CN104073268A - Coking-preventing raw coke oven gas waste heat recycling device for heat-conduction oil coke oven - Google Patents
Coking-preventing raw coke oven gas waste heat recycling device for heat-conduction oil coke oven Download PDFInfo
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- CN104073268A CN104073268A CN201410329566.9A CN201410329566A CN104073268A CN 104073268 A CN104073268 A CN 104073268A CN 201410329566 A CN201410329566 A CN 201410329566A CN 104073268 A CN104073268 A CN 104073268A
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention relates to a coking-preventing raw coke oven gas waste heat recycling device for a heat-conduction oil coke oven. The upper end of a top axle tube is connected with a top ascending tube; the lower end of a bottom axle tube is connected with a gas collecting tube; a heat exchanger is connected between the lower end of the top axle tube and the upper end of the bottom axle tube; a temperature of the heat-conduction oil in the heat exchanger can reach 320-350 DEG C; and the heat exchanger is connected with a heat-conduction oil system. According to the invention, the raw coke oven gas waste heat recycling device is distributed on the axle tubes, so that a coking problem in the raw coke gas waste heat recycling device is effectively prevented. A heat transfer medium of the waste heat recycling device adopts heat conduction oil with a higher boiling point, liquid-phase operation heat transfer efficiency for the heat-conduction oil is high, a low-pressure operation system is safe and stable; heated high-temperature heat-conduction oil can be used for directly supplying heat for a plurality of processes for coking production, and therefore, the raw coke oven gas waste heat can be sufficiently applied. A tube shell type heat-conduction oil heat exchanger structure is adopted, so that the device has the characteristics of being high in heat transfer efficiency, low in pressure and high in safety for a heat conduction oil liquid-phase operation system, convenient for recycling heat due to a high heat-transferred heating medium temperature, and the like.
Description
Technical field
The present invention relates to a kind of residual heat using device, be specifically related to a kind of raw gas heat recovery device.
Background technology
Along with social development, Fossil fuel consumption amount rapidly increases, and power supply situation is more and more nervous, the energy-conservation current development trend that become.Coking industry is big power consumer always, if do not taken appropriate measures, calorific losss a large amount of in production will cause huge energy wastage.In recent years, coking industry is updated operating procedure and is produced power consumption to reduce, and is not effectively utilized but account for so far the more than 30% raw gas waste heat of coking quantity of heat given up always.
For come out of the stove red Jiao's UTILIZATION OF VESIDUAL HEAT IN of coking plant, adopt at present Dry Quenching Technology to obtain first-stage success, but the universal scope of Dry Quenching Technology is also less; The waste heat of flue raw gas is used for by some enterprises the damping of coalingging at present, dry coking coal.For the huge crude-gas sensible heat of heat ratio, its UTILIZATION OF VESIDUAL HEAT IN is studied and engineering test both at home and abroad always, but bad because of engineering practice effect, not yet there are at present relevant waste heat recovery and use device to get the nod and widespread use.
For utilizing the waste heat of raw gas, people successively adopt water cold sleeve are installed in upcast, heat conductive oil bushing, the heat reclamation devices such as heat pipe and employing recovery of heat coking, the processing methodes such as preparing synthetic gas.But because technology is immature, the above-mentioned technique of each side reason such as security is not high, and coking phenomenon is serious, and economic benefit is low and method all do not obtain the extensive promotion and application in engineering.And traditional waste-heat recovery device is usually placed on coke oven coke oven uprising tube (comprising bottom upcast and top upcast two portions), raw gas easily in upcast exit condensation following current to upcast bottom, the radiative transfer of last tar top layer coal seam and coke in upcast bottom is subject to carbonizing chamber and polycondensation coking occurs react, and form a circle graphite settling, affect heat exchange, when serious, usually cause upcast to stop up, raw gas cannot be discharged.
Under the severe situation of current energy-conserving and environment-protective, summing up experience, breaks through thinking, the achievement of employing new technology, and a set of rational raw gas waste-heat recovery device meaning of research and design is huge.
Summary of the invention
It is low that the present invention is mainly used for solving the utilization rate of waste heat existing in raw gas waste heat recovery, waste-heat recovery device calculus China ink phenomenon is serious, safety in operation is not high, and the waste heat of recovery is not easy to the problems such as application, and a kind of thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking is provided.
