JP2001137691A - Device for carbon dioxide fixation - Google Patents
Device for carbon dioxide fixationInfo
- Publication number
- JP2001137691A JP2001137691A JP32540999A JP32540999A JP2001137691A JP 2001137691 A JP2001137691 A JP 2001137691A JP 32540999 A JP32540999 A JP 32540999A JP 32540999 A JP32540999 A JP 32540999A JP 2001137691 A JP2001137691 A JP 2001137691A
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- hydrogen
- reaction
- catalyst
- gas
- Prior art date
- Legal status (The legal status 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 status listed.)
- Pending
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 146
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 77
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 72
- 238000006243 chemical reaction Methods 0.000 claims abstract description 128
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 92
- 239000003054 catalyst Substances 0.000 claims abstract description 66
- 239000001257 hydrogen Substances 0.000 claims abstract description 58
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 58
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000007789 gas Substances 0.000 claims abstract description 52
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 32
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 238000000855 fermentation Methods 0.000 claims abstract description 18
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 17
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 16
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 12
- 238000002485 combustion reaction Methods 0.000 claims abstract description 11
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 9
- 230000004151 fermentation Effects 0.000 claims abstract description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 22
- 238000000354 decomposition reaction Methods 0.000 claims description 18
- 239000010815 organic waste Substances 0.000 claims description 11
- 230000003100 immobilizing effect Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 13
- 238000002156 mixing Methods 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 14
- 238000000034 method Methods 0.000 description 6
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910021536 Zeolite Inorganic materials 0.000 description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 4
- 239000010457 zeolite Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 150000001722 carbon compounds Chemical class 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000006229 carbon black Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000011787 zinc oxide Substances 0.000 description 2
- 101100325793 Arabidopsis thaliana BCA2 gene Proteins 0.000 description 1
- XMWRBQBLMFGWIX-UHFFFAOYSA-N C60 fullerene Chemical class C12=C3C(C4=C56)=C7C8=C5C5=C9C%10=C6C6=C4C1=C1C4=C6C6=C%10C%10=C9C9=C%11C5=C8C5=C8C7=C3C3=C7C2=C1C1=C2C4=C6C4=C%10C6=C9C9=C%11C5=C5C8=C3C3=C7C1=C1C2=C4C6=C2C9=C5C3=C12 XMWRBQBLMFGWIX-UHFFFAOYSA-N 0.000 description 1
- 102100033007 Carbonic anhydrase 14 Human genes 0.000 description 1
- 101000867862 Homo sapiens Carbonic anhydrase 14 Proteins 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 102100031083 Uteroglobin Human genes 0.000 description 1
- 108090000203 Uteroglobin Proteins 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- CXKCTMHTOKXKQT-UHFFFAOYSA-N cadmium oxide Inorganic materials [Cd]=O CXKCTMHTOKXKQT-UHFFFAOYSA-N 0.000 description 1
- CFEAAQFZALKQPA-UHFFFAOYSA-N cadmium(2+);oxygen(2-) Chemical compound [O-2].[Cd+2] CFEAAQFZALKQPA-UHFFFAOYSA-N 0.000 description 1
- 239000002134 carbon nanofiber Substances 0.000 description 1
- 229910021393 carbon nanotube Inorganic materials 0.000 description 1
- 239000002041 carbon nanotube Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 229910003472 fullerene Inorganic materials 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- DALYXJVFSIYXMA-UHFFFAOYSA-N hydrogen sulfide dimer Chemical compound S.S DALYXJVFSIYXMA-UHFFFAOYSA-N 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 229910000464 lead oxide Inorganic materials 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- YEXPOXQUZXUXJW-UHFFFAOYSA-N oxolead Chemical compound [Pb]=O YEXPOXQUZXUXJW-UHFFFAOYSA-N 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
- Y02W10/20—Sludge processing
-
- 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
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、大気中又は工場等
の排煙中に含まれる二酸化炭素を他の物質に変換して回
収する二酸化炭素固定化装置、下水道処理、生ゴミ処
理、家畜廃棄物処理などの環境制御分野一般、カーボン
ブラック等の炭素化合物製造分野に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a carbon dioxide fixing device for converting carbon dioxide contained in the air or in flue gas from factories or the like into other substances and recovering the same, sewerage treatment, garbage disposal, livestock disposal. The present invention relates to the general field of environmental control such as material treatment, and the field of manufacturing carbon compounds such as carbon black.
【０００２】[0002]
【従来の技術】工場、発電所、自動車等から大気中に排
出される二酸化炭素（ＣＯ２）は地球温暖化の主たる原
因であることが知られており、近年、このＣＯ２の排出
量を削減することが地球環境の保護の大きな課題となっ
ている。これに対し、従来より工場等の排煙や大気中の
ＣＯ２を固定化し除去するためのシステムが種々提案さ
れている。BACKGROUND ART Plant, plant, carbon dioxide discharged from an automobile or the like in the atmosphere (CO 2) is known to be a major cause of global warming, in recent years, emissions of CO 2 Reduction is a major issue in protecting the global environment. On the other hand, conventionally, various systems for fixing and removing flue gas from factories and the like and CO 2 in the atmosphere have been proposed.
【０００３】ＣＯ２を固定して再資源化する方法の一つ
に、例えば水素（Ｈ２）雰囲気下でＣＯ２を還元し、微
粉状の炭素に変換する方法が考案されている。その変換
方式は、大気や排ガス中からＣＯ２を分離するＣＯ２分
離装置、その分離されたＣＯ ２を濃縮するＣＯ２濃縮装
置、ＣＯ２とＨ２を触媒の存在下で反応させて微粉状炭
素を生成するＣＯ２／Ｈ２反応装置などから構成されて
いる。[0003] CO2Method of fixing and recycling resources
For example, hydrogen (H2) CO under atmosphere2To reduce
Methods have been devised for conversion to powdered carbon. That conversion
The method uses CO from air or exhaust gas.2To separate CO2Minute
Separation device, the separated CO 2To concentrate CO2Concentrating equipment
Place, CO2And H2Is reacted in the presence of a catalyst to remove pulverized coal.
