TWI484125B - 迴流懸浮式煅燒爐系統及其使用方法 - Google Patents
迴流懸浮式煅燒爐系統及其使用方法 Download PDFInfo
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- TWI484125B TWI484125B TW101116464A TW101116464A TWI484125B TW I484125 B TWI484125 B TW I484125B TW 101116464 A TW101116464 A TW 101116464A TW 101116464 A TW101116464 A TW 101116464A TW I484125 B TWI484125 B TW I484125B
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- cyclone dust
- dust collecting
- collecting device
- suspension calciner
- reflux suspension
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- 239000000725 suspension Substances 0.000 title claims description 30
- 238000004519 manufacturing process Methods 0.000 title 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 70
- 239000000428 dust Substances 0.000 claims description 43
- 239000001569 carbon dioxide Substances 0.000 claims description 35
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 35
- 238000002485 combustion reaction Methods 0.000 claims description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 25
- 239000003546 flue gas Substances 0.000 claims description 25
- 238000010992 reflux Methods 0.000 claims description 22
- 239000000843 powder Substances 0.000 claims description 21
- 238000001354 calcination Methods 0.000 claims description 20
- 238000000034 method Methods 0.000 claims description 19
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical group [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 10
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 9
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 6
- 101100513612 Microdochium nivale MnCO gene Proteins 0.000 claims description 3
- 239000002250 absorbent Substances 0.000 claims description 3
- 230000002745 absorbent Effects 0.000 claims description 3
- 230000003134 recirculating effect Effects 0.000 claims description 3
- 239000000567 combustion gas Substances 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
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- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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Description
本發明係有關於一種廢氣處理裝置,特別是有關於一種迴流懸浮式煅燒爐系統。
