JP4364022B2 - Energy recovery method from organic waste - Google Patents
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- JP4364022B2 JP4364022B2 JP2004075697A JP2004075697A JP4364022B2 JP 4364022 B2 JP4364022 B2 JP 4364022B2 JP 2004075697 A JP2004075697 A JP 2004075697A JP 2004075697 A JP2004075697 A JP 2004075697A JP 4364022 B2 JP4364022 B2 JP 4364022B2
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- 238000000034 method Methods 0.000 title claims description 31
- 239000010815 organic waste Substances 0.000 title claims description 30
- 238000011084 recovery Methods 0.000 title claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 128
- 229910021529 ammonia Inorganic materials 0.000 claims description 62
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 26
- 238000000354 decomposition reaction Methods 0.000 claims description 23
- 239000002351 wastewater Substances 0.000 claims description 21
- 238000002407 reforming Methods 0.000 claims description 18
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 16
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 16
- 229910052759 nickel Inorganic materials 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 14
- 239000001257 hydrogen Substances 0.000 claims description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 11
- 238000004140 cleaning Methods 0.000 claims description 10
- 238000010248 power generation Methods 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 8
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 7
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 7
- 230000018044 dehydration Effects 0.000 claims description 7
- 238000006297 dehydration reaction Methods 0.000 claims description 7
- 229910052747 lanthanoid Inorganic materials 0.000 claims description 7
- 150000002602 lanthanoids Chemical class 0.000 claims description 7
- 239000000377 silicon dioxide Substances 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000000428 dust Substances 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 5
- 229910044991 metal oxide Inorganic materials 0.000 claims description 5
- 150000004706 metal oxides Chemical class 0.000 claims description 5
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 5
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 5
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 21
- 238000002309 gasification Methods 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 11
- 229910052788 barium Inorganic materials 0.000 description 9
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 9
- 239000010801 sewage sludge Substances 0.000 description 7
- 238000004065 wastewater treatment Methods 0.000 description 6
- 238000005406 washing Methods 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000007738 vacuum evaporation Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052712 strontium Inorganic materials 0.000 description 1
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 description 1
- 230000036962 time dependent Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
-
- 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
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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
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
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- Degasification And Air Bubble Elimination (AREA)
Description
本発明は、下水汚泥、バイオマスなどの有機性廃棄物からのエネルギー回収方法に関するものである。 The present invention relates to a method for recovering energy from organic waste such as sewage sludge and biomass.
従来一般に、下水汚泥やバイオマスなどの有機性廃棄物は脱水または焼却され、脱水汚泥や焼却灰として埋め立て処分されてきたが、新たな処分場の確保は次第に困難になりつつある。また焼却時に発生する二酸化炭素は地球温暖化の原因とされ排出量の削減が求められている。このため最近では特許文献1に示されるように、有機性廃棄物を熱分解してガス化するとともに改質し、有機分を可燃性ガスとして回収する有機性廃棄物のガス化改質技術が開発されている。 Conventionally, organic waste such as sewage sludge and biomass has been dehydrated or incinerated and disposed of in landfill as dehydrated sludge or incinerated ash, but securing new disposal sites is becoming increasingly difficult. In addition, carbon dioxide generated during incineration is a cause of global warming and reduction of emissions is required. For this reason, recently, as shown in Patent Document 1, organic waste gasification reforming technology that thermally decomposes organic waste and gasifies and reforms, and recovers organic components as a combustible gas has been developed. Has been developed.
この方法により有機性廃棄物から可燃性ガスを得るためには、まず有機性廃棄物を脱水・乾燥する前処理を施したうえで、ガス化改質炉でガス化及び改質処理する方法が取られる。この前処理として行われる脱水、乾燥工程においては、有機性廃棄物中に含まれる窒素分の一部はアンモニアとして排水(ドレン水)に移行する。 In order to obtain a combustible gas from organic waste by this method, there is a method in which the organic waste is first subjected to pretreatment for dehydration and drying, and then gasified and reformed in a gasification reforming furnace. Taken. In the dehydration and drying steps performed as the pretreatment, a part of nitrogen contained in the organic waste is transferred to drainage (drain water) as ammonia.
