WO2014161396A1 - 一种热油与水蒸气联产的循环床有机载热体炉 - Google Patents

一种热油与水蒸气联产的循环床有机载热体炉 Download PDF

Info

Publication number
WO2014161396A1
WO2014161396A1 PCT/CN2014/072384 CN2014072384W WO2014161396A1 WO 2014161396 A1 WO2014161396 A1 WO 2014161396A1 CN 2014072384 W CN2014072384 W CN 2014072384W WO 2014161396 A1 WO2014161396 A1 WO 2014161396A1
Authority
WO
WIPO (PCT)
Prior art keywords
heating surface
heat transfer
heat
steam
transfer oil
Prior art date
Application number
PCT/CN2014/072384
Other languages
English (en)
French (fr)
Inventor
张衍国
王友才
李清海
Original Assignee
清华大学
北京一亚高科能源科技有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 清华大学, 北京一亚高科能源科技有限公司 filed Critical 清华大学
Publication of WO2014161396A1 publication Critical patent/WO2014161396A1/zh

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/22—Fuel feeders specially adapted for fluidised bed combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B33/00—Steam-generation plants, e.g. comprising steam boilers of different types in mutual association
    • F22B33/02—Combinations of boilers having a single combustion apparatus in common
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
    • F24H1/00—Water heaters, e.g. boilers, continuous-flow heaters or water-storage heaters
    • F24H1/10—Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium
    • F24H1/12—Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium
    • F24H1/14—Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium by tubes, e.g. bent in serpentine form
    • F24H1/16—Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium by tubes, e.g. bent in serpentine form helically or spirally coiled
    • F24H1/167—Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium by tubes, e.g. bent in serpentine form helically or spirally coiled using solid fuel

