CN105698549A - 一种氧化铝焙烧窑烟气旋流冷凝式换热装置及方法 - Google Patents
一种氧化铝焙烧窑烟气旋流冷凝式换热装置及方法 Download PDFInfo
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- CN105698549A CN105698549A CN201610059733.1A CN201610059733A CN105698549A CN 105698549 A CN105698549 A CN 105698549A CN 201610059733 A CN201610059733 A CN 201610059733A CN 105698549 A CN105698549 A CN 105698549A
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[O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000001354 calcination Methods 0.000 title claims abstract description 26
- 239000000779 smoke Substances 0.000 title abstract description 14
- 238000009833 condensation Methods 0.000 title abstract description 7
- 230000005494 condensation Effects 0.000 title abstract description 7
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 45
- 239000003546 flue gas Substances 0.000 claims description 45
- 229910001884 aluminium oxide Inorganic materials 0.000 claims description 26
- 239000000443 aerosol Substances 0.000 claims description 21
- 239000002893 slag Substances 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 239000000428 dust Substances 0.000 abstract description 2
- 238000005507 spraying Methods 0.000 abstract description 2
- 238000005406 washing Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 2
- 210000001503 Joints Anatomy 0.000 abstract 1
- 238000004134 energy conservation Methods 0.000 abstract 1
- 238000010248 power generation Methods 0.000 abstract 1
- 239000002918 waste heat Substances 0.000 abstract 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K Aluminium hydroxide Chemical compound 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[OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 241000208125 Nicotiana Species 0.000 description 2
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000011068 load Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
- F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
- F27M2001/00—Composition, conformation or state of the charge
- F27M2001/01—Charges containing mainly non-ferrous metals
- F27M2001/012—Aluminium
-
- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