CO that generates elementary2/ H2It consists of a reaction device
I have.
【０００４】[0004]
【発明が解決しようとする課題】上記装置では、二酸化
炭素固定化に必要なＨ２は外部から供給する必要があ
る。Ｈ２は主に水の電気分解により生成されるが、大き
な電力を消費するため、電力コストが高く運転コストが
大変高いものとなる。また、電力を得るためのもっとも
一般的な方法は火力発電であるが、火力発電では石油、
石炭、ＬＮＧ等の化石燃料を燃焼して大量のＣＯ２ガス
を排出するため、総合的なＣＯ２の削減効果は高くでき
ないというジレンマがある。この水素生成における高コ
スト問題を解決するため、有機廃棄物を嫌気性発酵する
ことによりメタンガス（ＣＨ４）を安価に製造し、この
ＣＨ４の分解によるＨ２の入手方法が提案されている。
しかしながら、ＣＨ４を分解しＨ２を製造する場合、そ
の分解反応は（１）式で示されるように吸熱反応であ
り、Ｈ２を製造するためには常に熱を供給する必要があ
る。 ＣＨ４→Ｃ＋２Ｈ２＋９０．１ｋＪ／ｍｏｌ――――――（１） ＣＯ２＋２Ｈ２→Ｃ＋２Ｈ２Ｏ−９６．０ｋＪ／ｍｏｌ――（２） また、二酸化炭素固定化反応は（２）式で示されるよう
に、発熱反応であるが、この反応は４００℃以上の温度
で進行するため、反応を開始させるための初期過程にお
いては熱の供給が必要である。このため、メタン分解反
応が生じる反応槽および二酸化炭素固定化反応が生じる
反応槽へ外部から熱を供給しなければならない。この熱
は原料ガスとしてＨ２もしくはＣＨ４を用い、これらを
燃焼させることにより供給されるが、原料ガスおよび熱
供給のための配管系統が複雑になり、装置製造コスト高
の一因になっている。さらに、外部でＨ２またはＣＨ４
を燃焼する場合、専用の燃焼器やコンプレッサなどが必
要になる。In the above apparatus, H 2 required for immobilizing carbon dioxide must be supplied from the outside. While H 2 is mainly generated by the electrolysis of water, to consume large power, it becomes the very high high operating costs power cost. Also, the most common method of obtaining electricity is thermal power generation, but thermal power generation uses oil,
There is a dilemma in that fossil fuels such as coal and LNG are burned to emit a large amount of CO 2 gas, so that the overall CO 2 reduction effect cannot be high. Therefore to solve the high cost problem in a hydrogen generating, organic waste methane gas (CH 4) was manufactured at low cost by anaerobic fermentation, how to obtain H 2 due to decomposition of the CH 4 it has been proposed.
However, when H 2 is produced by decomposing CH 4 , the decomposition reaction is an endothermic reaction as shown by the formula (1), and heat must always be supplied to produce H 2 . CH 4 → C + 2H 2 +90.1 kJ / mol --- (1) CO 2 + 2H 2 → C + 2H 2 O-96.0 kJ / mol --- (2) Further, the carbon dioxide fixing reaction is represented by formula (2). Is an exothermic reaction, as shown in FIG. 1, the reaction proceeds at a temperature of 400 ° C. or higher, so that heat needs to be supplied in an initial step for starting the reaction. For this reason, heat must be supplied from the outside to the reaction tank where the methane decomposition reaction occurs and the reaction tank where the carbon dioxide fixing reaction occurs. This heat is supplied by using H 2 or CH 4 as a raw material gas and burning it. However, a piping system for supplying the raw material gas and the heat becomes complicated, which contributes to an increase in apparatus manufacturing cost. I have. In addition, H 2 or CH 4
When burning, a dedicated combustor and compressor are required.
【０００５】有機廃棄物を嫌気性発酵することによりメ
タンガスを製造する場合、発生したＣＨ４中には窒素ガ
スと硫化水素ガスが多量に含まれている。これらのガス
はメタン分解・水素生成反応および二酸化炭素固定化反
応を阻害し、装置の稼働効率を低下させる原因となって
いる。また、硫化水素ガスは非常な悪臭を有しており、
装置周囲の環境を悪化させている。[0005] When producing the methane gas by organic waste to anaerobic fermentation, generated during CH 4 nitrogen gas hydrogen sulfide gas is contained in a large amount. These gases hinder the methane decomposition / hydrogen production reaction and the carbon dioxide fixation reaction, and cause a reduction in the operation efficiency of the apparatus. Also, hydrogen sulfide gas has a very bad smell,
The environment around the device is getting worse.
【０００６】ＣＯ２とＨ２を触媒の存在下で反応させて
微粉状炭素を生成する二酸化炭素固定化のための反応槽
においては、固定化される炭素は触媒表面上にひげ状に
生成するため、生成した炭素微粉末を反応槽外に取り除
くためには、この触媒表面にひげ状についた炭素と触媒
とを一旦反応槽の外部に取り出し、炭素と触媒を分離し
た後、触媒を反応槽に戻す必要がある。この操作は非常
に煩雑であるとともに、高価な炭素・触媒分離器を必要
とし、装置製造コストおよびランニングコスト高の原因
となっている。[0006] In a reaction tank for carbon dioxide fixation in which CO 2 and H 2 are reacted in the presence of a catalyst to produce fine carbon powder, the carbon to be fixed is formed in a whisker-like form on the catalyst surface. Therefore, in order to remove the generated carbon fine powder out of the reaction tank, the beard-like carbon on the catalyst surface and the catalyst are once taken out of the reaction tank, and after separating the carbon and the catalyst, the catalyst is removed from the reaction tank. Must be returned to This operation is very complicated, requires an expensive carbon / catalyst separator, and causes an increase in apparatus manufacturing cost and running cost.
