess cold circulating gas is withdrawn from the circuit ahead of the coke dry cooler and is mixed with the under-grate-firing gas to be fed to the coke ovens.
In accordance with another ernbodiment of the invention, the excess hot circulating gas, i.e. part of the circulating gas not needed to preheat the coal, is withdrawn between the coke cooling chamber and the preheating unit, after which it is passed through a waste heat boiler, and is mixed with the gas leaving the said preheating unit.
55~5 ~ccording to a preferred embodiment of the invention, part of the cooled down gas emerging from the preheating unit is withdrawn so as to adjust the operating temperature and is fed into the duct running from the coke cooling chamber to the said preheating unit~
The method according to the invention is particularly suitable for colliery coking plants and produces extremely little pollution, since the excess ~as can be mixed with the under-grate-firing gas for the coke-ovens, thus eliminating the conditioning of the equipment.
The invention will now be illustrated by means of the annexed drawings, in which:
FIGURE 1 is a diagram illustrating the method of cooling coke according to the invention, and FIGURE 2 is a diagram which illustrates another embodiment of the method according to the invention.
With reference to Figure 1 of the drawings, it will be seen that the hot circulating gas leaves the coke cooling chamber 101 at 103 and is sent to the waste heat steam boiler 105 via duct 107. The circulating gas leaves the waste heat steam boiler 105 at 109 and is thereafter sent to the combined washer cooler 111 by circulating through duct 113, which is at a temperature between 180 and 200C. It will be noted that a coolant, for example water, is introduced into the combined washer cooler 111 by means of a duct 115 from which it is sprayed into the combined washer cooler 111 by means of the spraying device 117. The hot circulating gas is passed through the combined washer cooler 111 via duct 119 and it leaves at 121.
This, in effect, removes the dust from the ~ Z~5~i9~
circulating gas and cools it to approximately the temperature of the coolant, for example about 20C. The thus cooled circulating gas is sent via duct 123, to a cooling unit 125 which operates in the same manner as, for example, a heat pump, where it is cooled down still further. The circulating gas, thus cooled down to this extent, is returned to the coke cooling chamber via duct 127, after which it is picked up by a blower 129 from which it is sent to the coke cooling chamber . 101, via duct 131.
Figure 2 illustrates another embodiment of the method according to the invention. According to this embodiment, there is provided a coke oven 1 inside of which there is a chamber 2 which is filled with preheated coal, the latter being introduced from above, through a system of ducts 3, by means of filling holes, not shown which can be closed off.
Fuel gas and combustion air are fed through ducts 5 and 6 and pass, through regenerators 4, into the flues (not shown) surrounding the oven chamber. The gases which are formed during the dry distillation are removed through riser pipes, not shown, from which they are sent into a receiver (also not shown).
The hot coke which is forced out of the coke oven at about 1000C, is removed in batches, by means of a bucket, through a pressure tight lock, after which it is sent to dry cooling unit 7 where the coke is dry cooled and releases its sensible heat to the circulating gas. The coke, cooled down to a temperature of ~ 200C, leaves the dry cooler through duct 12. The circulating gas enters dry cooler 7 via duct 8 and leaves it through duct 9, through which the hot gas 55~5 reaches unit 10 which is used for preheating the coal. The coking coal is introduced into the preheating unit via duct 11 and is filled into the coke oven chamber 2 via duct 3.
The circulatlng gas leaving the preheating unit 10, after having been freed as much as possible from dust carried along, for example in an electrostatic dust filter 13, is cooled in a gas cooler 14 to the desired final temperature of between 30 and 40C, for example, and is returned, through a pressure booster blower 15 and duct 8 to dry cooler 7.
The adjustment of the operating temperature of the preheating unit 10 is carried out in the following manner. A
specific volume of cooled gas is removed from ductl~, whichruns to filter 13 -through duct 17. This volume is fed into duct 9 by means of pressure booster blower 18. The portion of the gas leaving the dry cooler 7, and which is not required for heating the coking coal, is removed from duct 9 for producing steam in waste gas boiler 19, after which it is sent to duct 16 which runs to filter 13.