また、脱水、乾燥された有機性廃棄物はガス化改質炉において酸素、水蒸気、空気等と反応(部分燃焼)することによりH2,CO,CO2,H2Oから構成される可燃性ガスに改質される。このとき可燃性ガス中に含有される窒素分はアンモニアとしてガス中に移行し、ガス化改質炉の後段のガス洗浄工程において排水中へ移行する。 In addition, dehydrated and dried organic waste is combustible composed of H 2 , CO, CO 2 , and H 2 O by reacting with oxygen, water vapor, air, etc. (partial combustion) in a gasification reforming furnace. It is reformed to gas. At this time, the nitrogen content contained in the combustible gas is transferred into the gas as ammonia, and is transferred into the waste water in the gas cleaning step after the gasification reforming furnace.
このように有機性廃棄物の脱水・乾燥工程およびガスの洗浄工程において排水中に移行したアンモニアは、生物処理法、不連続塩素処理法、オゾン処理法などにより分解して放流したり、あるいはアンモニアストリッピング法により排水中から放散させ、放散されたアンモニアを燃焼分解あるいは吸着除去している。また放散させたアンモニアの処理方法としては、ガス化改質炉へ再投入して分解する方法もあるが分解率が悪く、投入したアンモニアはガス洗浄工程において再度排水中へ移行してしまう。いずれの方法でも、前処理やガス洗浄工程において排水中へ移行したアンモニア、及びガス洗浄工程において排水中へ移行したアンモニアはエネルギーとして全く利用されていない。
本発明は上記した従来の問題点を解決し、有機性廃棄物をガス化改質して可燃性ガスを回収する工程において、排水中へ移行したアンモニアから更にエネルギーを回収することができる有機性廃棄物からのエネルギー回収方法を提供するためになされたものである。 The present invention solves the above-mentioned conventional problems, and in the process of recovering combustible gas by gasifying and reforming organic waste, it is possible to recover further energy from ammonia transferred into waste water. It was made to provide a method for recovering energy from waste.
上記の課題を解決するためになされた本発明は、有機性廃棄物をガス化改質する前処理段階の脱水・乾燥工程で発生する排水、および脱水・乾燥した有機性廃棄物をガス化改質して発生させたガスの除塵・洗浄工程で発生する排水中に含まれるアンモニアを回収し、回収されたアンモニアを分解触媒により水素と窒素に分解して水素を回収し、この水素を発電装置のエネルギー源として利用することを特徴とするものである。 In order to solve the above-mentioned problems, the present invention is directed to gasifying and reforming wastewater generated in a dehydration / drying process in a pretreatment stage for gasifying and reforming organic waste, and dehydrated / dried organic waste. The ammonia contained in the wastewater generated in the dust removal and cleaning process of the gas generated by the gas is recovered, the recovered ammonia is decomposed into hydrogen and nitrogen by the decomposition catalyst, and hydrogen is recovered, and this hydrogen is recovered as a power generator. It is characterized by being used as an energy source.
なお、アンモニアの分解触媒として、アルミナ、シリカ、チタニア、ジルコニア等の金属酸化物担体上にニッケルまたはニッケル酸化物を第1成分として担持させ、更にアルカリ土類金属及びランタノイド元素の少なくとも一方を金属または酸化物の形で第2成分として添加したものを用いることができる。特に第1成分/担体の重量比を1〜40%、第2成分/担体の重量比を1〜15%としたアンモニア分解触媒を用いることが好ましい。
また発電装置が、水素ガスにより駆動されるガスエンジンまたは燃料電池であることが好ましい。
As an ammonia decomposition catalyst, nickel or nickel oxide is supported as a first component on a metal oxide carrier such as alumina, silica, titania, zirconia, and at least one of an alkaline earth metal and a lanthanoid element is a metal or What was added as a 2nd component in the form of an oxide can be used. In particular, it is preferable to use an ammonia decomposition catalyst in which the weight ratio of the first component / support is 1 to 40% and the weight ratio of the second component / support is 1 to 15%.
The power generation device is preferably a gas engine or a fuel cell driven by hydrogen gas.
本発明によれば、有機性廃棄物をガス化改質して可燃性ガスを回収することができるのみならず、この工程において排水中へ移行したアンモニアからも水素を回収し、発電装置のエネルギー源として利用することができる。このため有機性廃棄物からのエネルギー回収率が高まるとともに、環境への負担も軽減される。特に上記したアンモニア分解触媒を用いれば、水蒸気の存在下においても触媒活性の低下がなく、アンモニアをほぼ完全に分解して効率よく水素を得ることができる。 According to the present invention, not only the organic waste can be gasified and reformed to recover the combustible gas, but hydrogen is also recovered from the ammonia transferred into the wastewater in this process, and the energy of the power generation apparatus is recovered. Can be used as a source. This increases the energy recovery rate from organic waste and reduces the burden on the environment. In particular, when the above ammonia decomposition catalyst is used, the catalytic activity does not decrease even in the presence of water vapor, and ammonia can be decomposed almost completely and hydrogen can be obtained efficiently.