Definitions

  • the invention relates to a heat exchange system for co-production of hot oil and steam, and is a circulating fluidized bed combustion heat-conducting oil furnace, which belongs to the field of improvement of energy utilization equipment and methods.
  • the principle of the heat transfer oil furnace is to heat the organic carrier (heat transfer oil), and carry out the liquid phase circulation through the high temperature oil pump to transport the heated heat transfer oil to the heat equipment, and then return to the heat transfer oil furnace by using the heat outlet of the heat device. Form a complete thermal cycle system.
  • coal-fired heat-conducting oil furnaces are mostly layer furnaces or pulverized coal furnaces.
  • the efficiency of layer furnaces is relatively low, and the adaptability of coal types is poor.
  • the fuel coal powder required for the pulverized coal furnace is complicated to prepare and is not suitable for small and medium-sized equipment.
  • Recently, some people have used the circulating fluidized bed combustion boiler technology to develop a circulating fluidized bed coal-fired heat-conducting oil furnace.
  • the general circulating fluidized bed combustion boiler is superior to the chain furnace and the pulverized coal furnace, and the existing circulating fluidized bed coal-fired furnace.
  • the temperature stability in the dense phase region is achieved, which is more stable than the conventional layer furnace and the pulverized coal furnace, and the thermal efficiency is also improved.
  • the heat generated by the existing fluidized bed combustion boiler is usually exchanged with a single working medium, so that a considerable portion of the heat is difficult to be fully utilized, and there is a problem that the heat generation method is single, and the overall thermal efficiency needs to be further improved.
  • the object of the present invention is to provide a circulating bed organic heat carrier furnace in which hot oil and steam are co-produced, overcome the shortcomings of the existing heat transfer oil furnace technology, and adopt two kinds of working fluids of heat transfer oil and water, and set multiple kinds and more Class heating surface, different heating surfaces are set in different temperature intervals, different heat exchange modes are adopted, and hot oil and water vapor are generated at the same time.
  • a circulating bed organic heat-generating furnace combined with hot oil and steam comprising a coal feeding device, a combustion bed, a heating surface, a water side drum, a separator, a returning device, a tail flue, and a water side coal saving
  • the air preheater and the ash dropping device are characterized in that: the combustion bed adopts a circulating fluidized bed, and the first heat transfer oil radiation surface is arranged in the rising portion of the flue gas in the vertical section of the combustion bed, and the front surface of the tail flue is arranged
  • the second heat transfer oil radiates the heat receiving surface, and the heat transfer oil convection heating surface is arranged inside the front section of the tail flue;
  • the steam ceiling pipe heating section is arranged in the flue gas outlet section of the circulating fluidized bed, and the steam convection heating surface is arranged in the middle part of the tail flue, the high temperature smoke
  • the gas passes through the first heat-conducting oil to radiate the heating surface and the heated surface of the steam-top
  • the first heat transfer oil radiation heating surface and the second heat transfer oil radiation heat receiving surface 3b adopt a spiral type oil pipe, and the steam ceiling pipe heat receiving surface adopts a water pipe.
  • the invention has the following advantages and outstanding effects:
  • the coal type of the invention has good adaptability, adopts two working fluids of heat conducting oil and water, and sets multiple, multi-stage heating surfaces and different heat exchange modes in different temperature intervals. , producing hot oil at the same time And water vapor, significantly improved the overall thermal efficiency, with good economic and environmental benefits, and has a broad application prospect.
  • FIG. 1 is a schematic view showing a circulating bed organic heat carrier furnace in which hot oil and water vapor are produced in accordance with the present invention.
  • the invention relates to a circulating bed organic heat carrier furnace in which hot oil and steam are co-produced, and the main device comprises a coal feeding device 1, a combustion bed 2, a first heat conducting oil radiation heating surface 3a, and a second heat conducting oil radiation.
  • the heat transfer oil convection heating surface 10 the steam convection heating surface 11, the water side economizer 12, the air preheater 13, the ash hopper 14, the bag filter 15, the induced draft fan 16, and the chimney 17.
  • the combustion bed 2 adopts a circulating fluidized bed, the first heat transfer oil radiation surface 3a is arranged in the flue gas rising section of the combustion bed 2, and the second heat transfer oil radiation heating surface 3b is arranged on the front section of the tail flue 9
  • the heat transfer oil convection heating surface 10 is arranged inside the front section of the track 9; the steam ceiling pipe heating surface 5 is arranged in the flue gas outlet section of the circulating fluidized bed, and the steam convection heating surface 11 is arranged in the middle part of the tail flue.
  • the method of the organic heat medium furnace to which the invention belongs is as follows: the fuel is sent to the combustion bed 2 through the coal feeding device 1 for adiabatic combustion, and low-cost desulfurization is realized by adding limestone, etc., and the combustion temperature is controlled at 850 to 900 ° C to achieve low NOx combustion, the combustion efficiency can reach more than 97%.
  • the high-temperature flue gas generated by the combustion firstly radiates the heating surface 3a through the first heat-conducting oil, and the organic carrier is heated and then taken out by the heat-conducting oil collecting box 4, and sent to the heat-using equipment; the high-temperature flue gas entering the furnace top passes through the steam-covered roof heating surface 5
  • the steam generated by the endothermic enters the water side drum 6 in the form of a steam-water mixture, and is separated by the main steam pipe after being separated by steam and water, and sent to the steam equipment; the high-temperature flue gas containing dust is efficiently separated by the separator 7, and the solid particles are separated. Return to the combustion system via the return device 8.
  • a second heat transfer oil radiant heat receiving surface 3b and a heat transfer oil convection heat receiving surface 10 are disposed in a high temperature portion of the front portion of the tail flue 9, a steam convection heating surface 11 is disposed in the middle portion of the flue, and a water side economizer 12 and an air prestage are disposed in the rear portion of the flue.
  • Heater 13 The high-temperature flue gas passes through the separator and enters the tail flue 9 along the flue gas flow direction and the second heat transfer oil radiation heating surface 3b, the heat transfer oil convection heating surface 10, the steam convection heating surface 11, the water side economizer 12 and the air pre- The heat exchanger 13 exchanges heat to make full use of the heat in the flue gas.
  • an ashing device 14 is arranged to collect the ash deposited by the flue gas. After the heat exchange in the tail flue, the high-temperature flue gas becomes a low-temperature flue gas, and after being dedusted by the bag filter 15 , it is sent to the chimney 17 by the induced draft fan 16 for discharge.
  • the heat transfer oil is first sent to the heat transfer oil convection heating surface 10 through the heat transfer oil header 4a, and the heat oil heated by the heat is sequentially passed through the heat transfer oil header box 4b to the second heat transfer oil radiation heating surface 3b and the first heat transfer oil radiation heating surface.
  • 3a after further heating and heating, is sent to the heat-using equipment through the heat-conducting oil upper header 4c above the first heat-conducting oil radiation heating surface 3a, and the heat-exchanged low-temperature heat-conducting oil passes through the heat-conducting oil lower header 4a to enter the heat-conducting oil convection.
  • the heating surface 10 completes a cycle.
  • the heat transfer oil heated by the heat transfer oil convection heating surface 10 can also enter the first heat transfer oil radiation heating surface 3a and the second heat transfer oil radiation heat receiving surface 3b in parallel, and the heat transfer oil heated by heating passes through the heat conduction.
  • Oil on the header 4c leads to points Do not send to the heat equipment, the low-temperature heat-conducting oil after heat exchange enters the heat-conducting oil convection heating surface 10 through the heat-conducting oil lower header 4a to complete a cycle.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Air Supply (AREA)

