JP2023152201A - Renewable energy-utilized gas separation recovery method and renewable energy-utilized type gas separation recovery system - Google Patents
Renewable energy-utilized gas separation recovery method and renewable energy-utilized type gas separation recovery system Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 44
- 238000000926 separation method Methods 0.000 title claims abstract description 43
- 238000011084 recovery Methods 0.000 title claims abstract description 40
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 228
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 114
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 113
- 238000010521 absorption reaction Methods 0.000 claims abstract description 107
- 239000007788 liquid Substances 0.000 claims abstract description 104
- 239000000126 substance Substances 0.000 claims abstract description 84
- 239000002028 Biomass Substances 0.000 claims abstract description 37
- 238000010438 heat treatment Methods 0.000 claims abstract description 29
- 238000010248 power generation Methods 0.000 claims abstract description 27
- 230000008929 regeneration Effects 0.000 claims abstract description 24
- 238000011069 regeneration method Methods 0.000 claims abstract description 24
- 238000002485 combustion reaction Methods 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 239000000446 fuel Substances 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 238000007664 blowing Methods 0.000 claims abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 44
- 239000012530 fluid Substances 0.000 claims description 31
- 230000005611 electricity Effects 0.000 claims description 21
- 239000013529 heat transfer fluid Substances 0.000 claims description 19
- 238000000855 fermentation Methods 0.000 claims description 17
- 230000004151 fermentation Effects 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 230000001172 regenerating effect Effects 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 230000001737 promoting effect Effects 0.000 claims description 5
- 238000005516 engineering process Methods 0.000 abstract description 18
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000007906 compression Methods 0.000 abstract 1
- 230000006835 compression Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 140
- 239000002803 fossil fuel Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007791 dehumidification Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- -1 etc. Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000010794 food waste Substances 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000002101 nanobubble Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
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- 230000026676 system process Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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Classifications
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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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
Description
本発明は、アミン系の化学吸収液を用いてバイオガスや大気から二酸化炭素ガスを分離回収する場合など、化学吸収液を用いてガスを分離回収する際に、地熱蒸気や自噴源泉等の地熱流体やバイオガス燃焼熱、太陽熱などの再生可能エネルギー熱を利用して効率的にガスを分離回収する方法と、本方法を適用した再生可能エネルギー活用型のガス分離回収システムに関するものである。 The present invention is applicable to geothermal steam, artesian hot springs, etc. when separating and recovering gas using a chemical absorption liquid, such as when separating and recovering biogas or carbon dioxide gas from the atmosphere using an amine-based chemical absorption liquid. The present invention relates to a method for efficiently separating and recovering gas using renewable energy heat such as fluid, biogas combustion heat, and solar heat, and a gas separation and recovery system that utilizes renewable energy to which this method is applied.
地球温暖化の主要な原因物質となっている二酸化炭素の排出抑制や削減にむけて、化石燃料利用時の燃焼排ガスに含まれる二酸化炭素ガスを分離回収して地下貯留槽に圧入固定する技術や、空気やバイオガスに含まれる二酸化炭素ガスを分離回収して固定化するネガティブエミッション技術、さらには分離回収した二酸化炭素ガスを化成品原料として有効利用し、炭素循環システムを構築する二酸化炭素ガスの有効利用技術が期待されている。 In order to suppress and reduce emissions of carbon dioxide, which is a major cause of global warming, we are developing technology that separates and recovers carbon dioxide gas contained in combustion exhaust gas when fossil fuels are used, and fixes it by injecting it into underground storage tanks. , negative emission technology that separates and recovers and fixes carbon dioxide gas contained in air and biogas, and carbon dioxide gas that effectively uses separated and recovered carbon dioxide gas as raw material for chemical products to build a carbon circulation system. Effective utilization technology is expected.