以下に本発明の実施形態を示す。
図1は本発明の実施形態を示すブロック図であり、1は下水汚泥、バイオマスなどの窒素分を含む有機性廃棄物である。これらの有機性廃棄物1は多くの場合、大量の水分を含有しており、そのまま高温のガス化改質炉4に投入することができないのが普通であるので、脱水機2と乾燥機3とによる脱水・乾燥の前処理が行われる。脱水機2としては、ベルトプレス、フィルタープレス、ロータリープレスなどの従来公知の様々な形式のものを使用することができる。また乾燥機3の形式も任意であるが、例えば外部熱源を利用したパドルドライヤを用いることができる。
Embodiments of the present invention will be described below.
FIG. 1 is a block diagram showing an embodiment of the present invention, where 1 is an organic waste containing nitrogen such as sewage sludge and biomass. In many cases, these organic wastes 1 contain a large amount of moisture and cannot be put into the high-temperature
しかしどのような形式の脱水機2や乾燥機3を使用しても、水分を含んだ有機性廃棄物1を加熱するため、必ず多量の水蒸気が発生すると同時に、有機性廃棄物1が加熱分解されることによってアンモニアが発生する。このアンモニアは水蒸気が凝結した排水(乾燥ドレン)中に必ず移行する。本発明ではこのアンモニアを含むドレン水を排水処理工程5に送る。
However, no matter what type of
一方、脱水・乾燥の前処理が行われた有機性廃棄物は、ガス化改質炉4に送り込まれる。ガス化改質炉4の内部は600〜1400℃の高温に保たれており、外部から酸素・空気・水蒸気が供給されている。有機性廃棄物はガス化改質炉4の内部で部分酸化され、H分とC分はCO,H2等の燃料ガスに変換される。なお、ガス化炉と改質炉とは分離した炉とすることもできる。このガス化改質の工程自体は、前記の特許文献1にも示されているように公知である。
On the other hand, the organic waste that has undergone dehydration / drying pretreatment is sent to the
ガス化改質炉4から出た燃料ガスは、除塵・洗浄工程6においてダスト、S分などの不純物を取り除かれる。このとき、有機性廃棄物中のN分に由来するアンモニアが洗浄排水側に移行する。本発明ではこのアンモニアを高濃度で含む洗浄排水もまた、排水処理工程5に送られる。
From the
本実施形態では、これらのアンモニアを含む排水はストリッピング塔に送られ、公知のアンモニアストリッピング法により、アンモニアをガス中へ放散させる。ストリッピング塔の内部には格子や波板などが充填されており、塔下部から空気または水蒸気が吹き込まれる。アンモニア含有排水は消石灰などによってpHをアルカリ側に調整され、ストリッピング塔の上部から噴霧される。この結果、排水中のNH4OHはNH3とH2Oとに分解され、アンモニアガスのみが塔上部から回収される。このようにして排水中から、アンモニアガスのみを回収することができる。しかし本発明においてアンモニアの回収方法はストリッピング法に限定されるものではなく、吸着剤を用いるなど任意の手段を採ることができる。 In this embodiment, the wastewater containing ammonia is sent to a stripping tower, and ammonia is diffused into the gas by a known ammonia stripping method. The stripping tower is filled with lattices, corrugated plates, etc., and air or water vapor is blown from the bottom of the tower. The ammonia-containing wastewater is adjusted to the alkali side by slaked lime and sprayed from the upper part of the stripping tower. As a result, NH 4 OH in the waste water is decomposed into NH 3 and H 2 O, and only ammonia gas is recovered from the top of the tower. In this way, only ammonia gas can be recovered from the waste water. However, in the present invention, the ammonia recovery method is not limited to the stripping method, and any means such as using an adsorbent can be adopted.