According to the invention, the heat carrier is a combustible gas flowing in a closed circuit. The circulating gas may be produced, when the installation is started up, by feeding air into dry cooler 7 through duct 21, shown in dotted line in the drawing of Figure 2. This air is used only for starting the operation and is deviated from air duct 20. The air reacts with the hot coke and burns or gasifies a small portion thereof. During this operation, the circulating gas is enriched with the products resulting from the burning up, gasification and after-degasification of coke.
The excess gas is removed from the circuit between pressure booster blower 15 and dry cooler 7, via duct 22 and is fed to s~
hot gas duct 6, i.e. it i5 mixed with the under-grate-firing gas fed to the coke ovens.
In order to keep constant the desired calorific value of the circulating gas, the value of which is preferably between 2900 and 6300 kJ/m3N, it is possible to mix nitrogen, cleaned flue gas and/or air selectively with the circulating gas. The addition of air, which is substantially less costly, also causes a reduction in the hydrogen content and a slight increase in heat potential. Air is added through duct 20 into duct 9, where it is fed into the hot gas behind the dry cooler. Flue gas or nitrogen is added to the cold circulating gas, through duct 23, between blower 15 and dry cooler 7. The operating pressure in the coke dry cooler is at a level of about 1~00 mm water, so that the circulating gas may pass, without any increase in pressure, through subsequent stages of the method, thereby avoidiny negative pressure at any point in the system.
In the case of known installations for cooling coke, operating in conjunction with a steam producing device, the cooling gas, after cooling in the steam boiler, is returned to - the cooling chamber at a temperature of about 150C. In order to cool the coke down to about 200C, a correspondingly large volume of cooling gas and a correspondingly large cooling chamber are needed. Since the latter is lined with refractory material, a considerable investment is required.
It is also known to preheat the coal used to produce the coke in the coke oven by means of flue gas or blast furnace gas as a carrier gas which has withdrawn the sensible heat from the coke in a coke dry cooling unit. The use of a blast furnace gas as a carrier gas is known from German Patent 27 33 365. According to this method, which is mainly suitable for steel plant coke ovens where blast furnace gas is available, the cooled gas is returned to the circuit after the coal has been heated.
In all circulating processes, the volume of circu-lating gas is increased by gasification (coke burn up) and subsequent coke degasification, and a certain amount of circulating gas must therefore be removed continuously~ In the method disclosed in British Patent 1,334,373, a flue gas is used as the carrier gas. Because of the residual oxygen content in all flue gases, the increase in gas and the loss of coke by burn up is greater than with combustible gases, and the volume of circulating gas to be carried away is also greater. This gas enriched with pollutants is released to the atmosphere, and thus requires expensive conditioning equipment, such as after burners, dust removers and possibly desul-phurizing e~uipment.
It is the aim of the present invention to provide conditions for the low cost implementation of a method for the dry cooling of coke in which the carrier gas flows in a closed circuit between the step of dry cooling of coke and that of preheating coke, any excess of circulating gas being discarded without causing pollution.
According to the invention, this aim is achieved by cooling down the circulating gas leaving the waste gas steam ~oiler, before said gas enters the coke cooling chamber, in a combined washer cooler, approximately to the cooling tempera-ture thus removing the dust from said circulating gas.
This rnakes it possible to reduce considerably the size of the coke cooling chamber. The circulating gas is not freed from dust as usual, by means of a dry separator, but with a co~bined wet washer cooler, where the said circulating gas is not only cleaned, but is cooled down to a temperature close to that of the coolant used. Since the circulating gas which is returned to the coke cooling chamber has, according to the invention, a substantially lower temperature, for example below 20C., the volume of circulating gas can be reduced considerably, and the coke cooling chamber itself may also be considerably smaller. Because of the smaller volume of circulating gas, a smaller blower using less power may be ~Z~5~5 used. The arrangement according to the invention therefore results in a considerable reduction of the investment and of the operating costs.