提供一种氧化铝焙烧窑烟气旋流冷凝式换热装置及方法，装置包括相互连接的风机、喷雾器、烟囱、收雾器、回水池、溢流管、收尘器、热水泵、冷水泵、螺旋导流板、风管、用户；其方法包括：来自氧化铝焙烧窑的150-170℃热湿烟气通过风机、风管进入冷凝换热塔的下部，经过螺旋导流板后向上运行，经喷雾器喷淋对流热交换后，冷却水从50℃被加热至80℃后与烟气中的冷凝水汇合后进入回水池中后通过热水泵被送往用户使用，其优点是：回收热水可用于氧化铝生产中的赤泥和平盘洗涤、用户采暖或ORC余热发电。可以回收含湿含热烟气中的热量80％-90％以上，经济效益、节能减排及环保效果显著。
Description
技术领域
:
[0001]本发明涉及炉窑烟气余热利用工艺设备技术领域，特别是涉及氧化铝焙烧窑烟气换热装置及方法。
背景技术
:
[0002]在现有技术中，氢氧化铝焙烧是氧化铝生产过程的最后一道工序，该工序主要是将含有6%左右的附着水及35%晶格水的氢氧化铝通过焙烧炉在约1200°C的温度下进行脱水而形成氧化铝，在该生产过程中要通过煤气或者天然气进行燃烧升温，完成对氢氧化铝的脱水，在脱水过程中会产生大量的水烟气，水烟气温度基本在150 °C〜170°C之间，烟气含水量约在40 %〜50 %左右。该水份以水蒸气形式存在于烟气中，含有大量的汽化潜热。如此大量的含湿含热烟气带走了较多的热量和水份，造成氧化铝焙烧窑系统能量的损失，使得氧化铝生产成本高、能耗高。如果能回收该尾气中的热能和水，可以最大限度降低氧化铝生产的综合能耗，降低了氧化铝的生产成本，也最大限度实现了氧化铝生产的节能减排。
发明内容
:
[0003]本发明的目的是克服现有技术存在的缺陷，提供一种能回收氧化铝焙烧过程产生的大量气化潜热、最大限度降低氧化铝生产的综合能耗，降低氧化铝的生产成本、实现节能减排的氧化铝焙烧窑烟气换热装置及方法。
[0004]本发明的技术解决方案是:提供一种氧化铝焙烧窑烟气旋流冷凝式换热装置，包括风机、喷雾器、烟囱、收雾器、回水池、溢流管、收尘器、热水栗、冷水栗;其特征是:还包括螺旋导流板、风管、用户;风机安装在风管的入口处;风管的出口斜向安装在冷凝换热塔的下部;冷凝换热塔顶部与烟囱衔接;冷凝换热塔上部安装有收雾器，收雾器下方安装有喷雾器，喷雾器的下方安装有螺旋导流板;冷凝换热塔下部安装有回水池；回水池外部安装有热水管和溢流管；回水池外部的热水管连通收渣器和热水栗后连接用户，用户使用后的冷水通过冷却水管和冷水栗与冷凝换热塔上部安装的喷雾器连通。其装置特征还在于:与风管连通的风机为变频风机;风管倾斜向上布置在冷凝换热塔的下部;风管本体与冷凝换热塔塔体相切连接;螺旋导流板设置在冷凝换热塔筒体内边缘，螺旋导流板的螺旋是由低到高向上设置的，风管进风口与塔体内弧板相切;喷雾器设置有两排，每排喷淋管都设置有单独可调节的阀门；冷凝换热塔顶部设置的收雾器为W形除雾器;冷凝换热塔下部设置的螺旋导流板有3层。提供一种氧化铝焙烧窑烟气旋流冷凝式换热方法，其特征是:来自氧化铝焙烧窑的150_170°C热湿烟气A通过风机、风管进入冷凝换热塔的下部，热湿烟气A经过螺旋导流板后向上运行，在经受了喷雾器冷却喷雾水的喷淋并在冷凝换热塔中直接与冷却喷雾水进行对流热交换后，冷却水D从50°C被加热至80°C后与烟气中的冷凝水汇合后进入回水池中，加热至80°C的热水C经收渣器净化后通过热水栗被送往用户使用，从用户使用后返回的冷却水通过冷水栗从冷凝换热塔的上部进入冷凝换热塔后与来自氧化铝焙烧窑的150-170°C湿热烟气进行热交换后再返回回水池进入下一个循环；换热后的烟气经喷雾器、收雾器处理温度降至ere左右后从冷凝换热塔顶部进入烟囱再向大气排放;其方法特征还在于:用户包括利用热水洗涤生产流程中产生的赤泥和平盘的氧化铝生产用户、采暖或使用热水的周边用户、ORC余热发电用户；湿热烟气A通过变频风机在风管中倾斜向上旋流鼓入冷凝换热塔的下部。
[0005]本发明的有益效果是:回收的大量热水可直接用于氧化铝生产流程中赤泥和平盘洗涤、还可用于企业或周边用户采暖或用于ORC余热发电。由于将冷凝换热塔塔体内边缘设置有螺旋向上的导流板，其进风口与内弧板相切，当混合湿烟气进入冷凝换热塔塔体后，随螺旋导流板的螺旋向上运行，破坏了层流结构，加强了换热强度，并且在温度降到烟气露点温度后，结露的液滴因比重大于烟气比重而甩至塔壁和导流板上，并沿塔壁向下流走，实现与烟气分离，减小了后程除雾器的负荷，使得排烟含水降至最小范围。也达到混合气体适当的紊流效果、提高流体雷诺数值、且需尽可能的将烟气和冷凝水迅速分离，增加逆流换热过程、旋流冷凝式换热塔下部烟气入口处流速较快、促使烟气分布均匀。由于循环冷却水经总管后分为2根管流出，实现2排喷雾器喷淋，每排喷淋管都设置有阀门，通过调节阀门来提高喷淋效果。由于在旋流冷凝式换热塔顶部设置W形除雾器，可以有效防止液滴被烟气携带到换热器外，造成循环冷却水损失及烟道腐蚀。利用旋流冷凝式换热塔不仅回收了烟气中的显热和水蒸气的潜热，还回收了烟气中的水分和氧化铝粉尘。通过热工计算，本发明可以回收含湿含热烟气中的热量80%-90%以上，经济效益、节能减排及环保效果显著。
附图说明
:
[0006]图1是本发明实施例一种氧化铝焙烧窑烟气旋流冷凝式换热装置及方法流程图。
[0007]附图中:1.风机;2.风管;3.喷雾器;4.烟囱；5.收雾器;6.螺旋导流板;7.回水池；
8.溢流管;9.收渣器;10.热水栗；11.用户；12.冷水栗;A.热湿烟气;B.烟气;C.热水;D.冷水