この高濃度のアンモニアガスは、ニッケルベースのアンモニア分解触媒により分解され、N2とH2となる。ここで用いるアンモニア分解触媒は、アルミナ、シリカ、チタニア、ジルコニア等の金属酸化物担体上にニッケルまたはニッケル酸化物を第1成分として担持させ、更にアルカリ土類金属及びランタノイド元素の少なくとも一方を金属または酸化物の形で第2成分として添加したものが好ましい。このアンモニア分解触媒を触媒反応器の内部に充填しアンモニアガスを供給すれば、純粋な水素ガスを効率よく取り出すことができる。このアンモニア分解触媒については、後に詳細に説明する。 This high-concentration ammonia gas is decomposed by a nickel-based ammonia decomposition catalyst into N 2 and H 2 . The ammonia decomposition catalyst used here has nickel or nickel oxide supported as a first component on a metal oxide carrier such as alumina, silica, titania, zirconia, etc., and at least one of an alkaline earth metal and a lanthanoid element is a metal or What was added as a 2nd component in the form of an oxide is preferable. If this ammonia decomposition catalyst is filled in the catalyst reactor and ammonia gas is supplied, pure hydrogen gas can be taken out efficiently. This ammonia decomposition catalyst will be described in detail later.
この水素は、発電装置8のエネルギー源として利用することができる。発電装置8としては例えば燃料電池があり、本発明によれば燃料電池に有害なCOを全く含まない水素ガスが得られるため、有利である。しかし水素を燃料としてガスエンジンを駆動し、発電機を動かすこともできる。この場合にはガスエンジンの排熱はボイラにより回収し、乾燥機3の熱源として使用することができる。また温水として暖房などに利用することもできる。
This hydrogen can be used as an energy source of the
(アンモニア分解触媒の詳細)
本発明で用いるアンモニア分解触媒は、アルミナ、シリカ、チタニア、ジルコニア等の金属酸化物担体上にニッケルまたはニッケル酸化物を第1成分として担持させ、更にアルカリ土類金属及びランタノイド元素の少なくとも一方を金属または酸化物の形で第2成分として添加したものが好ましい。アルカリ土類金属としては、マグネシウム、カルシウム、ストロンチウム、バリウムなどが用いられ、ランタノイド元素としてはランタン、セリウムなどが用いられる。このようなアンモニア分解触媒は、例えば周知の共沈法によりニッケル/アルミナ触媒を製造し、これを乾燥させた後にバリウムなどの第2成分をエタノールや水に溶解させて含浸させる方法で製造することができる。
(Details of ammonia decomposition catalyst)
The ammonia decomposition catalyst used in the present invention has nickel or nickel oxide supported as a first component on a metal oxide support such as alumina, silica, titania, zirconia, etc., and at least one of an alkaline earth metal and a lanthanoid element is a metal. Or what was added as a 2nd component in the form of an oxide is preferable. Magnesium, calcium, strontium, barium and the like are used as the alkaline earth metal, and lanthanum and cerium are used as the lanthanoid element. Such an ammonia decomposition catalyst is manufactured by, for example, manufacturing a nickel / alumina catalyst by a well-known coprecipitation method, and drying and impregnating a second component such as barium in ethanol or water. Can do.
ここで第1成分/担体の重量比は、1〜40%、より好ましくは5〜25%、最も好ましくは10〜20%とする。また第2成分/担体の重量比は、1〜15%、より好ましくは5〜10%、最も好ましくは5〜10%とする。最良の実施形態においては、ニッケル15.7%、バリウム7.36%、残部アルミナである。アンモニア分解触媒の比表面積は、10〜1000m2/g、より好ましくは50〜500m2/g、最も好ましくは100〜300m2/gとする。また触媒粒子径は、10〜1000μm,より好ましくは200〜700μm,最も好ましくは300〜500μmである。 Here, the weight ratio of the first component / carrier is 1 to 40%, more preferably 5 to 25%, and most preferably 10 to 20%. The weight ratio of the second component / carrier is 1 to 15%, more preferably 5 to 10%, and most preferably 5 to 10%. In the best embodiment, nickel 15.7%, barium 7.36%, balance alumina. The specific surface area of the ammonia decomposition catalyst is 10 to 1000 m 2 / g, more preferably 50 to 500 m 2 / g, and most preferably 100 to 300 m 2 / g. The catalyst particle diameter is 10 to 1000 μm, more preferably 200 to 700 μm, and most preferably 300 to 500 μm.