【０００７】メタン分解・水素生成反応と二酸化炭素固
定化反応は別々の二つの反応槽で行われているが、メタ
ン分解・水素生成反応は（１）式で示されるように吸熱
反応であり、一方、二酸化炭素固定化反応は（２）式で
示されるように発熱反応である。従来の二酸化炭素固定
化装置ではメタン分解・水素生成用の反応槽には熱を供
給しなければならず、二酸化炭素固定化用の反応槽では
反応により得られる熱を有効利用するための熱交換機が
設けられている。従って、二つの反応槽に必要な配管系
統が複雑になり、装置製造コスト上昇の原因となってい
る。さらに、これらの反応を分離して行うことは熱効率
の点から考えると明らかに不利である。[0007] The methane decomposition / hydrogen production reaction and the carbon dioxide fixation reaction are performed in two separate reaction tanks, but the methane decomposition / hydrogen production reaction is an endothermic reaction as shown in equation (1). On the other hand, the carbon dioxide fixing reaction is an exothermic reaction as shown by the equation (2). In conventional carbon dioxide fixation equipment, heat must be supplied to the reaction tank for methane decomposition and hydrogen generation, and in the reaction tank for carbon dioxide fixation, a heat exchanger is used to make effective use of the heat obtained by the reaction. Is provided. Therefore, a piping system required for the two reaction tanks is complicated, which causes an increase in device manufacturing cost. Furthermore, performing these reactions separately is clearly disadvantageous in terms of thermal efficiency.
【０００８】そこで、本発明は、従来の技術の有する上
記問題点に鑑みてなされたものであって、熱効率が高
く、構造の簡単な、製造コストおよびランニングコスト
を低減できる二酸化炭素固定化装置を提供することを目
的とする。In view of the above, the present invention has been made in view of the above-mentioned problems of the prior art, and has an object to provide a carbon dioxide fixing device having high thermal efficiency, a simple structure, and capable of reducing manufacturing costs and running costs. The purpose is to provide.
【０００９】[0009]
【課題を解決するための手段】上記課題を解決するため
に本発明における二酸化炭素固定化装置は、有機廃棄物
を嫌気性発酵することによりメタンガスを生成する発酵
手段と、該メタンガスを分解して水素を取り出す水素生
成手段と、該水素ガスと二酸化炭素ガスとの化学反応に
より固体炭素を生成する二酸化炭素固定手段と、を有す
る二酸化炭素固定化装置であって、二酸化炭素固定化反
応が生じる反応槽内に二酸化炭素固定化用触媒と水素燃
焼用触媒を充填したものである。二酸化炭素固定化反応
を開始させるためには、反応槽内を４００℃以上に加熱
しなければならず、反応槽に熱を供給する必要がある
が、本発明においては、水素の一部を反応槽内に充填し
た水素燃焼用触媒上で燃焼させることにより、二酸化炭
素固定化反応開始に必要な熱を発生させ、反応槽外部か
らの熱の供給を不要とすることができる。これにより、
熱供給のための燃焼器、コンプレッサーやこれらに伴う
配管が不要となり、装置の簡素化が可能となる。Means for Solving the Problems In order to solve the above-mentioned problems, a carbon dioxide fixing device according to the present invention comprises a fermentation means for producing methane gas by anaerobic fermentation of organic waste, and a method for decomposing the methane gas. A carbon dioxide fixing device comprising: hydrogen generating means for extracting hydrogen; and carbon dioxide fixing means for generating solid carbon by a chemical reaction between the hydrogen gas and carbon dioxide gas, wherein a reaction in which the carbon dioxide fixing reaction occurs The tank is filled with a catalyst for fixing carbon dioxide and a catalyst for burning hydrogen. In order to start the carbon dioxide fixation reaction, the inside of the reaction tank must be heated to 400 ° C. or higher, and it is necessary to supply heat to the reaction tank. By burning on the hydrogen combustion catalyst filled in the tank, the heat required for starting the carbon dioxide fixing reaction is generated, and the supply of heat from outside the reaction tank can be eliminated. This allows
A combustor, a compressor for supplying heat, and piping associated therewith are not required, and the apparatus can be simplified.
【００１０】さらに、有機廃棄物を嫌気性発酵すること
によりメタンガスを製造する際にメタンガス中に含まれ
る窒素および硫化水素ガスを、二酸化炭素固定化反応が
生じる反応槽の前段で分離する手段を設けたものであ
る。メタンガスが反応槽に導入される前に窒素および硫
化水素ガスを分離しておくことにより、反応槽内での二
酸化炭素固定化反応を阻害する要因をあらかじめ取り除
くことができ、装置全体の稼働効率を上昇させることが
可能となる。Further, means is provided for separating nitrogen and hydrogen sulfide gas contained in methane gas at the stage preceding the reaction tank in which the carbon dioxide fixation reaction takes place when methane gas is produced by anaerobic fermentation of organic waste. It is a thing. By separating nitrogen and hydrogen sulfide gas before methane gas is introduced into the reaction tank, it is possible to remove factors that hinder the carbon dioxide fixation reaction in the reaction tank in advance, and to improve the operating efficiency of the entire system. It can be raised.