台灣在西元2006年時如果各部門不分攤用電所排放的二氧化碳,則能源工業(能源轉換)的二氧化碳排放為164,086千公噸,佔燃料燃燒總排放的61.86%。但如果就各主要部門之二氧化碳排放分析,在分攤用電排放之情況下台灣在西元2006年能源工業(能源轉換)的二氧化碳排放為18,509千公噸,佔燃料燃燒總排放的6.98%,由上述的數據可以知道能源工業發電給各部門使用所產生的二氧化碳佔燃料燃燒總排放的54.88%。幾乎佔台灣二氧化碳總排放量的一半以上,也因此電廠的二氧化碳排放如能有效的被捕獲將能大幅減少二氧化碳的排放。
水泥業亦為二氧化碳排放之大宗,但空氣燃燒與氣密不佳,即使系統煅燒產生二氧化碳,排放的煙氣二氧化碳濃度仍然只有25-30 vol%,依舊需要捕獲技術提高濃度才具有再利用與封存效益,此外,水泥業為六大耗能產業之一,製程採空氣燃燒又多半沒有保溫,熱損過多能源效益低,唯一提高效率的方法是透過餘熱發電回收,但投資成本與所需場地空間大。另外,傳統技術未能掌握輕質碳酸鈣商機。
根據上述,本發明一實施例提供一種迴流懸浮式煅燒爐系統,包括:包含有複數個單元之旋風集塵設備;一直立燃燒窯,包括一頂側和一底側,其中直立燃燒窯之頂側連接旋風集塵設備之最下側的單元,直立燃燒窯之底側連接旋風集塵設備之最上側的單元;一風車,連接旋風集塵設備之最上側的單元;及一排料系統,連接旋風集塵設備之最下側的單元。
本發明一實施例提供一種迴流懸浮式煅燒爐系統,包括:複數個單元之旋風集塵設備,其中旋風集塵設備之頂部單元係用作一進料系統、一直立燃燒窯、一風車及一排料系統,進料系統中的粉體下落旋風集塵設備,上述粉體下落經過數個旋風集塵設備之單元與逆向的高溫煙氣混合熱交換,產生煅燒反應並釋出二氧化碳進入煙氣中,且此煙氣經過分流程序與風車推動輸送至進料系統,作為粉體的進料輸送氣體。
為讓本發明之特徵能更明顯易懂,下文特舉實施例,並配合所附圖式,作詳細說明如下:
以下詳細討論實施本發明之實施例。所討論之特定實施例僅用來揭示使用實施例的特定方法,而不用來限定揭示的範疇。
本發明係揭示有關於二氧化碳捕獲系統之煅燒設備,在高溫下捕獲例如電廠排氣中之二氧化碳,提高二氧化碳
之捕獲,並使吸附劑不斷再利用,減少反應時間且節省燃料,降低二氧化碳捕獲成本。本發明係利用具時間與燃料效率的「迴流懸浮式煅燒爐」在節省能源與降低成本下進行吸收劑煅燒,例如煅燒碳酸鈣(CaCO3
)得到氧化鈣(CaO),藉以製成輕質碳酸鈣或利用其進行二氧化碳的捕獲。
第1圖顯示本發明一實施例迴流懸浮式煅燒爐系統示意圖,請參照第1圖,本實施例迴流懸浮式煅燒爐系統由進料系統102、包括複數個單元之旋風集塵設備104、直立燃燒窯106、風車108及排料系統110組成,其中該旋風集塵設備104之頂部單元用作進料系統102,旋風集塵設備之每一單元104底部以旋轉閥(rotary valve)或法藍(flange)與其餘的旋風集塵設備單元相接,並區隔彼此設備壓力。如第1圖所示,直立燃燒窯106包括一頂側和一底側,其中直立燃燒窯106之頂側連接旋風集塵設備104之最下側的單元,直立燃燒窯106之底側連接旋風集塵設備104之最上側的單元。風車108係連接該旋風集塵設備104之最上側的單元,且排料系統110亦包括一頂側和一底側,排料系統110之頂側係連接旋風集塵設備104之最下側的單元,而排料系統110之底側係透過一管路(以虛線表示)而連接於用以連接風車108與旋風集塵設備104之最上側的單元之間之管路(以虛線表示)。
進料系統102的運作乃利用風車108推動位於旋風集塵設備之一高處單元(例如為由最上側數來第二個單元)之
出口約600~1000℃之高濃度二氧化碳,氣送來自於排料系統110之底側所供應之將進行煅燒程序的碳酸鈣(CaCO3
)到進料系統102(頂端的旋風集塵設備),在旋風集塵設備104中氣固分離後,碳酸鈣(CaCO3
)之粉體受到重力向下落經過數個旋風集塵設備104之單元,與由下而上的煙氣逆向交錯(其中煙氣的來源為燃燒機排出的燃燒反應產物,本實施例煙氣包含有水和二氧化碳),充分熱交換後,產生煅燒反應,形成氧化鈣(CaO),並釋出二氧化碳,而旋風集塵設備104之最下方單元則將經煅燒反應後所形成之氧化鈣(CaO)的粉體傳輸至排料系統110之後,於排料系統110中反應生成可供應至進料系統102(頂端的旋風集塵設備)進行煅燒程序的碳酸鈣(CaCO3
)。在本實施例中,該煙氣之溫度範圍為500℃~1000℃。含有二氧化碳之煙氣經風車108推動輸送至進料系統102,作為如進行煅燒程序的碳酸鈣(CaCO3
)之粉體的進料輸送氣體。部分之煙氣係排放進行封存或二氧化碳再利用,亦使整個系統壓力與質量維持穩定;部分的煙氣在氣送氣固分離完畢之後係傳輸至直立燃燒窯106之底側處,並加入適量高純度氧氣(例如大於93%之純氧),作為直立燃燒窯106之燃燒空氣,與燃料一起燃燒加熱至900-1200℃,進入旋風集塵設備104之底部單元,以提高二氧化碳之濃度,並具抑制純氧燃燒高溫的功能,避免粉體燒結與設備損壞,粉體後續進入排料系統110。迴流量的多寡乃是本設備控制煙氣溫度的關鍵,煙氣由下往上流動與粉體充分熱交換,提供煅燒粉體所需之煅
燒能量,其中熱煙氣成分以二氧化碳和水蒸汽為主。煅燒粉體可使用金屬碳酸化物之吸收劑,其可以為CaCO3
、ZeCO3
、MgCO3
、MnCO3
或NiCO3
等。若熱煙氣要直接封存或使其二氧化碳再利用,降溫冷凝之後可直接分離水並得到高濃度之二氧化碳。直立燃燒窯的部分可以針對去碳酸化不足的部分做加強,拉長直立燃燒窯106高度延長粉體滯留時間,使煅燒反應率維持在90%以上。