For realizing above-mentioned object, technical scheme of the present invention is: a kind of thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking, comprise interchanger, top bridge tube, bottom bridge tube, bridge tube upper end, top is connected with top upcast, bridge tube lower end, bottom is connected with effuser, be characterized in: between bridge tube lower end, top and bridge tube upper end, bottom, be connected interchanger, it is 320-350 DEG C that the thermal oil in interchanger can reach temperature, and interchanger is connected with heat-conducting oil system.
Interchanger comprises interchanger top flange, interchanger flange in the bottom, thermal oil entrance, thermofin, thermal oil outlet, interchanger dividing plate, heat exchanger tube; Interchanger top is connected with top bridge tube by interchanger top flange, interchanger bottom is connected with bottom bridge tube by interchanger flange in the bottom, thermofin is arranged in below interchanger top flange, heat exchanger tube is arranged in the middle of interchanger, thermal oil outlet is arranged in interchanger top-side, thermal oil entrance is arranged in interchanger bottom sides, and interchanger dividing plate separates heat exchanger shell pass, and heat exchanger tube is arranged in the middle of interchanger.
Ammonia spray nozzle is arranged on bridge tube right side, bottom, turnover panel is arranged in bridge tube bottom, bottom, between bottom bridge tube and top upcast, be connected with bypass pipe, bypass pipe top is connected with bridge tube side, top, bypass pipe bottom is connected with bridge tube side, bottom, bypass pipe top layout bypass pipe top valve, bypass pipe top valve hypomere is arranged bypass pipe flange, bypass pipe bottom valve is arranged in bypass pipe bottom.
Heat-conducting oil system comprises heating plant, strainer, pump; Heating plant one side is connected with thermal oil outlet, and heating plant opposite side is connected with strainer one side, and strainer opposite side is connected with pump intake, and pump discharge is connected with thermal oil entrance.The curved outside of top bridge tube is provided with clean-out opening.
Compared with prior art, technique effect of the present invention is:
(1) waste-heat recovery device interchanger is arranged on bridge tube, avoid the thermal radiation of carbonizing chamber top layer coke heat exchanger bottom, thereby effectively avoid interchanger calculus China ink problem, solved a major issue that hinders the safe operation of raw gas waste-heat recovery device.
(2) make full use of raw gas waste heat, the present invention can be down to raw gas temperature below 350 DEG C from approximately 650 DEG C.Current raw gas waste-heat recovery device is cooled to raw gas temperature more than 450-500 DEG C from 650-700 DEG C conventionally, because this waste-heat recovery device can be avoided exchanger tube wall and occurs calculus China ink phenomenon, therefore raw gas temperature can be reduced to lower level, realize the high efficiente callback utilization to raw gas waste heat.
(3) this waste-heat recovery device adopts thermal oil as heat-transfer medium, and because thermal oil boiling point is higher, maximum operating temperature can reach 320-350 DEG C, and in this device, in liquid phase operation, heat transfer efficiency is high, and system the feature such as stablizes in low pressure operation status safety.In addition, thermal oil can be up to 250-300 DEG C through this waste-heat recovery device temperature after heating, and temperature and heat transfer efficiency all higher higher-grade thermal oil thermal source can be directly used in the coal damping of coke-oven plant, ammonia still process, and crude benzene refining, in coke dry quenching boiler feed-water preheating.
Be usually placed on coke oven coke oven uprising tube for traditional raw gas waste-heat recovery device, its interchanger inwall easily forms coking material affects the defect of heat exchange, the present invention is arranged in raw gas waste-heat recovery device on bridge tube, has effectively prevented the coking problem in raw gas waste-heat recovery device.The heat-transfer medium of waste-heat recovery device adopts the higher thermal oil of boiling point, thermal oil liquid phase operation heat transfer efficiency is high, low pressure operation security of system is stable, and high temperature heat conductive oil after heating can directly carry out heat supply for many techniques of coking production, and therefore raw gas waste heat can fully be applied.In addition, also designed clean-out opening, the device such as bypass pipe ensures the safe and reliable operation of this waste-heat recovery device.