【００１１】また、二酸化炭素固定化のための反応槽
に、二酸化炭素固定化用触媒の表面に生成する固体状炭
素を分離できる剥離剤を、二酸化炭素固定化用触媒と混
合して充填したものである。剥離剤を混合しておくこと
により、生成した炭素微粉末を反応槽外に取り除くため
の高価な炭素／触媒分離器を必要とせず、装置製造コス
トを削減することができる。さらに、炭素と触媒とを一
旦反応槽の外部に取り出し、炭素と触媒を分離した後、
触媒を反応槽に戻すという煩雑な操作も不要となり、ラ
ンニングコストの低減を可能とする。[0011] Further, a reaction vessel for immobilizing carbon dioxide is filled with a release agent capable of separating solid carbon generated on the surface of the catalyst for immobilizing carbon dioxide, mixed with the catalyst for immobilizing carbon dioxide. It is. By mixing the release agent, an expensive carbon / catalyst separator for removing the generated carbon fine powder out of the reaction tank is not required, and the manufacturing cost of the apparatus can be reduced. Furthermore, after the carbon and the catalyst are once taken out of the reaction tank and the carbon and the catalyst are separated,
The complicated operation of returning the catalyst to the reaction tank is not required, and the running cost can be reduced.
【００１２】さらに、メタン分解・水素生成用触媒と二
酸化炭素固定化用触媒を一つの反応槽内に充填したもの
である。これら２種類の触媒を適当量混合し、吸熱反応
であるメタン分解・水素生成反応と、発熱反応である二
酸化炭素固定化反応とを一つの反応槽内で行わせること
で、メタン分解・水素生成反応に必要な熱量を二酸化炭
素固定化反応で発生する熱量で供給可能となる。これに
より反応槽が一つになり、反応槽に必要であった熱供
給、熱回収のための配管系が不要となり、装置製造コス
トを削減することができる。また、装置の保守、点検が
非常に容易となる。さらに、二酸化炭素固定化反応で発
生する熱をほぼ１００％有効利用することが可能にな
り、ランニングコストの低減がはかれる。Further, a catalyst for methane decomposition / hydrogen generation and a catalyst for immobilizing carbon dioxide are filled in one reaction vessel. An appropriate amount of these two types of catalysts are mixed, and the endothermic reaction of methane decomposition and hydrogen generation and the exothermic reaction of carbon dioxide fixation are performed in a single reaction tank, thereby decomposing methane and generating hydrogen. The amount of heat required for the reaction can be supplied by the amount of heat generated in the carbon dioxide fixing reaction. As a result, the number of the reaction tanks becomes one, and a piping system for heat supply and heat recovery required for the reaction tanks is not required, so that the apparatus manufacturing cost can be reduced. Further, maintenance and inspection of the device become very easy. Further, it is possible to effectively use almost 100% of the heat generated in the carbon dioxide fixing reaction, thereby reducing the running cost.
【００１３】本発明の二酸化炭素固定化装置は上記のよ
うに構成されており、配管系統および反応槽の簡素化、
反応熱の有効利用等が可能となり、装置の製造コストお
よびランニングコストを低減することができる。The carbon dioxide fixing apparatus of the present invention is configured as described above, and simplifies the piping system and the reaction tank.
The reaction heat can be effectively used, and the manufacturing cost and running cost of the apparatus can be reduced.
【００１４】[0014]
【発明の実施の形態】図１は、本発明のメタン発酵を利
用した二酸化炭素固定化装置の一実施例を示している。DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 shows an embodiment of the carbon dioxide immobilization apparatus using methane fermentation of the present invention.
【００１５】本実施例の二酸化炭素固定化装置は、生ゴ
ミなどの有機廃棄物を嫌気性発酵槽で細菌によって分解
しＣＨ４を発生させるメタン発酵槽２、硫化水素分離部
４、窒素分離部６、水素発生および二酸化炭素固定化反
応が起こる反応槽８、熱交換器１８、凝縮器２０、水素
分離器２２および燃料電池２４を備えている。反応槽８
内部には邪魔板１０、メタン分解・水素生成反応のため
の触媒と二酸化炭素固定化反応のための触媒および剥離
剤が混合された触媒１２、焼結板１４および水素燃焼用
の触媒１６が配置されている。[0015] Carbon dioxide fixation device of this embodiment, methane fermentation tank 2 for generating a decomposition CH 4 by bacteria of organic waste such as garbage by anaerobic fermentation tank, hydrogen sulfide separation unit 4, a nitrogen separation unit 6, a reaction tank 8 in which hydrogen generation and a carbon dioxide fixing reaction occur, a heat exchanger 18, a condenser 20, a hydrogen separator 22, and a fuel cell 24. Reaction tank 8
Inside, a baffle plate 10, a catalyst 12 in which a catalyst for methane decomposition / hydrogen generation reaction, a catalyst for carbon dioxide fixing reaction and a stripping agent are mixed, a sintered plate 14, and a catalyst 16 for hydrogen combustion are arranged. Have been.
【００１６】有機廃棄物をメタン細菌などの細菌と共に
メタン発酵槽２に導入し、有機廃棄物の嫌気性発酵によ
って、ＣＨ４やＣＯ２を含むガスを生じさせる。その発
生ガス中には、主生成物であるＣＨ４の他に窒素ガス、
硫化水素ガスが含まれており、まずこの発生ガスは硫化
水素分離部４に送られる。硫化水素分離部は内部に酸化
亜鉛（ＺｎＯ）が充填されており、（３）式で示される
反応により硫化水素を吸着することにより発生ガス中の
硫化水素を除去する。 Ｈ２Ｓ＋ＺｎＯ→ＺｎＳ＋Ｈ２Ｏ――――――（３） さらに、硫化水素を除去された発生ガスは窒素分離部６
へ送られる。窒素分離部６内部にはゼオライトが充填さ
れており、ゼオライトの分子篩い作用により、二酸化炭
素、メタン、窒素の混合ガスから窒素を分離する。ここ
で、窒素ガス分離に使用可能なゼオライトとしては、Ｃ
ａ−、Ｂａ−モルデナイト等がある。The organic waste is introduced into the methane fermentation tank 2 together with bacteria such as methane bacteria, and gas containing CH 4 and CO 2 is generated by anaerobic fermentation of the organic waste. The generated gas contains nitrogen gas in addition to the main product CH 4 ,
Hydrogen sulfide gas is contained, and this generated gas is first sent to the hydrogen sulfide separation unit 4. The hydrogen sulfide separation section is filled with zinc oxide (ZnO), and removes the hydrogen sulfide in the generated gas by adsorbing the hydrogen sulfide by the reaction represented by the formula (3). H 2 S + ZnO → ZnS + H 2 O (3) Further, the generated gas from which hydrogen sulfide has been removed is supplied to the nitrogen separation unit 6.