根據上述,本發明「迴流懸浮式煅燒爐系統」係利用純氧燃燒(oxy-combustion)概念,在煅燒爐燃燒器完成CO2
-O2
燃燒。煅燒(calcine)金屬碳酸化物,利用尾氣迴流(Flue gas recirculation)方式控制入口煙氣溫度在900-1200℃,逐步增加煅燒爐內部煙氣二氧化碳濃度。本發明迴流懸浮式煅燒爐系統具有以下優點:第一,可製造高濃度二氧化碳有利地質封存與工業再利用;第二,促進能源效率,讓低於煅燒還原之溫度之煙氣透過再加熱循環釋出高溫反應熱,最後循環尾氣還可作為氣送氣體輸送進料的金屬碳酸化物;第三,系統得到煅燒後的金屬氧化物則可作為吸附劑或工業原料使用;第四,本發明流程中製成的氧化鈣(CaO)有助於生產大量的輕質碳酸鈣,輕質碳酸鈣在工業中有相當大的應用範圍,具有相當高之經濟效益。
雖然本發明已以較佳實施例發明如上,然其並非用以限定本發明,任何熟習此技藝者,在不脫離本發明之精神和範圍內,當可作些許之更動與潤飾,因此本發明之保護範圍當視後附之申請專利範圍所界定者為準。
102...進料系統
104...旋風集塵設備
106...直立燃燒窯
108...風車
110...排料系統
第1圖顯示本發明一實施例迴流懸浮式煅燒爐系統示意圖。
102...進料系統
104...旋風集塵設備
106...直立燃燒窯
108...風車
110...排料系統
Claims (20)
- 一種迴流懸浮式煅燒爐系統,包括:包含有複數個單元之旋風集塵設備;一直立燃燒窯,包括一頂側和一底側,其中該直立燃燒窯之頂側連接該旋風集塵設備之最下側的單元,該直立燃燒窯之底側連接該旋風集塵設備之最上側的單元;一風車,連接該旋風集塵設備之最上側的單元;及一排料系統,連接該旋風集塵設備之最下側的單元。
- 如申請專利範圍第1項所述之迴流懸浮式煅燒爐系統,其中旋風集塵設備之最上側的單元係為該迴流懸浮式煅燒爐系統的進料系統。
- 如申請專利範圍第1項所述之迴流懸浮式煅燒爐系統,其中該旋風集塵設備包括3~7個單元。
- 如申請專利範圍第1項所述之迴流懸浮式煅燒爐系統,其中該旋風集塵設備之每一單元底部以旋轉閥(rotary valve)或法藍(flange)與其餘的旋風集塵設備單元相接。
- 如申請專利範圍第1項所述之迴流懸浮式煅燒爐系統,其中該進料系統中的粉體下落至該旋風集塵設備,上述粉體下落經過複數個旋風集塵設備之單元與逆向的煙氣混合熱交換,產生煅燒反應並釋出二氧化碳,且該含有二氧化碳之煙氣經該風車推動輸送至該進料系統,作為該粉體的進料輸送氣體。
- 如申請專利範圍第5項所述之之迴流懸浮式煅燒爐系統,其中該粉體為碳酸鈣(CaCO3 )。
- 如申請專利範圍第5項所述之之迴流懸浮式煅燒爐系統,其中該煅燒反應係使用金屬碳酸化物之吸收劑。
- 如申請專利範圍第7項所述之之迴流懸浮式煅燒爐系統,,其中該金屬碳酸化物包括CaCO3 、ZeCO3 、MgCO3 、MnCO3 或NiCO3 。
- 一種迴流懸浮式煅燒爐系統之使用方法,包括:提供包含有複數個單元之旋風集塵設備、一直立燃燒窯、一風車及一排料系統,其中該旋風集塵設備之頂部單元係用作一進料系統;使該進料系統中的粉體下落該旋風集塵設備,上述粉體下落經過數個旋風集塵設備之單元與逆向之含有二氧化碳的煙氣混合熱交換,產生煅燒反應並釋出二氧化碳;及使該含有二氧化碳的煙氣經該風車推動輸送至該進料系統,作為該粉體的進料輸送氣體。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中部分輸送至該進料系統的含有二氧化碳的煙氣係於該直立燃燒窯中進行純氧燃燒。
- 如申請專利範圍第10項所述之迴流懸浮式煅燒爐系統之使用方法,其中該純氧燃燒後之氣體係進入該旋風集塵設備之底部的單元。
- 如申請專利範圍第10項所述之迴流懸浮式煅燒爐系統之使用方法,其中該純氧燃燒係加入純氧和燃料。
- 如申請專利範圍第10項所述之迴流懸浮式煅燒爐系統之使用方法,其中該純氧燃燒之溫度為900-1200℃。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中該粉體為碳酸鈣(CaCO3 )。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中該粉體經煅燒反應形成氧化鈣(CaO)。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中該煅燒反應釋出包含二氧化碳之煙氣之溫度為600~1000℃。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中該煙氣之溫度範圍為500℃~1000℃。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,尚包括使該釋出煙氣中之二氧化碳進行封存或再利用。
- 如申請專利範圍第9項所述之迴流懸浮式煅燒爐系統之使用方法,其中該煅燒反應係使用金屬碳酸化物之吸收劑。
- 如申請專利範圍第19項所述之迴流懸浮式煅燒爐系統之使用方法,其中該金屬碳酸化物包括CaCO3 、ZeCO3 、MgCO3 、MnCO3 或NiCO3 。
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