このうち、二酸化炭素ガスの分離回収方法としては、二酸化炭素ガスとの反応性が高いアミン系水溶液で構成される化学吸収液に二酸化炭素を吸収させた後に、この吸収液を化石燃料の燃焼で生じた燃焼ガスの熱で発生させたボイラ蒸気や排気ガス等によって加熱することで、二酸化炭素ガスを脱離させながら化学吸収液を再生したうえで、再生した化学吸収液に再び二酸化炭素ガスを吸収させて循環を行う、化学吸収液を用いた二酸化炭素ガスの分離回収技術が広く知られており、本技術においてボイラ起動から二酸化炭素の分離回収装置が稼働するまでのタイムラグ期間における二酸化炭素ガスの排出を抑制するため、再生可能エネルギー発電設備と二次電池から得られる放電電力によって電気ヒータを用いてボイラ蒸気を発生させ、化学吸収液の加熱再生を行うことで、ボイラ起動工程中の二酸化炭素ガスの排出抑制を行うボイラープラント技術（特許文献１）が開示されている。 Among these methods, carbon dioxide gas is separated and recovered by absorbing carbon dioxide into a chemical absorption liquid made of an amine-based aqueous solution that is highly reactive with carbon dioxide gas, and then using this absorption liquid by burning fossil fuels. The chemical absorption liquid is regenerated while desorbing carbon dioxide gas by heating with boiler steam or exhaust gas generated by the heat of the combustion gas generated, and then carbon dioxide gas is added to the regenerated chemical absorption liquid again. Carbon dioxide gas separation and recovery technology using a chemical absorption liquid that absorbs and circulates is widely known. In order to reduce CO2 emissions during the boiler startup process, boiler steam is generated using an electric heater using discharge power obtained from renewable energy power generation equipment and secondary batteries, and the chemical absorption liquid is heated and regenerated. A boiler plant technology (Patent Document 1) that suppresses carbon gas emissions is disclosed.
また、前記のアミン系水溶液を用いた二酸化炭素ガスの分離回収技術では、ガスの分離回収に要するエネルギーの８０％程度が化学吸収液に含まれる水分の加熱蒸発に消費されていることから、二酸化炭素ガス吸収後の化学吸収液を再生するために処理液の減圧処理と、空気や窒素等のストリッピングガスを用いることで消費エネルギーを削減するほか、再生前後の化学吸収液を熱交換器を介して熱交換することで再生前の化学吸収液を予熱したり、再生後の化学吸収液を冷却器を介して冷却水によって冷却することで、化学吸収液の二酸化炭素ガスの吸収性能や吸収量を高める技術（特許文献２）が開示されている。 In addition, in the carbon dioxide gas separation and recovery technology using the above-mentioned amine-based aqueous solution, about 80% of the energy required for gas separation and recovery is consumed in heating and evaporating the water contained in the chemical absorption liquid. In order to regenerate the chemical absorption liquid after absorbing carbon gas, energy consumption can be reduced by reducing the pressure of the processing liquid and using a stripping gas such as air or nitrogen. By preheating the chemical absorption liquid before regeneration through heat exchange through A technique for increasing the amount (Patent Document 2) is disclosed.
前記の通り、特許文献１の従来技術によれば、化石燃料を利用するボイラ等において、起動工程も含めて燃焼排気ガスから二酸化炭素ガスを効率よく回収して、ボイラ等の利用時における二酸化炭素の排出量を削減できるほか、特許文献２の従来技術によれば、化学吸収液を用いた二酸化炭素の分離回収プロセスにおいて、多大なエネルギー消費と二酸化炭素排出の要因となっている、二酸化炭素ガスを吸収した化学吸収液の加熱再生において、エネルギー消費量を削減して二酸化炭素の分離回収効率を高めることが可能となるが、これらの技術には以下に示す３つの課題がある。 As mentioned above, according to the prior art disclosed in Patent Document 1, carbon dioxide gas is efficiently recovered from combustion exhaust gas, including the startup process, in boilers that use fossil fuels, etc., and carbon dioxide gas is recovered when the boilers are used. In addition, according to the conventional technology of Patent Document 2, carbon dioxide gas, which is a cause of large energy consumption and carbon dioxide emissions, can be reduced in the carbon dioxide separation and recovery process using a chemical absorption liquid. In heating and regenerating the chemical absorption liquid that has absorbed carbon dioxide, it is possible to reduce energy consumption and increase the efficiency of separating and recovering carbon dioxide, but these techniques have the following three problems.