Abstract

一种热油与水蒸气联产的循环床有机载热体炉，包括给煤装置（1）、燃烧床（2）、受热面、水侧锅筒（6）、分离器（7）、回料装置（8）、水侧省煤器（12）、空气预热器（13）、落灰装置（14）、布袋除尘器（15）、引风机（16）和烟囱（17）。燃料在绝热燃烧床（2）内燃烧放出热量，高温烟气通过导热油辐射受热面（3a，3b）和蒸汽顶棚管受热面（5）,经分离器（7）进行烟尘分离后进入尾部烟道（9）,依次通过导热油辐射受热面（3a，3b）、导热油对流受热面（10）、蒸汽对流受热面（11）、水侧省煤器（12）、空气预热器（13），进入烟气处理系统。

Description

说 明 书 一种热油与水蒸气联产的循环床有机载热体炉
技术领域
本发明涉及一种热油与水蒸气联产的换热系统， 是循环流化床燃烧导热油炉， 属于能源 利用设备及方法改进领域。
背景技术
导热油炉的原理是将有机载体 （导热油） 加热， 并通过高温油泵进行液相循环将加热后 的导热油输送到用热设备， 再由用热设备出油口回到导热油炉加热， 形成一个完整的热循环 系统。
目前使用的燃煤导热油炉多是层燃炉或者煤粉炉， 层燃炉效率相对较低， 煤种适应性较 差。 煤粉炉所需的燃料煤粉制备复杂， 不适用于中小型设备。 近来有人沿用现有的循环流化 床燃烧锅炉技术开发循环流化床燃煤导热油炉， 一般的循环流化床燃烧锅炉优于链条炉和煤 粉炉， 现有循环流化床燃煤炉依靠颗粒回流带出密相区燃烧富余的热量实现密相区的温度稳 定， 比传统的层燃炉和煤粉炉运行更加稳定， 热效率也有所提高。 但现有的流化床燃烧锅炉 所产生的热量通常以单一的工质交换出去， 导致相当部分的热量难以充分利用， 存在产生热 量方式单一的问题， 且整体热效率有待进一步提高。
发明内容
本发明的目的在于提供热油与水蒸汽联产的循环床有机载热体炉， 克服现有导热油炉技 术的缺点， 通过采用导热油和水两种工质， 并且设置多种、 多级受热面， 在不同的温度区间 设置不同的受热面， 采用不同的换热方式， 同时产生热油、 水蒸汽。
本发明采用的技术方案是：
一种热油与水蒸气联产的循环床有机载热体炉， 包括给煤装置、 燃烧床、 受热面、 水侧 锅筒、 分离器、 回料装置、 尾部烟道、 水侧省煤器、 空气预热器和落灰装置， 其特征在于： 所述的燃烧床采用循环流化床， 燃烧床立段的烟气上升段布置第一导热油辐射面， 尾部烟道 前段立面布置第二导热油辐射受热面， 尾部烟道的前段内部布置导热油对流受热面； 循环流 化床上部的烟气出口段布置蒸汽顶棚管受热面， 尾部烟道中段布置蒸汽对流受热面， 高温烟 气在燃烧床内通过第一导热油辐射受热面和蒸汽顶棚管受热面， 经分离器进行烟尘分离后进 入尾部烟道， 沿烟道方向依次通过第二导热油辐射受热面、 导热油对流受热面、 蒸汽对流受 热面、 水侧省煤器和空气预热器， 最终进入烟气排放系统。
上述技术方案中，所述的第一导热油辐射受热面和第二导热油辐射受热面 3b采用盘旋式 油管， 所述的蒸汽顶棚管受热面采用水管。
本发明具有以下优点及突出性效果： 本发明煤种适应性好， 通过采用导热油和水两种工 质， 并且在不同的温度区间设置多种、 多级受热面以及采用不同的换热方式， 同时产生热油 和水蒸汽， 显著提高了综合热效率， 具有良好的经济效益和环境效益， 应用前景十分广阔。 附图说明
图 1是本发明涉及的一种热油与水蒸气联产的循环床有机载热体炉的示意图。