Brief description of the drawings
Fig. 1 is the system schematic of retrieving arrangement of the present invention;
Fig. 2 is heat exchanger structure schematic diagram of the present invention;
Fig. 3 is the vertical view of Fig. 2.
Embodiment
Below in conjunction with the drawings and specific embodiments, the invention will be further described.
As shown in Figure 1 to Figure 3, a kind of thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking, comprise carbonizing chamber 1, bottom upcast 2, turnover panel 3, refractory brick 4, bypass pipe bottom valve 5, interchanger flange in the bottom 6, bypass pipe 7, upcast flange 8, top upcast 9, bypass pipe flange 10, bypass pipe top valve 11, manhole cover 12, top bridge tube valve 13, top bridge tube 14, clean-out opening 15, interchanger top flange 16, heating plant 17, interchanger 18, ammonia spray nozzle 19, pump 20, strainer 21, bottom bridge tube 22, effuser 23, effuser support and coke oven body 24, thermal oil entrance 25, thermofin 26, thermal oil outlet 27, interchanger dividing plate 28, heat exchanger tube 29.
The annexation of above-mentioned parts is as follows:
Bottom upcast 2 is placed on carbonizing chamber 1, and upcast 2 inwalls in bottom are arranged refractory brick 4; Top upcast 9 is connected with bottom upcast 2 by upcast flange 8, and manhole cover 12 is placed in above top upcast 9; Bridge tube 14 right sides in top are connected with top upcast 9 sides, and bridge tube 14 bottoms in top are connected with the interchanger top flange 16 on interchanger 18, are successively furnished with from the inlet to the outlet top bridge tube valve 13 and clean-out opening 15 on top bridge tube 14; Interchanger 18 tops are connected with top bridge tube 14 by interchanger top flange 16, interchanger 18 bottoms are connected with bottom bridge tube 22 by interchanger flange in the bottom 6, thermofin 26 is arranged in below interchanger top flange 16, heat exchanger tube 29 is arranged in the middle of interchanger 18, thermal oil outlet 27 is arranged in interchanger 18 top-side, thermal oil entrance 25 is arranged in interchanger 18 bottom sides, and interchanger dividing plate 28 separates interchanger 18 shell sides, and heat exchanger tube 29 is arranged in the middle of interchanger 18; Bridge tube 22 tops, bottom are connected with the interchanger flange in the bottom 6 on interchanger 18, and ammonia spray nozzle 19 is arranged on bridge tube 22 right sides in bottom, and turnover panel 3 is arranged in bridge tube 22 bottoms in bottom; Effuser 23 is connected with bottom bridge tube 22 bottoms, and effuser 23 is arranged on effuser support and coke oven body 24; Bypass pipe 7 tops are connected with top bridge tube 14 sides, bypass pipe 7 bottoms are connected with bottom bridge tube 22 sides, bypass pipe 7 top layout bypass pipe top valves 11, valve 11 hypomeres in bypass pipe top are arranged bypass pipe flange 10, bypass pipe bottom valve 5 is arranged in bypass pipe 7 bottoms; Heating plant 17 1 sides are connected with thermal oil outlet 27, and heating plant 17 opposite sides are connected with strainer 21 1 sides, and strainer 21 opposite sides are connected with pump 20 entrances, and pump 20 exports with thermal oil entrance 25 and is connected.
Clean-out opening 15 is arranged in top bridge tube 14 curved outside, while occurring stopping up, cleans by the interior heat exchanger tube 29 of clean-out opening 15 heat exchanger 18 in interchanger 18; Described ammonia spray nozzle 19 is arranged in bridge tube 22 tops, bottom, and until raw gas, after interchanger 18 coolings, ammonia spray nozzle 19 is to the further cooling down of raw gas.Top bridge tube 14 and bottom bridge tube 22 diameters and top upcast 9 diameters approach, and clean-out opening 15 sizes are advisable can see all heat exchanger tube 29 at vertical position.
Bypass pipe 7 tops are connected with top bridge tube 14 sides on bridge tube valve 13 right sides, top; bypass pipe 7 bottoms are connected with bottom bridge tube 22 right sides; in the time there is serious obstruction in interchanger 18; open bypass pipe top valve 11 and bypass pipe bottom valve 5; and close top bridge tube valve 13; make raw gas enter bottom bridge tube 22 through bypass pipe 7, normally circulate to realize raw gas, and protect interchanger 18.Bypass pipe 7 diameters are about 1/3 of top bridge tube 14 diameters, to save initial cost.