まず特許文献１の従来技術における起動工程以外の通常運転時と、特許文献２の従来技術では、化学吸収液の加熱再生において、化石燃料を利用するボイラから得られる水蒸気やごみ焼却施設等で発生する排気ガスの熱が利用されており、ごみ焼却施設で燃焼する廃棄物の中に化石燃料起源の炭化水素化合物も含まれていることを考慮すれば、いずれも再生可能エネルギー熱を利用した加熱再生とはなっておらず、二酸化炭素ガスの分離回収プロセスに係わる化石燃料の消費と二酸化炭素の排出が伴うため、正味の二酸化炭素分離回収量が減少するという課題がある。 First, during normal operation other than the start-up process in the conventional technology of Patent Document 1, and in the conventional technology of Patent Document 2, during heating and regeneration of chemical absorption liquid, steam generated from boilers that use fossil fuels and waste incineration facilities, etc. However, considering that the waste burned at waste incineration facilities also contains hydrocarbon compounds derived from fossil fuels, it is possible to use renewable energy heat for heating. There is a problem that the net amount of carbon dioxide separation and recovery decreases because it is not recycled, and the process of separating and recovering carbon dioxide gas involves consumption of fossil fuels and emission of carbon dioxide.
また、特許文献１の従来技術では、化石燃料を利用するボイラの起動工程時における二酸化炭素ガスの分離回収において、太陽光発電や風力発電等の再生可能エネルギー電力と、これら電力を充電した二次電池の放電利用による吸収液の加熱再生によって、起動工程時における二酸化炭素ガスの分離回収に係わる化石燃料の消費と二酸化炭素の排出を削減することは可能であるが、その期間は起動工程時に限定され、太陽光や風力発電等の変動性電源と二次電池による電力供給による電気ヒータ加熱では、発電電力の不安定性や二次電池の蓄電容量に限界があるため、長期間の通常運転時における安定稼働と持続維持が困難であることに加え、発電電力の変換効率や二次電池への充放電効率と、放電電力による電熱ヒータの電熱効率に係わる電力損失が伴い、化学吸収液の加熱再生に係わるエネルギーの変換効率が低いという課題がある。 In addition, in the conventional technology of Patent Document 1, in the separation and recovery of carbon dioxide gas during the startup process of a boiler that uses fossil fuels, renewable energy power such as solar power generation or wind power generation and a secondary It is possible to reduce fossil fuel consumption and carbon dioxide emissions associated with the separation and recovery of carbon dioxide gas during the start-up process by heating and regenerating the absorption liquid using battery discharge, but this period is limited to the start-up process. However, with electric heater heating using variable power sources such as solar power and wind power generation and power supplied by secondary batteries, there is a limit to the instability of the generated power and the storage capacity of the secondary batteries, so it is difficult to use during long-term normal operation. In addition to being difficult to maintain stable operation and sustain, there is a power loss related to the conversion efficiency of generated power, the charging and discharging efficiency of secondary batteries, and the electric heating efficiency of electric heaters due to discharged power, and heating regeneration of chemical absorption liquid is difficult. There is a problem that the conversion efficiency of energy related to is low.
さらに、いずれの従来技術においても、化学吸収液の冷却と、分離回収ガスに含まれる水蒸気等の凝縮除去における冷却において、冷却器や冷却水を利用しているが、これらに供給する冷熱の具体的な供給方法が開示されておらず、これらの冷熱供給において、化石燃料起源の電気や熱を利用する場合には、冷熱供給に係わる化石燃料の消費と二酸化炭素の排出が伴うため、燃料コストが嵩み、正味の二酸化炭素分離回収量が減少するほか、系統電力の接続が困難な地域での技術適用ができず、停電時には稼働を継続できないという課題がある。 Furthermore, in any of the conventional technologies, a cooler or cooling water is used for cooling the chemical absorption liquid and cooling for condensation removal of water vapor contained in the separated and recovered gas. However, if electricity or heat derived from fossil fuels is used to supply cold heat, the consumption of fossil fuels and the emission of carbon dioxide will be involved, resulting in lower fuel costs. In addition to increasing the amount of carbon dioxide and reducing the net amount of carbon dioxide separation and capture, the technology cannot be applied in areas where it is difficult to connect to grid electricity, and there are issues with continued operation in the event of a power outage.
同様に、特許文献２の従来技術における減圧ポンプや化学吸収液の循環ポンプなど、いずれの従来技術においても、システムを構成するポンプやガス圧縮機、ガスブロワ等の電気設備の駆動電力が再生可能エネルギー利用による方法となっておらず、これら設備の駆動電力が化石燃料起源の電力の場合には、電力消費に伴うコストが嵩み、正味の二酸化炭素分離回収量が減少するほか、系統電力の接続が困難な地域での技術適用ができず、停電時には稼働を継続できないという課題がある。 Similarly, in any of the conventional technologies such as the decompression pump and the chemical absorption liquid circulation pump in the prior art of Patent Document 2, the driving power of the electric equipment such as the pump, gas compressor, gas blower, etc. that makes up the system is renewable energy. If the electricity used to drive these facilities is derived from fossil fuels, the cost associated with electricity consumption will increase, the net amount of carbon dioxide separation and capture will decrease, and the connection of grid electricity will be required. The problem is that the technology cannot be applied in areas where it is difficult to operate, and that it cannot continue operating during a power outage.