Moreover, by using an additional cooling unit, or a heat pump like unit, it is possible to provide additional cooling for the circulating gas leaving the washer cooler, before said gas enters the coke cooling chamber. This again reduces the volume of circulating gas and, at the same time, allows part of the water vapour to be removed from the circu-lating gas by condensation~ The resulting nearly dry gasbehaves like the circulating gas which is used in a normal dry coke cooling process and eliminates additional coke burn onO This allows the method according to the invention to be still more economical.
In accordance with a preferred ernbodiment of the invention, the clrculating gas between the coke dry cooler and the coal preheater is a combustible gas. The calorific value of the cornbustible gas is adjusted by feeding nitrogen or clean flue gas into the cold circulating gas ahead of the coke dry cooler, and/or by feeding air into the hot circulating gas after the coke dry cooler. Any excess cold circulating gas is withdrawn from the circuit ahead of the coke dry cooler and is mixed with the under-grate-firing gas to be fed to the coke ovens.
In accordance with another ernbodiment of the invention, the excess hot circulating gas, i.e. part of the circulating gas not needed to preheat the coal, is withdrawn between the coke cooling chamber and the preheating unit, after which it is passed through a waste heat boiler, and is mixed with the gas leaving the said preheating unit.
55~5 ~ccording to a preferred embodiment of the invention, part of the cooled down gas emerging from the preheating unit is withdrawn so as to adjust the operating temperature and is fed into the duct running from the coke cooling chamber to the said preheating unit~
The method according to the invention is particularly suitable for colliery coking plants and produces extremely little pollution, since the excess ~as can be mixed with the under-grate-firing gas for the coke-ovens, thus eliminating the conditioning of the equipment.
The invention will now be illustrated by means of the annexed drawings, in which:
FIGURE 1 is a diagram illustrating the method of cooling coke according to the invention, and FIGURE 2 is a diagram which illustrates another embodiment of the method according to the invention.
With reference to Figure 1 of the drawings, it will be seen that the hot circulating gas leaves the coke cooling chamber 101 at 103 and is sent to the waste heat steam boiler 105 via duct 107. The circulating gas leaves the waste heat steam boiler 105 at 109 and is thereafter sent to the combined washer cooler 111 by circulating through duct 113, which is at a temperature between 180 and 200C. It will be noted that a coolant, for example water, is introduced into the combined washer cooler 111 by means of a duct 115 from which it is sprayed into the combined washer cooler 111 by means of the spraying device 117. The hot circulating gas is passed through the combined washer cooler 111 via duct 119 and it leaves at 121.
This, in effect, removes the dust from the ~ Z~5~i9~
circulating gas and cools it to approximately the temperature of the coolant, for example about 20C. The thus cooled circulating gas is sent via duct 123, to a cooling unit 125 which operates in the same manner as, for example, a heat pump, where it is cooled down still further. The circulating gas, thus cooled down to this extent, is returned to the coke cooling chamber via duct 127, after which it is picked up by a blower 129 from which it is sent to the coke cooling chamber . 101, via duct 131.
Figure 2 illustrates another embodiment of the method according to the invention. According to this embodiment, there is provided a coke oven 1 inside of which there is a chamber 2 which is filled with preheated coal, the latter being introduced from above, through a system of ducts 3, by means of filling holes, not shown which can be closed off.
Fuel gas and combustion air are fed through ducts 5 and 6 and pass, through regenerators 4, into the flues (not shown) surrounding the oven chamber. The gases which are formed during the dry distillation are removed through riser pipes, not shown, from which they are sent into a receiver (also not shown).
The hot coke which is forced out of the coke oven at about 1000C, is removed in batches, by means of a bucket, through a pressure tight lock, after which it is sent to dry cooling unit 7 where the coke is dry cooled and releases its sensible heat to the circulating gas. The coke, cooled down to a temperature of ~ 200C, leaves the dry cooler through duct 12. The circulating gas enters dry cooler 7 via duct 8 and leaves it through duct 9, through which the hot gas 55~5 reaches unit 10 which is used for preheating the coal. The coking coal is introduced into the preheating unit via duct 11 and is filled into the coke oven chamber 2 via duct 3.