图中： 1-给煤装置， 2-燃烧床， 3a_第一导热油辐射受热面， 3b_第二导热油辐射受热面， 4a_导热油下集箱， 4b_导热油中集箱， 4c-导热油下集箱， 5-蒸汽顶棚管受热面， 6_水侧锅筒， 7-分离器， 8-回料装置， 9-尾部烟道， 10-导热油对流受热面， 11-蒸汽对流受热面， 12-水侧 省煤器， 13-空气预热器， 14-落灰装置， 15-布袋除尘器， 16-引风机， 17-烟囱。
具体实施方式
下面结合附图详细描述本发明的具体工艺及运行流程：
本发明所述的一种热油与水蒸气联产的循环床有机载热体炉， 主要装置包括给煤装置 1、 燃烧床 2、 第一导热油辐射受热面 3a、 第二导热油辐射受热面 3b、 导热油下集箱 4a、 导热油 中集箱 4b、 导热油上集箱 4c、 蒸汽顶棚管受热面 5、 水侧锅筒 6、 分离器 7、 回料装置 8、 尾 部烟道 9、 导热油对流受热面 10、 蒸汽对流受热面 11、 水侧省煤器 12、 空气预热器 13、 落 灰装置 14、 布袋除尘器 15、 引风机 16和烟囱 17。 所述的燃烧床 2采用循环流化床， 燃烧床 2立段的烟气上升段布置第一导热油辐射面 3a， 尾部烟道 9前段立面布置第二导热油辐射受 热面 3b， 尾部烟道 9的前段内部布置导热油对流受热面 10; 循环流化床上部的烟气出口段布 置蒸汽顶棚管受热面 5， 尾部烟道中段布置蒸汽对流受热面 11。
本发明所属的有机载热体炉采用的方法是： 燃料经给煤装置 1送入燃烧床 2进行绝热燃 烧， 通过添加石灰石等实现低成本脱硫， 燃烧温度控制在 850〜900°C实现低 NOx燃烧， 燃烧 效率可达 97%以上。 燃烧产生的高温烟气首先通过第一导热油辐射受热面 3a， 有机载体经加 热后由导热油集箱 4引出， 送到用热设备； 进入炉顶的高温烟气通过蒸汽顶棚管受热面 5， 吸热产生的蒸汽以汽水混合物的形式进入水侧锅筒 6， 进行汽水分离后经主汽管引出， 送往 用汽设备； 含尘的高温烟气经过分离器 7进行高效分离， 固体颗粒经回料装置 8返回燃烧系 统。 在尾部烟道 9前段的高温部分设置第二导热油辐射受热面 3b和导热油对流受热面 10， 烟道中段设置蒸汽对流受热面 11， 烟道后段设置水侧省煤器 12和空气预热器 13。 高温烟气 经过分离器后进入尾部烟道 9， 沿烟气流向依次与第二导热油辐射受热面 3b、 导热油对流受 热面 10、 蒸汽对流受热面 11、水侧省煤器 12和空气预热器 13换热， 使烟气中的热量得到充 分利用。 尾部烟道 9的下端均设置落灰装置 14， 收集烟气沉积下来的灰。 经过尾部烟道换热 后， 高温烟气变成低温烟气， 经布袋除尘器 15进行除尘后， 由引风机 16送至烟囱 17排放。
导热油首先通过导热油下集箱 4a送入导热油对流受热面 10， 受热升温后的热油通过导 热油中集箱 4b依次进入第二导热油辐射受热面 3b和第一导热油辐射受热面 3a， 经进一步加 热升温后通过第一导热油辐射受热面 3a上方的导热油上集箱 4c引出送至用热设备， 换热后 的低温导热油再通过导热油下集箱 4a进入导热油对流受热面 10， 完成一次循环。 同时， 经 过导热油对流受热面 10换热升温的导热油也可以以并联方式同时进入第一导热油辐射受热 面 3a和第二导热油辐射受热面 3b换热，经过加热升温的导热油通过导热油上集箱 4c引出分 别送至用热设备， 换热后的低温导热油再通过导热油下集箱 4a进入导热油对流受热面 10， 完成一次循环。