Interchanger 18 is tube shell type structure, shell side circulation thermal oil, tube side circulation raw gas; Interchanger dividing plate 28 of interchanger 18 intermediate arrangement, thermal oil enters interchanger 18 from thermal oil entrance 25, exports 27 outflow heat exchangers 18 from thermal oil; Interchanger dividing plate 28 is arranged in interchanger 18 shell sides, to increase the mobile disturbance of thermal oil, improves its heat-transfer effect; Described interchanger 18 interior conduits are arranged to the heat exchanger tube 29 of similar 3 × 3 tube bank form, to improve the compactedness of interchanger; The thermofin 26 of the thick silica wool composition of the interchanger about 30mm of 18 top layout one deck, to prevent that raw gas is not before entering heat exchanger tube 29, thereby interchanger 18 top planes be cooled separate out tar cause heat exchanger tube 29 entrances stop up; Described interchanger 18 tops and bottom are separately installed with interchanger top flange 16 and interchanger flange in the bottom 6; In the time that interchanger 18 breaks down, turn on interchanger top flange 16 and interchanger flange in the bottom 6 bolts, unscrew bypass pipe flange 10, safeguard and change with heat exchanger 18; Interchanger 18 external diameters are equal to or greater than top bridge tube 14 diameters, in the situation that not affecting the normal work of other equipment of coke-oven plant, strengthen as far as possible interchanger 18 external diameters, to improve its heat interchanging area, increase heat, the about 1.2-2 rice of interchanger height; Raw gas enter interchanger 18 before temperature be about 650 DEG C, after interchanger 18 heat exchange, raw gas temperature can be down to below 300-350 DEG C, thermal oil enter interchanger 18 before temperature lower more than 50 DEG C in interchanger 18 exit temperature than raw gas, thermal oil go out from interchanger 18 before temperature can be up to 200-330 DEG C.
Heat-transfer medium in heat-conducting oil system is synthetic class thermal oil, is liquid phase operation, and its maximum operation (service) temperature can reach about 320-350 DEG C; Heat-conducting oil system can be drawn the high temperature heat conductive oil of heating in interchanger 18 from thermal oil outlet 27, by heating plant 17 by the thermal oil being heated by raw gas for coke-oven plant or other industry, life heat source, final thermal oil is by strainer 21, and pump 20 is back to thermal oil entrance 25; A coke oven comprises many carbonizing chambers 1 conventionally, and therefore the thermal oil of the waste-heat recovery device on all carbonizing chambers 1 should be pooled to same large heat-conducting oil system, with cost-saving.
All fixing part outer walls of raw coke oven gas pipeline system, bypass pipe 7, interchanger 18, heat-conducting oil heating system are all laid one layer of heat preservation silica wool or perlite, improve utilization rate of waste heat, and improve coke oven top work operating environment to reduce raw gas heat radiation.
Know-why of the present invention is: find that after deliberation the tar in raw gas starts to separate out in a large number when lower than 350 DEG C, and when the tar of separating out in temperature during higher than 380-410 DEG C tar just there is polycondensation coking reaction and form graphite.Traditional waste-heat recovery device is usually placed on coke oven coke oven uprising tube (comprising bottom upcast 2 and top upcast 9 two portions), raw gas easily in upcast exit condensation following current to upcast bottom, last tar is subject to the radiative transfer in top layer coal seam and coke in carbonizing chamber 1 and polycondensation coking occurs reacts in upcast bottom, and form a circle graphite settling, affect heat exchange, when serious, usually cause upcast to stop up, raw gas cannot be discharged.The present invention proposes waste-heat recovery device to be arranged in (in the middle of top bridge tube 14 and bottom bridge tube 22) on bridge tube, calculate and find by analysis, only can there is condensation in raw gas, and the tar of condensation meeting following current is to the lower bottom bridge tube 22 of temperature, tar can not form the settlings such as graphite in exchanger tube wall, therefore can effectively avoid waste-heat recovery device generation calculus China ink phenomenon.The heat catalysis that this waste-heat recovery device adopts, for synthetic class thermal oil, is in a liquid state under this material normal temperature, and boiling point is very high, and maximum operation (service) temperature can reach 320-350 DEG C, is therefore in operation all the time in liquid phase state, and heat transfer efficiency is high; In addition, because heating agent moves in liquid phase, therefore the pressure rating of heat exchanger and residual neat recovering system is less demanding, and security of system hidden danger is less, and property safe and reliable to operation is high.