また、従来技術の適用ガスは、化石燃料を利用するボイラ排ガスのほか、バイオガスや燃焼排ガス等の二酸化炭素含有ガスであり、バイオガスから二酸化炭素を分離回収した際に得られるバイオメタン等の可燃ガスを利用した際に発生する二酸化炭素ガスの分離回収まで含まれていないことから、これらの従来技術だけでは、大気中の二酸化炭素を分離回収したり、バイオガス起源の二酸化炭素を全量分離回収して固定化する、ネガティブエミッションに応用できないという課題がある。 In addition, the gases to which the conventional technology is applied include boiler exhaust gas that uses fossil fuels, as well as carbon dioxide-containing gases such as biogas and combustion exhaust gas, and biomethane and other gases obtained when carbon dioxide is separated and recovered from biogas. Since these conventional technologies do not include the separation and recovery of carbon dioxide gas generated when combustible gas is used, it is not possible to separate and recover atmospheric carbon dioxide or completely separate the carbon dioxide originating from biogas. There is a problem in that it cannot be collected and fixed, and cannot be applied to negative emissions.
本発明は、これらの課題に鑑みてなされたものであり、その目的は、再生可能エネルギーを利用して、エネルギー消費に係わるコストや二酸化炭素ガスの排出量を削減しながら、電力系統の停電影響を受けることなく、電力系統への接続困難な場所への適用や、二酸化炭素ガスのネガティブエミッションにも応用可能な、再生可能エネルギー活用によるガスの分離回収方法と、本技術を適用した、再生可能エネルギー活用型のガス分離回収システムを提供することである。 The present invention was made in view of these issues, and its purpose is to reduce the impact of power outages on the power system while reducing energy consumption costs and carbon dioxide emissions by using renewable energy. A gas separation and recovery method using renewable energy, which can be applied to places where it is difficult to connect to the power grid and negative emissions of carbon dioxide gas, and a renewable energy system using this technology. The objective is to provide an energy-utilizing gas separation and recovery system.
上記課題を解決するため、請求項１に記載の発明は、
化学吸収液を用いたガスの分離回収工程において、分離回収するガスを吸収させた化学吸収液と地熱流体を熱交換器を介して熱交換させるか、地熱かバイオマス燃焼熱、または太陽熱によって熱せられた熱媒流体と熱交換器を介して熱交換させるか、再生可能エネルギー電力で駆動する電気ヒータを介して熱せられた熱媒流体と熱交換器を介して熱交換させるか、いずれか一つ以上の熱交換方法によって、化学吸収液を加熱再生しながらガスを分離回収することを特徴とする。In order to solve the above problem, the invention according to claim 1,
In the gas separation and recovery process using a chemical absorption liquid, the chemical absorption liquid that has absorbed the gas to be separated and recovered and the geothermal fluid are heat exchanged via a heat exchanger, or heated by geothermal heat, biomass combustion heat, or solar heat. or exchange heat with a heat transfer fluid heated by an electric heater powered by renewable energy, or exchange heat with a heat transfer fluid heated by an electric heater powered by renewable energy. The above heat exchange method is characterized in that gas is separated and recovered while heating and regenerating the chemical absorption liquid.
請求項２に記載の発明は、
請求項１に記載のガス分離回収方法において、熱交換後の地熱流体または熱媒流体と、分離回収するガスを吸収させた化学吸収液を、熱交換器を介して熱交換させることで、加熱再生前の化学吸収液を、熱交換後の地熱流体か熱媒流体の熱を用いて予熱昇温させることを特徴とする。The invention according to claim 2 is
In the gas separation and recovery method according to claim 1, the geothermal fluid or heating medium fluid after heat exchange and the chemical absorption liquid that has absorbed the gas to be separated and recovered are heated by exchanging heat through a heat exchanger. It is characterized by preheating and raising the temperature of the chemical absorption liquid before regeneration using the heat of the geothermal fluid or heat transfer fluid after heat exchange.