The circulatlng gas leaving the preheating unit 10, after having been freed as much as possible from dust carried along, for example in an electrostatic dust filter 13, is cooled in a gas cooler 14 to the desired final temperature of between 30 and 40C, for example, and is returned, through a pressure booster blower 15 and duct 8 to dry cooler 7.
The adjustment of the operating temperature of the preheating unit 10 is carried out in the following manner. A
specific volume of cooled gas is removed from ductl~, whichruns to filter 13 -through duct 17. This volume is fed into duct 9 by means of pressure booster blower 18. The portion of the gas leaving the dry cooler 7, and which is not required for heating the coking coal, is removed from duct 9 for producing steam in waste gas boiler 19, after which it is sent to duct 16 which runs to filter 13.
According to the invention, the heat carrier is a combustible gas flowing in a closed circuit. The circulating gas may be produced, when the installation is started up, by feeding air into dry cooler 7 through duct 21, shown in dotted line in the drawing of Figure 2. This air is used only for starting the operation and is deviated from air duct 20. The air reacts with the hot coke and burns or gasifies a small portion thereof. During this operation, the circulating gas is enriched with the products resulting from the burning up, gasification and after-degasification of coke.
The excess gas is removed from the circuit between pressure booster blower 15 and dry cooler 7, via duct 22 and is fed to s~
hot gas duct 6, i.e. it i5 mixed with the under-grate-firing gas fed to the coke ovens.
In order to keep constant the desired calorific value of the circulating gas, the value of which is preferably between 2900 and 6300 kJ/m3N, it is possible to mix nitrogen, cleaned flue gas and/or air selectively with the circulating gas. The addition of air, which is substantially less costly, also causes a reduction in the hydrogen content and a slight increase in heat potential. Air is added through duct 20 into duct 9, where it is fed into the hot gas behind the dry cooler. Flue gas or nitrogen is added to the cold circulating gas, through duct 23, between blower 15 and dry cooler 7. The operating pressure in the coke dry cooler is at a level of about 1~00 mm water, so that the circulating gas may pass, without any increase in pressure, through subsequent stages of the method, thereby avoidiny negative pressure at any point in the system.
Claims (5)
1. A method for utilizing the sensible heat which is formed during the dry cooling of coke by means of a gas, in which, for preheating the coal used in producing the coke, a circulating gas is passed through a waste heat boiler or the like heat-consuming unit and, after being freed from dust, is then returned to the coke cooling chamber, any excess gas being removed from the circuit, characterized in that the circulating gas leaving the waste gas boiler is cooled down in a combined washer-cooler, before entering the coke cooling chamber, approximately to coolant temperature, thereby removing dust therefrom.
2. A method according to claim 1, characterized in that before entering the coke cooling chamber, the circulating gas leaving the washer-cooler is passed, through a cooling unit or a heat-exchanger.
3. A method according to claim 1, characterized in that between the coke dry cooler and the coal preheater the circulating gas consists of a combustible gas, the desired calorific heat value thereof being adjusted by feeding nitrogen or cleaned flue gas into the cold circulating gas ahead of the coke dry cooler and/or by feeding air into the hot circulating gas after the coke dry cooler, and in that excess cold circulating gas is withdrawn from the circuit ahead of the coke dry cooler and is mixed with under-grate-firing gas fed to coke ovens.
4. A method according to claim 1, characterized in that excess hot circulating gas is withdrawn between the coke cooling chamber and the preheating unit, to be passed through a waste gas steam boiler, after which said circulating gas is mixed with the gas leaving the said preheating unit.