以下に、このアンモニア分解触媒の特性を実験により確認した結果を示す。予備実験によりアンモニア分解触媒は水蒸気の存在下では活性が低下することが確認されているが、実際には水蒸気が存在しない条件でアンモニア分解触媒を使用することは容易ではない。このため以下のグラフは全て水蒸気の存在下におけるアンモニア転化率を示す。なおアンモニア流量は9.1×10−3mol/h,水蒸気/アンモニアの比は5.5×10−2kg・h/molとした。 Below, the result of having confirmed the characteristic of this ammonia decomposition catalyst by experiment is shown. Although it has been confirmed by preliminary experiments that the activity of the ammonia decomposition catalyst decreases in the presence of water vapor, it is not easy to actually use the ammonia decomposition catalyst under conditions where water vapor does not exist. Thus, the following graphs all show ammonia conversion in the presence of water vapor. The ammonia flow rate was 9.1 × 10 −3 mol / h, and the water vapor / ammonia ratio was 5.5 × 10 −2 kg · h / mol.
図2のグラフは、アルミナ担体にニッケルのみを担持させた触媒と、更に第2成分を添加した各種触媒のアンモニア転化率を示すもので、横軸は反応温度である。図2の上段のグラフは第2成分としてアルカリ土類金属を添加したもの、下段のグラフは第2成分としてランタノイド元素を添加したものである。いずれもニッケルに対する添加金属のモル比を0.3とした。これらのグラフに示されるように、第2成分を添加することにより触媒活性が向上することが分かる。特にバリウムを添加した場合に最も優れた結果を示している。 The graph of FIG. 2 shows the ammonia conversion rate of a catalyst in which only nickel is supported on an alumina support and various catalysts to which a second component is further added, and the horizontal axis represents the reaction temperature. The upper graph in FIG. 2 is obtained by adding an alkaline earth metal as the second component, and the lower graph is obtained by adding a lanthanoid element as the second component. In all cases, the molar ratio of the added metal to nickel was set to 0.3. As shown in these graphs, it can be seen that the catalytic activity is improved by adding the second component. In particular, the best results are shown when barium is added.
図3のグラフは、ニッケルに対するバリウムのモル比がアンモニア転化率に及ぼす影響を示すものである。反応温度を450℃とすれば、このモル比が0.1〜0.3の範囲において、水蒸気の存在下においてもアンモニア転化率はほぼ100%に達することが分かる。さらに図4のグラフは、最も活性の高かったニッケルに対するバリウムのモル比が0.2のアンモニア分解触媒について、その経時変化を調べたものである。使用を継続してもアンモニア転化率がほとんど低下しないことが分かる。 The graph of FIG. 3 shows the influence of the molar ratio of barium to nickel on the ammonia conversion. It can be seen that when the reaction temperature is 450 ° C., the ammonia conversion reaches almost 100% even in the presence of water vapor when the molar ratio is in the range of 0.1 to 0.3. Further, the graph of FIG. 4 shows the change over time of the ammonia decomposition catalyst having the highest activity of barium to nickel with a molar ratio of 0.2. It can be seen that even if the use is continued, the ammonia conversion rate hardly decreases.
以上の実験では触媒担体としてアルミナを使用したが、シリカ、チタニア、ジルコニア等を用いることもできる。図5のグラフは、第1成分をニッケル、第2成分をバリウムとし、担体をアルミナ、ジルコニア、チタニアの3種類に変更した場合のそれぞれのアンモニア転化率を示すグラフであり、担体をジルコニアやチタニアに変更してもほぼ同様の結果が得られることを示している。図5には記載されていないが、シリカの場合もほぼ同様である。 In the above experiments, alumina was used as the catalyst carrier, but silica, titania, zirconia, or the like can also be used. The graph of FIG. 5 is a graph showing the ammonia conversion rates when the first component is nickel, the second component is barium, and the carrier is changed to three types of alumina, zirconia, and titania. The carrier is zirconia or titania. This shows that almost the same result can be obtained even when changed to. Although not shown in FIG. 5, the same applies to the case of silica.
上記したように、アルミナ、シリカ、チタニア、ジルコニアから選択された金属酸化物担体上にニッケルまたはニッケル酸化物を第1成分として担持させ、更にアルカリ土類金属及びランタノイド元素の少なくとも一方を金属または酸化物の形で第2成分として添加したアンモニア分解触媒を用いれば、アンモニアをほぼ完全に分解して効率よく水素を得ることができることが確認された。 As described above, nickel or nickel oxide is supported as a first component on a metal oxide support selected from alumina, silica, titania, and zirconia, and at least one of an alkaline earth metal and a lanthanoid element is metal or oxidized. It was confirmed that if ammonia decomposition catalyst added as a second component in the form of a product is used, ammonia can be decomposed almost completely and hydrogen can be obtained efficiently.