When raw gas enters bottom upcast 2 from carbonizing chamber of coke oven 1, temperature is generally 650-750 DEG C, through bottom upcast 2, top upcast 9, after top bridge tube 14, before entering interchanger 18, temperature is about 650 DEG C, raw gas is cooled to the 300-350 DEG C of following rear bottom bridge tube 22 that flows in interchanger 18, in bottom bridge tube 22, be cooled to 75-85 DEG C of left and right by the ammoniacal liquor spraying in ammonia spray nozzle 19, enter subsequently in the processing units such as primary cooler in effuser 23 and coke-oven plant thereof.Thermal oil temperature before entering interchanger 18 from thermal oil entrance 25 is lower more than 50 DEG C in interchanger 18 temperature outs than raw gas, after being warming up to 200-330 DEG C after interchanger 18 heat exchange, thermal oil flows out from thermal oil outlet 27, enter subsequently heating plant 17, strainer 21 and pump 20.
Application the present invention recycle raw gas waste heat, comprises the following steps:
before coke oven does not start coking, check whether each pipeline has fault, in each pipeline and system under normal circumstances, open the switch of heating plant 17 and strainer 21, connect pump 20 power supplys, operation heat-conducting oil system.
open top bridge tube valve 13, close bypass pipe top valve 11 and bypass pipe bottom valve 5, close clean-out opening 15, close manhole cover 12, in the time that other preparation work of coking by coke oven is all ready to, open ammonia spray nozzle 19, start coking by coke oven.
in the time that coke oven need to be shut down or occur on a large scale fault for a long time, after coke oven is shut down for some time (no longer producing raw gas), close ammonia spray nozzle 19, close the pump 20 of heat-conducting oil system, heating plant 17, strainer 21.In the time that coke oven starts use again, repetitive process
,
,
.
in the time that the heat exchanger tube 29 in interchanger 18 is in operation appearance obstruction, can opens clean-out opening 15 heat exchanger pipelines 29 and clean; When heat exchanger tube 29 is stopped up when more serious; open bypass pipe top valve 11 and bypass pipe bottom valve 5, close top bridge tube valve 13, make raw gas from bypass pipe 7, flow into bottom bridge tube 22; and strengthen the unlatching amplitude of ammonia spray nozzle 19, to protect interchanger 18.
Through this raw gas waste-heat recovery device analytical calculation and numerical evaluation are shown, this device exchanger tube wall that is in operation there will not be calculus China ink phenomenon, and this device to the utilization ratio of raw gas waste heat up to more than 29%, this is high more than traditional raw gas waste-heat recovery device utilization rate of waste heat, in addition, adopt this device also can reduce the sprinkling of coke oven ammoniacal liquor and measure approximately 36%, the primary cooler circulating cooling water yield approximately 33%.Thermal oil calorific value total amount after this waste-heat recovery device heating is huge, and temperature is up to 200-330 DEG C, and heat-conducting oil efficiency is high in addition, therefore this heat can be directly used in the coal damping in coke-oven plant, ammonia still process, crude benzene refining, in the techniques such as coke dry quenching boiler feed-water preheating.The present invention changes less to traditional coke oven, only upcast height is improved to 1.2-2 rice this device can be installed, less on the production technique of traditional coke oven and design impact, is convenient to transformation and promotes.In sum, this raw gas waste-heat recovery device has operation and does not occur calculus China ink phenomenon, and utilization rate of waste heat is high, low pressure operation is safe and reliable, the waste heat utilizing is applied conveniently again, and the features such as transformation and simple installation, are the good coking industry energy-efficient equipments of a kind of promotion prospect.