5. A method according to claims 1, 3 or 4, characterized in that part of cooled gas emerging from the preheating unit is withdrawn for adjusting operating tempera-ture and is fed into a duct running from the coke cooling chamber to the preheating unit.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3404684A DE3404684C2 (en) | 1984-02-10 | 1984-02-10 | Process for utilizing the sensible heat generated when coke is dry-cooled by means of a gas |
| DEDE-P3404684 | 1984-02-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1245595A true CA1245595A (en) | 1988-11-29 |
Family
ID=6227296
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000471353A Expired CA1245595A (en) | 1984-02-10 | 1985-01-02 | Method for dry cooling coke using the sensible heat formed during dry cooling |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0151727A3 (en) |
| JP (1) | JPS60188489A (en) |
| CA (1) | CA1245595A (en) |
| DE (1) | DE3404684C2 (en) |
| ES (1) | ES8605019A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106479542A (en) * | 2016-10-27 | 2017-03-08 | 武汉钢铁股份有限公司 | Water gas preparation technology based on CDQ and coking coal dehumidifying |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT387785B (en) * | 1986-06-30 | 1989-03-10 | Waagner Biro Ag | METHOD AND DEVICE FOR COOLING SHEET GOODS BY MEANS OF A GAS CIRCUIT |
| CN106590700B (en) * | 2016-10-27 | 2019-07-16 | 武汉钢铁有限公司 | A kind of dry coke quenching unit residual heat and energy utilization system |
| CN109027989B (en) * | 2018-08-01 | 2020-06-16 | 青岛京润石化设计研究院有限公司 | Method for utilizing residual heat of coal coke powder of fluidized bed |
| CN110108033A (en) * | 2019-03-12 | 2019-08-09 | 北京北燃供热有限公司 | It is a kind of for heating medium-sized gas fired-boiler flue gas waste heat recovery apparatus |
| CN109810717A (en) * | 2019-03-22 | 2019-05-28 | 唐山中润煤化工有限公司 | A kind of method reducing dry coke quenching coke burning and the device for preparing dry coke quenching |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE435572C (en) * | 1923-01-18 | 1928-06-06 | Bamag Meguin Akt Ges | Dry cooling of coke |
| US3888742A (en) * | 1974-01-23 | 1975-06-10 | Waagner Biro American | Pollution-free coal-preheating with waste heat from dry coke-quenching |
| FR2265840B3 (en) * | 1974-04-01 | 1977-12-02 | Buettner Schilde Haas Ag | |
| 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 |
| DE2733365C3 (en) * | 1977-07-23 | 1980-06-19 | Didier Engineering Gmbh, 4300 Essen | Process for using the sensible heat of coke in a coking plant |
| DE3123141A1 (en) * | 1981-06-11 | 1982-12-30 | Krupp-Koppers Gmbh, 4300 Essen | METHOD AND DEVICE FOR OPERATING A COOKING PLANT |
| DE3216898C1 (en) * | 1982-05-06 | 1983-10-06 | Didier Eng | Process for utilising the sensible coke heat in dry coke cooling |
-
1984
- 1984-02-10 DE DE3404684A patent/DE3404684C2/en not_active Expired
- 1984-12-07 EP EP84114895A patent/EP0151727A3/en not_active Withdrawn
-
1985
- 1985-01-02 CA CA000471353A patent/CA1245595A/en not_active Expired
- 1985-02-07 JP JP60021036A patent/JPS60188489A/en active Pending
- 1985-02-08 ES ES540238A patent/ES8605019A1/en not_active Expired
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106479542A (en) * | 2016-10-27 | 2017-03-08 | 武汉钢铁股份有限公司 | Water gas preparation technology based on CDQ and coking coal dehumidifying |
| CN106479542B (en) * | 2016-10-27 | 2019-08-20 | 武汉钢铁有限公司 | The water-gas preparation process to be dehumidified based on Dry Quenching and coking coal |
Also Published As
| Publication number | Publication date |
|---|---|
| ES8605019A1 (en) | 1986-03-16 |
| EP0151727A3 (en) | 1987-01-14 |
| JPS60188489A (en) | 1985-09-25 |
| DE3404684A1 (en) | 1985-08-22 |
| EP0151727A2 (en) | 1985-08-21 |
| DE3404684C2 (en) | 1986-01-23 |
| ES540238A0 (en) | 1986-03-16 |
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