Claims

权 利 要 求 书
1、 一种热油与水蒸气联产的循环床有机载热体炉， 包括给煤装置 （1 )、 燃烧床（2)、 受 热面、 水侧锅筒 （6)、 分离器 （7)、 回料装置 （8)、 尾部烟道 （9)、 水侧省煤器 （12)、 空气 预热器 （13 ) 和落灰装置 （14)， 其特征在于： 所述的燃烧床 （2 ) 采用循环流化床， 燃烧床
( 2 )立段的烟气上升段布置第一导热油辐射面 （3a)， 尾部烟道（9)前段立面布置第二导热 油辐射受热面 （3b)， 尾部烟道（9) 的前段内部布置导热油对流受热面 （10); 循环流化床上 部的烟气出口段布置蒸汽顶棚管受热面（5)， 尾部烟道（9) 中段布置蒸汽对流受热面（11 )， 高温烟气在燃烧床内通过第一导热油辐射受热面 （3a) 和蒸汽顶棚管受热面 （5)， 经分离器
( 7 )进行烟尘分离后进入尾部烟道（9)， 沿烟道方向依次通过第二导热油辐射受热面（3b)、 导热油对流受热面 （10)、 蒸汽对流受热面 （11 )、 水侧省煤器（12 )和空气预热器 （13)， 最 终进入烟气排放系统。
2、 权利要求 1所述的一种热油与水蒸气联产的循环床有机载热体炉， 其特征在于： 所 述的第一导热油辐射受热面 （3a) 和第二导热油辐射受热面 （3b ) 采用盘旋式油管， 所述的 蒸汽顶棚管受热面 （5 ) 采用水管。
PCT/CN2014/072384 2013-04-03 2014-02-21 一种热油与水蒸气联产的循环床有机载热体炉 WO2014161396A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201310116093.X 2013-04-03
CN201310116093.XA CN103216937B (zh) 2013-04-03 2013-04-03 一种热油与水蒸气联产的循环床有机载热体炉

Publications (1)

Publication Number Publication Date
WO2014161396A1 true WO2014161396A1 (zh) 2014-10-09

Family

ID=48814955

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2014/072384 WO2014161396A1 (zh) 2013-04-03 2014-02-21 一种热油与水蒸气联产的循环床有机载热体炉

Country Status (2)

Country Link
CN (1) CN103216937B (zh)
WO (1) WO2014161396A1 (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112808168A (zh) * 2021-03-14 2021-05-18 北京四维天拓技术有限公司 一种复合加热的水热反应装置及其复合加热方法

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103216937B (zh) * 2013-04-03 2016-03-30 清华大学 一种热油与水蒸气联产的循环床有机载热体炉
CN103423869B (zh) * 2013-08-13 2016-04-13 北京热华能源科技有限公司 一种卧式循环流化床导热油炉
CN104566947A (zh) * 2013-10-17 2015-04-29 无锡东马锅炉科技有限公司 一种热水蒸汽联产锅炉装置与方法
CN104033271B (zh) * 2014-05-26 2016-06-15 北京时代科锐新能源科技有限公司 一种高效余热回收利用系统
CN105485712A (zh) * 2016-01-13 2016-04-13 北京一亚高科能源科技有限公司 一种导热油锅炉
CN107687632A (zh) * 2017-08-22 2018-02-13 杭州锅炉集团股份有限公司 导热油与水蒸汽双介质联产循环流化床锅炉
CN109827333A (zh) * 2019-03-21 2019-05-31 佛山市三水粤山装饰实业有限公司 一种节能减排的导热油炉系统
CN110470055B (zh) * 2019-08-30 2020-12-25 嘉兴北化高分子助剂有限公司 一种高效导热油锅炉
CN114923177B (zh) * 2022-06-15 2024-03-01 清华大学 双介质tfb气化焚烧炉和实施废料气化焚烧方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200952825Y (zh) * 2006-09-21 2007-09-26 四川东方锅炉工业锅炉集团有限公司 带导热油加热装置的复合锅炉
CN101634449A (zh) * 2009-09-01 2010-01-27 东南大学 循环流化床温烟气循环氧燃烧减排二氧化碳的方法
CN102012097A (zh) * 2010-04-28 2011-04-13 山东圣威新能源有限公司 流化床油水双介质循环锅炉
CN102322632A (zh) * 2011-09-09 2012-01-18 山东圣威新能源有限公司 一种低造价、小型化、模块式、直流循环流化床锅炉
CN103216937A (zh) * 2013-04-03 2013-07-24 清华大学 一种热油与水蒸气联产的循环床有机载热体炉
CN203203246U (zh) * 2013-04-03 2013-09-18 清华大学 一种热油与水蒸气联产的循环床有机载热体炉