具体实施方式
:
[0008]下面结合附图进一步详细介绍本发明实施例的一种氧化铝焙烧窑烟气旋流冷凝式换热装置，如图1所示的一种氧化铝焙烧窑烟气旋流冷凝式换热装置，包括相互连接的风机1、喷雾器3、烟囱4、收雾器5、回水池7、溢流管8、收渣器9、热水栗1、冷水栗12、螺旋导流板6、风管2、用户11;风机I安装在风管2的入口处;风管2的出口斜向安装在冷凝换热塔13的下部;冷凝换热塔13顶部与烟囱4衔接;冷凝换热塔13由上至下依次安装有收雾器5、喷雾器
3、螺旋导流板6、回水池7;回水池7外部安装有热水管和溢流管8;回水池外部的热水管连通收渣器9和热水栗10后连接用户11，用户11使用后的冷水通过冷却水管和冷水栗12与冷凝换热塔13上部安装的喷雾器3连通;风机I为变频风机;风管2倾斜向上布置在冷凝换热塔13的下部;风管2本体与冷凝换热塔13塔体相切连接;螺旋导流板6设置在冷凝换热塔13筒体内边缘，螺旋导流板的螺旋是由低到高向上设置的，风管进风口与塔体内弧板相切;喷雾器3有两排，每排喷淋管都安装可调节的阀门；收雾器5为W形除雾器;冷凝换热塔13下部设置的螺旋导流板6有3层。提供一种氧化铝焙烧窑烟气旋流冷凝式换热方法，其特征是:来自氧化铝焙烧窑的150-170 0C热湿烟气A通过风机1、风管2进入冷凝换热塔13的下部，热湿烟气A经过螺旋导流板6后向上运行，在冷凝换热塔13中与冷却喷雾水进行对流热交换后，冷却水D从50 °C被加热至80°C后与烟气中的冷凝水汇合后进入回水池7中，加热至80 °C的热水C经收渣器9净化后通过热水栗10被送往用户11使用，从用户11使用后返回的冷却水通过冷水栗12从冷凝换热塔13的上部进入冷凝换热塔后与湿热烟气进行热交换后再返回回水池进入下一个循环;换热后的烟气经喷雾器3、收雾器5处理温度降至ere左右后从冷凝换热塔13顶部进入烟囱4向大气排放。用户11包括利用热水洗涤生产流程中产生的赤泥和平盘的氧化铝生产用户、采暖或使用热水的周边用户、ORC余热发电用户;湿热烟气A通过变频风机I在风管2中倾斜向上旋流鼓入冷凝换热塔13的下部。因事故等原因溢出的水就经过溢流管8外排了。
Claims (7)
1.一种氧化铝焙烧窑烟气旋流冷凝式换热装置，包括风机(I)、喷雾器(3)、烟囱(4)、收雾器(5)、回水池(7)、溢流管(8)、收渣器(9)、热水栗(10)、冷水栗(12);其特征是:还包括螺旋导流板(6)、风管(2)、用户(11);风机(I)安装在风管(2)的入口处;风管(2)的出口斜向安装在冷凝换热塔(13)的下部;冷凝换热塔(13)顶部与烟囱(4)衔接;冷凝换热塔(13)上部安装有收雾器(5)，收雾器(5)下方安装有喷雾器(3)，喷雾器(3)的下方安装有螺旋导流板(6);冷凝换热塔(13)下部安装有回水池(7);回水池(7)外部安装有热水管和溢流管(8);回水池外部的热水管连通收渣器(9)和热水栗(10)后连接用户(11)，用户(11)使用后的冷水通过冷却水管和冷水栗(12)与冷凝换热塔(13)上部安装的喷雾器(3)连通。
2.如权利要求1所示的一种氧化铝焙烧窑烟气旋流冷凝式换热装置，其特征在于:与风管(2)连通的风机(I)为变频风机;风管(2)倾斜向上布置在冷凝换热塔(13)的下部;风管(2)本体与冷凝换热塔(13)塔体相切连接。
3.如权利要求1所示的一种氧化铝焙烧窑烟气旋流冷凝式换热装置，其特征在于:螺旋导流板(6)设置在冷凝换热塔(13)筒体内边缘，螺旋导流板的螺旋是由低到高向上设置的，风管进风口与塔体内弧板相切。
4.如权利要求1所示的一种氧化铝焙烧窑烟气旋流冷凝式换热装置，其特征在于:喷雾器(3)设置有两排，每排喷淋管都设置有单独可调节的阀门；冷凝换热塔(13)顶部设置的收雾器(5)为W形除雾器;冷凝换热塔(13)下部设置的螺旋导流板(6)有3层。
5.一种氧化铝焙烧窑烟气旋流冷凝式换热方法，其特征是:来自氧化铝焙烧窑的150-170°C热湿烟气A通过风机(I)、风管(2)进入冷凝换热塔(13)的下部，热湿烟气A经过螺旋导流板(6)后向上运行，在经受了喷雾器(3)冷却喷雾水的喷淋并在冷凝换热塔(13)中直接与冷却喷雾水进行对流热交换后，冷却水D从50 °C被加热至80 °C后与烟气中的冷凝水汇合后进入回水池(7)中，加热至80°C的热水C经收渣器(9)净化后通过热水栗(10)被送往用户(11)使用，从用户(11)使用后返回的冷却水通过冷水栗(12)从冷凝换热塔(13)的上部进入冷凝换热塔后与来自氧化铝焙烧窑的150-170°C湿热烟气进行热交换后再返回回水池进入下一个循环；换热后的烟气经喷雾器(3)、收雾器(5)处理温度降至ere左右后从冷凝换热塔(13)顶部进入烟囱(4)再向大气排放。
6.如权利要求5所示的一种氧化铝焙烧窑烟气旋流冷凝式换热方法，其特征在于:用户(11)包括利用热水洗涤生产流程中产生的赤泥和平盘的氧化铝生产用户、采暖或使用热水的周边用户、ORC余热发电用户。
7.如权利要求5所示的一种氧化铝焙烧窑烟气旋流冷凝式换热方法，其特征在于:湿热烟气A通过变频风机(I)在风管(2)中倾斜向上旋流鼓入冷凝换热塔(13)的下部。
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