Sent to The inside of the nitrogen separation section 6 is filled with zeolite, and nitrogen is separated from a mixed gas of carbon dioxide, methane, and nitrogen by the molecular sieving action of zeolite. Here, the zeolite usable for nitrogen gas separation is C
a- and Ba-mordenite.
【００１７】メタン発酵槽２で発生したガスは硫化水素
分離部４および窒素分離部６で硫化水素ガスおよび窒素
ガスを取り除かれた後、反応槽８下部に導入される。反
応槽８には固定化されるＣＯ２および水素分離器２２か
ら供給されるＨ２も下部から導入される。導入されたＣ
Ｈ４は触媒１２により分解され水素を生成する。この分
解反応は（１）式で示したように吸熱反応であり、熱を
供給する必要がある。本発明ではこの熱を、水素分離器
２２から供給されるＨ２を触媒１６上で燃焼させること
によって得るものである。触媒１６としては、例えばＡ
ｌ２Ｏ３を担体とするＰｔ、Ａｕなどを用いることがで
き、反応槽８内にマット状に充填される。水素の燃焼反
応は（４）式で表される。 Ｈ２＋１／２Ｏ２→Ｈ２Ｏ−２８５ｋＪ／ｍｏｌ―――――（４） この水素の燃焼により反応槽８全体の温度を上昇させる
ことができ、メタン分解・水素生成反応を進行させるこ
とができる。ここで得られたＨ２を用いて、（２）式で
示される二酸化炭素固定化反応が触媒１２上で進行する
が、この二酸化炭素固定化反応は４００℃以上で進行す
るものであり、反応を開始させるためには触媒１２を４
００℃以上に加熱しなければならない。本発明ではこの
加熱に必要な熱も、触媒１６上での水素の燃焼反応から
得るものであり、反応槽８には反応槽外部から熱を供給
する必要がない。触媒１２としては、例えばＳｉＯ２や
Ａｌ ２Ｏ３を担体とするＮｉ、Ｃｏなどを用いることが
でき、通気性を有する焼結板上に層状に配置されてい
る。The gas generated in the methane fermenter 2 is hydrogen sulfide
Hydrogen sulfide gas and nitrogen in the separation section 4 and the nitrogen separation section 6
After the gas is removed, it is introduced into the lower part of the reaction tank 8. Anti
CO fixed in the tank 82And hydrogen separator 22
H supplied from2Is also introduced from the bottom. Introduced C
H4Is decomposed by the catalyst 12 to generate hydrogen. This minute
The dissolution reaction is an endothermic reaction as shown in equation (1),
Need to supply. In the present invention, this heat is
H supplied from 222Burning on the catalyst 16
Is gained by: As the catalyst 16, for example, A
l2O3Can be used as a carrier such as Pt, Au, etc.
Then, the reaction tank 8 is filled in a mat shape. Anti-hydrogen combustion
The response is expressed by equation (4). H2+ 1 / 2O2→ H2O-285 kJ / mol --- (4) The temperature of the entire reaction vessel 8 is increased by the combustion of the hydrogen.
To promote the methane decomposition and hydrogen production reactions.
Can be. H obtained here2And using equation (2)
The indicated carbon dioxide fixation reaction proceeds on catalyst 12.
However, this carbon dioxide fixing reaction proceeds at 400 ° C. or higher.
In order to start the reaction, 4
Must be heated above 00 ° C. In the present invention,
The heat required for heating is also derived from the combustion reaction of hydrogen on the catalyst 16.
Heat is supplied to the reaction tank 8 from outside the reaction tank.
No need to do. As the catalyst 12, for example, SiO 22And
Al 2O3Using Ni, Co, etc., as a carrier
Can be arranged in layers on a sintered plate with air permeability.
You.
【００１８】メタン分解・水素生成反応および二酸化炭
素固定化反応で生成した炭素粉末は触媒１２中に混合さ
れている剥離剤により触媒１２から剥離されるが、この
遊離した炭素粉末は飛散しやすく、反応槽８の後段へと
運ばれ、パイプの目詰まり等のトラブルの原因となる。
本発明ではこのようなトラブルを防止するため、反応槽
８内に邪魔板１０を設置している。邪魔板１０により遊
離した炭素粉末は反応槽８の外部へ飛散することはな
く、すべて回収される。また、触媒１２中に剥離剤を混
合した結果、生成した炭素粉末を触媒から分離するため
の炭素・触媒分離器を必要とせず、反応器８内から容易
に炭素粉末を回収することができる。The carbon powder produced by the methane decomposition / hydrogen generation reaction and the carbon dioxide fixation reaction is separated from the catalyst 12 by the release agent mixed in the catalyst 12, but the released carbon powder is easily scattered. It is carried to the latter stage of the reaction tank 8 and causes a trouble such as clogging of a pipe.