請求項３に記載の発明は、
請求項１に記載の熱交換後の地熱流体または熱媒流体と、請求項２に記載の予熱熱交換後の地熱流体または熱媒流体のいずれか、または両方を熱源として駆動する、吸収式または吸着式の冷凍機によって得られる冷水を用いて、加熱再生後の化学吸収液か、化学吸収液の蒸気を含む分離回収ガスの何れか、または両方を冷却することを特徴とする。The invention according to claim 3 is
Absorption type or It is characterized by using cold water obtained by an adsorption type refrigerator to cool either the chemical absorption liquid after heating and regeneration, the separated and recovered gas containing the vapor of the chemical absorption liquid, or both.
請求項４に記載の発明は、
請求項１に記載の熱交換後の地熱流体または熱媒流体と、請求項２に記載の予熱熱交換後の地熱流体または熱媒流体のいずれか、または両方を熱源として駆動するフラッシュ式またはバイナリー式の発電機によって得られる電力か、再生可能エネルギー電力によって駆動するターボ冷凍機を介して得られる冷水を用いて、加熱再生後の化学吸収液か、化学吸収液の蒸気を含む分離回収ガスの何れか、または両方を冷却することを特徴とする。The invention according to claim 4 includes:
A flash type or binary device that drives either or both of the geothermal fluid or heat transfer fluid after heat exchange according to claim 1 and the geothermal fluid or heat transfer fluid after preheating heat exchange according to claim 2 as a heat source. The chemical absorption liquid after heating and regeneration, or the separated and recovered gas containing the vapor of the chemical absorption liquid, is heated and regenerated using electric power obtained from a conventional generator or cold water obtained through a centrifugal chiller driven by renewable energy electricity. It is characterized by cooling either or both.
請求項５に記載の発明は、
地熱流体か、バイオマス燃焼熱か地熱または太陽熱によって加熱された蒸気を駆動力とするタービンに直結されたガス吸気圧縮機か、再生可能エネルギー電力によって駆動するガス吸気圧縮機によって、分離回収ガスを含む混合気を吸気圧縮し、前記圧縮ガスを化学吸収液のタンク内に微細気泡化して噴出供給することで、化学吸収液への分離ガス吸収を促進させることを特徴とする。The invention according to claim 5 includes:
containing separated and recovered gas by a gas inlet compressor connected directly to a turbine driven by geothermal fluid, biomass combustion heat, geothermal or solar heated steam, or by a gas inlet compressor driven by renewable energy electricity. The method is characterized in that the air-fuel mixture is taken in and compressed, and the compressed gas is turned into fine bubbles and ejected into the chemical absorption liquid tank, thereby promoting the absorption of the separated gas into the chemical absorption liquid.
請求項６に記載の発明は、
地熱流体か、バイオマス燃焼熱か地熱または太陽熱によって加熱された蒸気を駆動力とするタービンに直結されたガス吸気送風ブロワか、再生可能エネルギー電力によって駆動するガス吸気送風ブロワによって、分離回収ガスを含む混合気を、化学吸収液が流下する容器内に吸気送風することで、化学吸収液への分離ガス吸収を促進させることを特徴とする。The invention according to claim 6 includes:
containing separated and recovered gas by a gas inlet blower directly connected to a turbine driven by geothermal fluid, biomass combustion heat, geothermal or solar heated steam, or by a gas inlet blower driven by renewable energy electricity. The method is characterized in that absorption of the separated gas into the chemical absorption liquid is promoted by sucking and blowing the air mixture into a container into which the chemical absorption liquid flows.
請求項７に記載の発明は、
地熱流体か、バイオマス燃焼熱か地熱または太陽熱によって加熱された蒸気を駆動力とするタービンに直結された化学吸収液の送液循環ポンプか、再生可能エネルギー電力によって駆動する化学吸収液の送液循環ポンプによって、分離回収するガスを吸収した化学吸収液か、再生可能エネルギーによって加熱再生された化学吸収液の何れかまたは両方が送液循環されることを特徴とする。The invention according to claim 7 includes:
A chemical absorption liquid circulation pump directly connected to a turbine driven by geothermal fluid, biomass combustion heat, geothermal or solar heated steam, or a chemical absorption liquid circulation pump driven by renewable energy electricity. The pump is characterized in that the chemical absorption liquid that has absorbed the gas to be separated and recovered, or the chemical absorption liquid that has been heated and regenerated using renewable energy, or both, are fed and circulated.