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200952825Y (zh) * 2006-09-21 2007-09-26 四川东方锅炉工业锅炉集团有限公司 带导热油加热装置的复合锅炉
CN101634449A (zh) * 2009-09-01 2010-01-27 东南大学 循环流化床温烟气循环氧燃烧减排二氧化碳的方法
CN102012097A (zh) * 2010-04-28 2011-04-13 山东圣威新能源有限公司 流化床油水双介质循环锅炉
CN102322632A (zh) * 2011-09-09 2012-01-18 山东圣威新能源有限公司 一种低造价、小型化、模块式、直流循环流化床锅炉
CN103216937A (zh) * 2013-04-03 2013-07-24 清华大学 一种热油与水蒸气联产的循环床有机载热体炉
CN203203246U (zh) * 2013-04-03 2013-09-18 清华大学 一种热油与水蒸气联产的循环床有机载热体炉

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112808168A (zh) * 2021-03-14 2021-05-18 北京四维天拓技术有限公司 一种复合加热的水热反应装置及其复合加热方法

Also Published As

Publication number Publication date
CN103216937A (zh) 2013-07-24
CN103216937B (zh) 2016-03-30

Similar Documents

Publication Publication Date Title
WO2014161396A1 (zh) 一种热油与水蒸气联产的循环床有机载热体炉
CN104728823B (zh) 一种新型超临界二氧化碳燃煤锅炉
CN203203246U (zh) 一种热油与水蒸气联产的循环床有机载热体炉
TW201533392A (zh) 一種臥式循環流化床過熱蒸汽鍋爐
CN203571721U (zh) 以生物质为燃料的燃烧供热系统
CN205090598U (zh) 一种立式水火管结构的燃煤粉热水锅炉
CN106369591A (zh) 一种炉前烟气干燥连续捆烧生物质锅炉
CN107726305B (zh) 一种适合全负荷scr脱硝的锅炉及工作方法
CN202791972U (zh) 一种锅炉尾部烟气余热利用系统
CN102242921A (zh) 一种用于罐式碳素煅烧炉尾气余热发电系统的余热锅炉
CN201884079U (zh) 利用煅烧车间导热油炉余热的汽轮发电机组回热系统
CN103574594B (zh) 以生物质为燃料的燃烧供热系统
CN204006649U (zh) 一种多管式高温热风炉
CN102537917A (zh) 带调温器的锅炉烟气余热回收装置
CN203443378U (zh) 一种改进的带副产煤气补燃的石灰窑废气余热发电系统
CN201229117Y (zh) 辊道窑余热回收装置
CN108626714A (zh) 一种生物质燃烧发电系统及其锅炉尾气处理装置
CN105318307A (zh) 一种双锅筒横置式沉降室喷淋脱硝角管锅炉
CN209310262U (zh) 一种供暖用余热回收锅炉
CN202390367U (zh) 一种带有氮气补充器的干法熄焦烟气热量回收装置
CN208652524U (zh) 采用大比例烟气再循环的对流换热超临界二氧化碳锅炉结构
CN201672675U (zh) 流化床油水双介质循环锅炉
CN104848261A (zh) 一种高效率回风炉
CN105650661A (zh) 新型锅炉热管余热回收设备
CN204062980U (zh) 一种双锅筒横置式沉降室喷淋脱硝角管锅炉

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14780281

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14780281

Country of ref document: EP

Kind code of ref document: A1