In the present invention, a baffle plate 10 is provided in the reaction tank 8 in order to prevent such a trouble. The carbon powder released by the baffle plate 10 does not scatter to the outside of the reaction tank 8 and is all recovered. Further, as a result of mixing the stripping agent in the catalyst 12, a carbon / catalyst separator for separating the generated carbon powder from the catalyst is not required, and the carbon powder can be easily recovered from the reactor 8.
【００１９】反応槽８で生成した混合ガスは熱交換器１
８を通り、凝縮器２０に導入される。熱交換器１８にお
いて高温の混合ガスは降温され、この際に混合ガスから
得られる熱は熱交換器１８に蓄えられる。混合ガス中の
水蒸気は凝縮器２０で水となり、系外へ排出される。水
蒸気を取り除かれた混合ガスはさらに水素分離器２２に
導入される。水素分離器２２において、混合ガス中に含
まれる水素が分離精製され、この水素ガスは一部は燃料
電池２４に導入され電力として蓄えられ、一部は水素燃
焼用の水素として反応槽８に導入される。水素分離器２
２には、水素分子を選択的に透過させる透過膜を利用す
る、あるいは水素分子を選択的に吸着する吸着剤を利用
する等の、周知の種々の方法を用いることができる。残
りの排ガスである未反応の二酸化炭素およびメタンは熱
交換器１８へと運ばれ、熱交換器１８で蓄えられた熱に
より昇温された後、再び反応槽８に循環される。The mixed gas generated in the reaction tank 8 is supplied to the heat exchanger 1
8 and is introduced into the condenser 20. The temperature of the high-temperature mixed gas is lowered in the heat exchanger 18, and the heat obtained from the mixed gas at this time is stored in the heat exchanger 18. Water vapor in the mixed gas becomes water in the condenser 20 and is discharged out of the system. The mixed gas from which the water vapor has been removed is further introduced into the hydrogen separator 22. In the hydrogen separator 22, hydrogen contained in the mixed gas is separated and purified, and a part of this hydrogen gas is introduced into the fuel cell 24 and stored as electric power, and a part is introduced into the reaction tank 8 as hydrogen for hydrogen combustion. Is done. Hydrogen separator 2
Various well-known methods, such as using a permeable membrane that selectively permeates hydrogen molecules or using an adsorbent that selectively adsorbs hydrogen molecules, can be used for 2. The remaining unreacted carbon dioxide and methane, which are the exhaust gas, are carried to the heat exchanger 18, heated up by the heat stored in the heat exchanger 18, and circulated again to the reaction tank 8.
【００２０】二酸化炭素固定化反応は発熱反応であり、
一旦反応が開始すれば熱の供給は必要でなく、逆に生成
する熱をメタン分解・水素生成反応に利用することがで
きる。触媒１２に混合されるメタン分解・水素生成反応
用触媒と二酸化炭素固定化反応用触媒の混合量を適当に
調整し、さらに反応槽８に供給される水素ガスの量を調
整することで触媒１６上において水素ガスの燃焼により
発生する熱量を適当に調節することにより、メタン分解
・水素生成反応に必要な熱を、反応槽８外部より供給す
ること無しに、過不足無く発生させることが可能にな
り、理想的な熱効率が実現でき、ランニングコストの低
減が可能になる。The carbon dioxide fixing reaction is an exothermic reaction,
Once the reaction starts, it is not necessary to supply heat. Conversely, the generated heat can be used for the methane decomposition / hydrogen production reaction. By appropriately adjusting the mixing amount of the catalyst for the methane decomposition / hydrogen production reaction and the catalyst for the carbon dioxide fixing reaction mixed in the catalyst 12, and further adjusting the amount of hydrogen gas supplied to the reaction tank 8, the catalyst 16 By appropriately adjusting the amount of heat generated by the combustion of hydrogen gas above, it is possible to generate the heat required for the methane decomposition / hydrogen production reaction without excess or deficiency without supplying it from outside the reaction tank 8. Therefore, ideal thermal efficiency can be realized, and running costs can be reduced.
【００２１】反応槽８から排出される反応ガスを熱交換
器１８、凝縮器２０および水素分離器２８に送った後、
再び反応槽８に循環させることにより、混合ガス中のＣ
Ｏ２をすべて炭素と水に変換でき、外部に一切のＣＯ２
を排出しないことが可能となる。After the reaction gas discharged from the reaction tank 8 is sent to the heat exchanger 18, the condenser 20 and the hydrogen separator 28,
By circulating again in the reaction tank 8, C in the mixed gas
All O 2 can be converted to carbon and water, and no external CO 2
Is not discharged.
【００２２】反応槽８で生成し分離された炭素は工業用
カーボンブラックとして使用することができ、廃棄物を
有用物質に変換することが可能であり、資源の節約に貢
献することができる。The carbon generated and separated in the reaction tank 8 can be used as industrial carbon black, and can convert waste into useful substances, contributing to resource saving.
【００２３】以上、本発明の実施例を説明したが、本発
明は上記実施例に限定されるものではなく、特許請求範
囲に記載された本発明の要旨の範囲内で種々の変更を行
うことができる。例えば、硫化水素分離部４で使用され
る充填剤としては、酸化亜鉛の他にも常温で硫化水素ガ
スと反応して硫化物を生成する化合物であれば良く、酸
化鉛、酸化カドミウム等を用いることができる。さら
に、窒素分離部６で使用される充填剤としては、ゼオラ
イトの他にも適当なサイズの細孔を有し分子篩い作用を
示す材料であれば良く、多孔質シリカ等を用いることが
できる。また、触媒１２に混合される二酸化炭素固定化
反応用触媒としてＮｉ−ＳｉＯ２を用いることにより、
カーボンナノチューブ、カーボンナノファイバー、フラ
ーレン等の付加価値の高い炭素化合物を生成することを
ができる。上記触媒には第３成分としてＰｔ、Ｌａ、Ｃ
ｅ、Ｋ等を添加してもよい。Although the embodiments of the present invention have been described above, the present invention is not limited to the above-described embodiments, and various changes may be made within the scope of the present invention described in the appended claims. Can be. For example, the filler used in the hydrogen sulfide separation unit 4 may be any compound other than zinc oxide that reacts with hydrogen sulfide gas at room temperature to generate a sulfide, such as lead oxide or cadmium oxide. be able to. The filler used in the nitrogen separation section 6 may be any material other than zeolite as long as it has pores of an appropriate size and exhibits a molecular sieving action, and porous silica or the like can be used. Further, by using Ni—SiO 2 as a catalyst for a carbon dioxide fixing reaction mixed with the catalyst 12,
High value-added carbon compounds such as carbon nanotubes, carbon nanofibers and fullerenes can be produced. The catalyst contains Pt, La, C as a third component.