Claims (5)
1. one kind prevents the thermal oil waste heat of coke oven crude gas retrieving arrangement of coking, comprise interchanger (18), top bridge tube (14), bottom bridge tube (22), top bridge tube (14) upper end is connected with top upcast (9), bridge tube (22) lower end, bottom is connected with effuser (23), it is characterized in that: between bridge tube (14) lower end, described top and bottom bridge tube (22) upper end, be connected interchanger (18), it is 320-350 DEG C that thermal oil in described interchanger (18) can reach temperature, and described interchanger (18) is connected with heat-conducting oil system.
2. the thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking according to claim 1, is characterized in that: described interchanger (18) comprises interchanger top flange (16), interchanger flange in the bottom (6), thermal oil entrance (25), thermofin (26), thermal oil outlet (27), interchanger dividing plate (28), heat exchanger tube (29), described interchanger (18) top is connected with top bridge tube (14) by interchanger top flange (16), interchanger (18) bottom is connected with bottom bridge tube (22) by interchanger flange in the bottom (6), thermofin (26) is arranged in interchanger top flange (16) below, heat exchanger tube (29) is arranged in the middle of interchanger (18), thermal oil outlet (27) is arranged in interchanger (18) top-side, thermal oil entrance (25) is arranged in interchanger (18) bottom sides, interchanger dividing plate (28) separates interchanger (18) shell side, heat exchanger tube (29) is arranged in the middle of interchanger (18).
3. the thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking according to claim 1, it is characterized in that: ammonia spray nozzle (19) is arranged on described bottom bridge tube (22) right side, turnover panel (3) is arranged in bottom bridge tube (22) bottom, between bottom bridge tube (22) and top upcast (9), be connected with bypass pipe (7), described bypass pipe (7) top is connected with top bridge tube (14) side, bypass pipe (7) bottom is connected with bottom bridge tube (22) side, bypass pipe (7) top layout bypass pipe top valve (11), bypass pipe top valve (11) hypomere is arranged bypass pipe flange (10), bypass pipe bottom valve (5) is arranged in bypass pipe (7) bottom.
4. the thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking according to claim 1, is characterized in that: described heat-conducting oil system comprises heating plant (17), strainer (21), pump (20); Described heating plant (17) one sides are connected with thermal oil outlet (27), heating plant (17) opposite side is connected with strainer (21) one sides, strainer (21) opposite side is connected with pump (20) entrance, and pump (20) outlet is connected with thermal oil entrance (25).
5. the thermal oil waste heat of coke oven crude gas retrieving arrangement that prevents coking according to claim 1, is characterized in that: the curved outside of described top bridge tube (14) is provided with clean-out opening (15).
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| CN201410329566.9A CN104073268A (en) | 2014-07-11 | 2014-07-11 | Coking-preventing raw coke oven gas waste heat recycling device for heat-conduction oil coke oven |
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| CN201410329566.9A CN104073268A (en) | 2014-07-11 | 2014-07-11 | Coking-preventing raw coke oven gas waste heat recycling device for heat-conduction oil coke oven |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110452714A (en) * | 2019-08-17 | 2019-11-15 | 河北科技大学 | A kind of coal oven dithio-gas high temperature withdrawing device and method |
| CN111351378A (en) * | 2018-12-21 | 2020-06-30 | 赛峰航空助推器股份有限公司 | Fuel oil heat exchanger |
| CN116608701A (en) * | 2023-05-19 | 2023-08-18 | 江苏东九重工股份有限公司 | Sensible heat waste heat recovery device and method for molten calcium carbide |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111351378A (en) * | 2018-12-21 | 2020-06-30 | 赛峰航空助推器股份有限公司 | Fuel oil heat exchanger |
| CN110452714A (en) * | 2019-08-17 | 2019-11-15 | 河北科技大学 | A kind of coal oven dithio-gas high temperature withdrawing device and method |
| CN116608701A (en) * | 2023-05-19 | 2023-08-18 | 江苏东九重工股份有限公司 | Sensible heat waste heat recovery device and method for molten calcium carbide |
| CN116608701B (en) * | 2023-05-19 | 2023-12-01 | 江苏东九重工股份有限公司 | Sensible heat waste heat recovery device and method for molten calcium carbide |
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Application publication date: 20141001 |