以下に図6を参照しつつ、本発明の実施例を説明する。
含水率80%の下水汚泥を、12500kg/hの流量で減圧蒸発式乾燥機10に送り込み脱水乾燥させた。下水汚泥中の水分は10000kg/h、DS(乾燥固形分)は2500kg/hであり、減圧蒸発式乾燥機10から29.6kg/hのアンモニアを含む9870kg/hの乾燥ドレン水が発生した。乾燥ドレン水中のアンモニア濃度は3000mg/Lである。この乾燥ドレン水は排水処理工程5に送られた。
Hereinafter, an embodiment of the present invention will be described with reference to FIG.
Sewage sludge having a water content of 80% was sent to the
脱水乾燥させた下水汚泥は、ガス化炉と改質炉に送られてガス化改質され、発生させたガスはフィルタ11で除塵され、更に洗浄されて5995m3/hの燃料ガスとなった。この燃料ガスはボイラ12とガスエンジン13に送られ、発電に使用した。
The dewatered and dried sewage sludge is sent to a gasification furnace and a reforming furnace to be gasified and reformed. The generated gas is removed by a filter 11 and further washed to become a fuel gas of 5995 m 3 / h. . This fuel gas was sent to the
ガスの洗浄排水中には16.1kg/hのアンモニアが含有されており、この洗浄排水も排水処理工程5に送られた。排水処理工程5では乾燥ドレン水と洗浄排水とを集め、水中に含まれているアンモニアをアンモニアストリッピング法によりガス中へ放散させた。放散させたアンモニア量は45.7kg/hである。このアンモニアを前記したニッケル15.7%、バリウム7.36%、残部アルミナからなる分解触媒により水素と窒素に分解して90m3/hの水素ガスを回収した。その発熱量は275Mcal/hであり、この水素をボイラ12とガスエンジン13に送り発電に使用した。このように、本発明によれば275Mcal/hだけ有機性廃棄物である下水汚泥からのエネルギー回収量が増加したこととなる。
The gas cleaning wastewater contained 16.1 kg / h of ammonia, and this cleaning wastewater was also sent to the
1 有機性廃棄物
2 脱水機
3 乾燥機
4 ガス化改質炉
5 排水処理工程
6 除塵・洗浄工程
7 分解触媒
8 発電装置
10 減圧蒸発式乾燥機
11 フィルタ
12 ボイラ
13 ガスエンジン
DESCRIPTION OF SYMBOLS 1
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JP4605992B2 (en) * | 2003-03-28 | 2011-01-05 | 三井造船株式会社 | Fuel cell power generation process and fuel cell system |
JP4225866B2 (en) * | 2003-09-01 | 2009-02-18 | 株式会社栗本鐵工所 | Organic sludge treatment method |
KR100710911B1 (en) | 2005-12-27 | 2007-04-27 | 류지순 | A electric-power generation equipment use of waste water |
JP4787966B2 (en) * | 2007-03-30 | 2011-10-05 | 国立大学法人群馬大学 | Method for dry treatment of nitrogen-containing waste and apparatus therefor |
JP2010094667A (en) * | 2008-09-17 | 2010-04-30 | Nippon Shokubai Co Ltd | Ammonia-decomposition catalyst, method of producing the same, and method of treating ammonia |
JP5547936B2 (en) * | 2008-09-17 | 2014-07-16 | 株式会社日本触媒 | Ammonia decomposition catalyst, production method thereof, and ammonia treatment method |
WO2010032790A1 (en) * | 2008-09-17 | 2010-03-25 | 株式会社日本触媒 | Catalyst for ammonia decomposition, process for producing same, and method of treating ammonia |
WO2010107065A1 (en) * | 2009-03-17 | 2010-09-23 | 株式会社日本触媒 | Catalyst for production of hydrogen and process for producing hydrogen using the catalyst, and catalyst for combustion of ammonia, process for producing the catalyst, and method for combustion of ammonia using the catalyst |
JP5483705B2 (en) * | 2009-03-17 | 2014-05-07 | 株式会社日本触媒 | Hydrogen production catalyst and hydrogen production method using the same |
JP5624343B2 (en) * | 2009-03-17 | 2014-11-12 | 株式会社日本触媒 | Hydrogen production method |
JP5763890B2 (en) * | 2009-03-17 | 2015-08-12 | 株式会社日本触媒 | Hydrogen production catalyst and hydrogen production method using the same |
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