e, K and the like may be added.
【００２４】[0024]
【発明の効果】以上説明したように、本発明に係る二酸
化炭素固定化装置は次のような効果を有している。 （１）二酸化炭素固定化反応が生じる反応槽内に二酸化
炭素固定化用触媒と水素燃焼用触媒を充填することによ
り、二酸化炭素固定化反応開始に必要な熱を水素燃焼用
触媒上で水素ガスを燃焼させることにより発生させ、反
応槽外部からの熱の供給を不要とすることができ、装置
の簡素化が可能となる。 （２）有機廃棄物を嫌気性発酵することによりメタンガ
スを製造する際にメタンガス中に含まれる窒素および硫
化水素ガスを反応槽の前段で分離する手段を有すること
により、反応槽内での二酸化炭素固定化反応を阻害する
要因を取り除くことができ、装置全体の稼働効率を上昇
させることが可能となる。 （３）反応槽に、二酸化炭素固定化用触媒の表面に生成
する固体状炭素を分離できる剥離剤を、二酸化炭素固定
化用触媒と混合して充填することにより、炭素／触媒分
離器を必要とせず、装置製造コストを削減することがで
きる。 （４）反応槽内に邪魔板を設置することにより、生成す
る炭素粉末の飛散を防止することができ、炭素粉末の回
収を容易にする。 （５）メタン分解・水素生成用触媒と二酸化炭素固定化
用触媒を一つの反応槽内に充填することにより、二酸化
炭素固定化反応で発生する熱を有効利用することが可能
になり、ランニングコストの低減がはかれる。さらに、
反応槽が一つになり、反応槽に必要であった熱供給、熱
回収のための配管系が不要となり、装置製造コストを削
減することができる。 （６）有用な炭素化合物を副製品として得ることができ
る。As described above, the carbon dioxide fixing device according to the present invention has the following effects. (1) By filling a reaction vessel in which a carbon dioxide fixation reaction takes place with a carbon dioxide fixation catalyst and a hydrogen combustion catalyst, the heat required for starting the carbon dioxide fixation reaction is converted into hydrogen gas on the hydrogen combustion catalyst. Is generated by burning, and supply of heat from the outside of the reaction tank is not required, and the apparatus can be simplified. (2) When methane gas is produced by anaerobic fermentation of organic waste, a means for separating nitrogen and hydrogen sulfide gas contained in the methane gas at a stage prior to the reaction tank is provided. Factors that hinder the immobilization reaction can be removed, and the operating efficiency of the entire device can be increased. (3) A carbon / catalyst separator is required by filling the reaction tank with a release agent capable of separating solid carbon generated on the surface of the carbon dioxide fixing catalyst mixed with the carbon dioxide fixing catalyst. The manufacturing cost of the apparatus can be reduced. (4) By disposing a baffle plate in the reaction tank, the generated carbon powder can be prevented from being scattered, and the recovery of the carbon powder is facilitated. (5) By filling a catalyst for methane decomposition / hydrogen generation and a catalyst for carbon dioxide fixation in one reaction vessel, it is possible to effectively use the heat generated in the carbon dioxide fixation reaction, and to reduce running costs. Is reduced. further,
The reaction tank becomes one, and a piping system for heat supply and heat recovery required for the reaction tank becomes unnecessary, so that the apparatus manufacturing cost can be reduced. (6) A useful carbon compound can be obtained as a by-product.
【図１】本発明の二酸化炭素固定化装置の実施例の全体
構成図である。FIG. 1 is an overall configuration diagram of an embodiment of a carbon dioxide fixing device of the present invention.
２---メタン発酵槽 ４---硫化水素分離部 ６---窒素分離部 ８---反応槽 １０---邪魔板 １２、１６---触媒 １４---焼結板 １８---熱交換器 ２０---凝縮器 ２２---水素分離器 ２４---燃料電池 2 --- Methane fermentation tank 4 --- Hydrogen sulfide separation unit 6 --- Nitrogen separation unit 8 --- Reaction tank 10 --- Baffle plate 12, 16 --- Catalyst 14 --- Sintered plate 18- --Heat exchanger 20 --- Condenser 22 --- Hydrogen separator 24 --- Fuel cell
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D004 AA02 AA03 AB05 CA18 CA34 CC09 4D059 AA01 AA07 BA12 BA15 CA14 CC10 DA37 4G046 CA02 CB02 CC08 CC09 JA01 4G075 AA04 BA06 BD04 BD12 CA02 CA54 DA01 EB01 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D004 AA02 AA03 AB05 CA18 CA34 CC09 4D059 AA01 AA07 BA12 BA15 CA14 CC10 DA37 4G046 CA02 CB02 CC08 CC09 JA01 4G075 AA04 BA06 BD04 BD12 CA02 CA54 DA01 EB01
Claims (4)
メタンガスを生成する発酵手段と、該メタンガスを分解
して水素を取り出す水素生成手段と、該水素ガスと二酸
化炭素ガスとの化学反応により固体炭素を生成する二酸
化炭素固定手段と、を有する二酸化炭素固定化装置にお
いて、二酸化炭素固定化反応が生じる反応槽内に二酸化
炭素固定化用触媒と水素燃焼用触媒を充填したことを特
徴とする二酸化炭素固定化装置。1. A fermentation means for producing methane gas by anaerobic fermentation of an organic waste, a hydrogen production means for decomposing the methane gas and extracting hydrogen, and a solid by a chemical reaction between the hydrogen gas and carbon dioxide gas. A carbon dioxide fixing device having carbon dioxide fixing means for producing carbon, wherein a carbon dioxide fixing catalyst and a hydrogen combustion catalyst are filled in a reaction tank in which a carbon dioxide fixing reaction occurs. Carbon immobilization device.
と生成する固体状炭素とを分離する剥離剤を充填したこ
とを特徴とする請求項１記載の二酸化炭素固定化装置。2. The apparatus for immobilizing carbon dioxide according to claim 1, wherein said reaction tank is filled with a release agent for separating a catalyst for immobilizing carbon dioxide and solid carbon produced.
メタンガスを生成する発酵手段と、該メタンガスを分解
して水素を取り出す水素生成手段と、該水素ガスと二酸
化炭素ガスとの化学反応により固体炭素を生成する二酸
化炭素固定手段と、を有する二酸化炭素固定化装置にお
いて、該メタンガス中に含有される窒素ガスおよび硫化
水素ガスを分離する手段を有することを特徴とする二酸
化炭素固定化装置。3. A fermentation means for generating methane gas by anaerobic fermentation of organic waste, a hydrogen generation means for decomposing the methane gas and extracting hydrogen, and a solid by a chemical reaction between the hydrogen gas and carbon dioxide gas. A carbon dioxide fixing apparatus comprising: carbon dioxide fixing means for generating carbon; and a means for separating nitrogen gas and hydrogen sulfide gas contained in the methane gas.
メタンガスを生成する発酵手段と、該メタンガスを分解
して水素を取り出す水素生成手段と、該水素ガスと二酸
化炭素ガスとの化学反応により固体炭素を生成する二酸
化炭素固定手段と、を有する二酸化炭素固定化装置にお
いて、二酸化炭素固定化反応が生じる反応槽内にメタン
分解・水素生成用触媒と二酸化炭素固定化用触媒を充填
したことを特徴とする二酸化炭素固定化装置。4. A fermenting means for producing methane gas by anaerobic fermentation of organic waste, a hydrogen producing means for decomposing the methane gas to extract hydrogen, and a solid by a chemical reaction between the hydrogen gas and carbon dioxide gas. A carbon dioxide fixing device having carbon dioxide fixing means for generating carbon, wherein a catalyst for methane decomposition / hydrogen generation and a catalyst for carbon dioxide fixing are filled in a reaction tank in which a carbon dioxide fixing reaction occurs. CO2 immobilization device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32540999A JP2001137691A (en) | 1999-11-16 | 1999-11-16 | Device for carbon dioxide fixation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32540999A JP2001137691A (en) | 1999-11-16 | 1999-11-16 | Device for carbon dioxide fixation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2001137691A true JP2001137691A (en) | 2001-05-22 |
Family
ID=18176531
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
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| JP (1) | JP2001137691A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2449233A (en) * | 2007-05-14 | 2008-11-19 | Timothy James Ronald Kruger | A process for reducing carbon dioxide to carbon utilising methane |
| JP2015516361A (en) * | 2012-04-16 | 2015-06-11 | シーアストーン リミテッド ライアビリティ カンパニー | Method for treating off-gas containing carbon oxides |
| JP2016502491A (en) * | 2012-11-29 | 2016-01-28 | シーアストーン リミテッド ライアビリティ カンパニー | Reactor and method for producing solid carbon material |
| US9731970B2 (en) | 2012-04-16 | 2017-08-15 | Seerstone Llc | Methods and systems for thermal energy recovery from production of solid carbon materials by reducing carbon oxides |
| US9796591B2 (en) | 2012-04-16 | 2017-10-24 | Seerstone Llc | Methods for reducing carbon oxides with non ferrous catalysts and forming solid carbon products |
| US11951428B2 (en) | 2016-07-28 | 2024-04-09 | Seerstone, Llc | Solid carbon products comprising compressed carbon nanotubes in a container and methods of forming same |
-
1999
- 1999-11-16 JP JP32540999A patent/JP2001137691A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2449233A (en) * | 2007-05-14 | 2008-11-19 | Timothy James Ronald Kruger | A process for reducing carbon dioxide to carbon utilising methane |
| JP2015516361A (en) * | 2012-04-16 | 2015-06-11 | シーアストーン リミテッド ライアビリティ カンパニー | Method for treating off-gas containing carbon oxides |
| US9731970B2 (en) | 2012-04-16 | 2017-08-15 | Seerstone Llc | Methods and systems for thermal energy recovery from production of solid carbon materials by reducing carbon oxides |
| US9796591B2 (en) | 2012-04-16 | 2017-10-24 | Seerstone Llc | Methods for reducing carbon oxides with non ferrous catalysts and forming solid carbon products |
| US10106416B2 (en) | 2012-04-16 | 2018-10-23 | Seerstone Llc | Methods for treating an offgas containing carbon oxides |
| JP2016502491A (en) * | 2012-11-29 | 2016-01-28 | シーアストーン リミテッド ライアビリティ カンパニー | Reactor and method for producing solid carbon material |
| US11951428B2 (en) | 2016-07-28 | 2024-04-09 | Seerstone, Llc | Solid carbon products comprising compressed carbon nanotubes in a container and methods of forming same |
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