請求項８に記載の発明は、
請求項１に記載の熱交換後の地熱流体または熱媒流体と、請求項２に記載の予熱熱交換後の地熱流体または熱媒流体のいずれか、または両方を熱源として駆動するフラッシュ式またはバイナリー式の発電機によって得られる電力か、再生可能エネルギー電力によって、請求項３に記載の冷凍機とその附帯設備か、請求項４に記載の発電機とターボ冷凍機の附帯設備か、請求項５に記載のガス吸気圧縮機か、請求項６に記載のガス吸気ブロワか、請求項７に記載の送液循環ポンプとその附帯設備のうち、何れか一つ以上が駆動されることを特徴とする。The invention according to claim 8 includes:
A flash type or binary device that drives either or both of the geothermal fluid or heat transfer fluid after heat exchange according to claim 1 and the geothermal fluid or heat transfer fluid after preheating heat exchange according to claim 2 as a heat source. The refrigerator and its ancillary equipment according to claim 3, the generator and centrifugal chiller ancillary equipment according to claim 4, or claim 5, by electricity obtained by a generator of the formula or renewable energy electricity. The gas intake compressor according to claim 6, the gas intake blower according to claim 6, or the liquid feeding circulation pump and its ancillary equipment according to claim 7 are driven. do.
請求項９に記載の発明は、
請求項１および請求項２に記載の熱交換後の地熱流体または熱媒流体と、請求項３に記載の冷凍機駆動後の地熱流体または熱媒流体と、請求項４に記載の発電機駆動後の地熱流体または熱媒流体のいずれか一つ以上を用いてバイオマスのメタン発酵槽を加温し、前記メタン発酵槽から得られるバイオガスから、請求項１～請求項８に記載の何れか一つ以上の方法によって、バイオガス中の二酸化炭素を分離回収することを特徴とする。The invention according to claim 9 includes:
The geothermal fluid or heat transfer fluid after heat exchange according to claims 1 and 2, the geothermal fluid or heat transfer fluid after driving the refrigerator according to claim 3, and the generator drive according to claim 4. Any one of claims 1 to 8 from the biogas obtained from the methane fermentation tank by heating a biomass methane fermentation tank using one or more of the subsequent geothermal fluid or heat transfer fluid. It is characterized by separating and recovering carbon dioxide in biogas by one or more methods.
請求項１０に記載の発明は、
請求項９に記載の方法によってバイオマスをメタン発酵し、得られるバイオガスから二酸化炭素ガスを分離回収することで、バイオガス起源の二酸化炭素ガスとバイオメタンを分離して回収するとともに、回収したバイオメタンを燃料として発電システムか燃焼システムを運転して、得られる再生可能エネルギー電力と再生可能エネルギー熱を、請求項１～請求項９の電力や熱として利用しつつ、発電システムか燃焼システムからの排気ガスに含まれる二酸化炭素ガスを、請求項１～請求項９に記載の方法によって分離回収することを特徴とする。The invention according to claim 10 is
By methane fermenting biomass by the method according to claim 9 and separating and recovering carbon dioxide gas from the obtained biogas, carbon dioxide gas and biomethane originating from the biogas are separated and recovered, and the recovered biomass is While operating the power generation system or combustion system using methane as fuel and using the renewable energy power and renewable energy heat obtained as the power and heat according to claims 1 to 9, The present invention is characterized in that carbon dioxide gas contained in exhaust gas is separated and recovered by the methods described in claims 1 to 9.
請求項１１に記載の発明は、
請求項１０に記載の方法によってバイオマスをメタン発酵し、得られるバイオガス中の二酸化炭素ガスと、バイオガス中のバイオメタンを利用する際に発生するバイオメタン起源の二酸化炭素ガスとを分離回収することで、バイオマス起源の二酸化炭素ガスを分離回収することを特徴とする。The invention according to claim 11 is
Biomass is subjected to methane fermentation by the method according to claim 10, and carbon dioxide gas in the obtained biogas and carbon dioxide gas originating from biomethane generated when using biomethane in the biogas are separated and recovered. This system is characterized by the ability to separate and recover carbon dioxide gas originating from biomass.
請求項１２に記載の発明は、
請求項１～請求項８に記載の何れか一つ以上の方法によって、再生可能エネルギーを用いて空気から空気中の二酸化炭素ガスを分離回収する、再生可能エネルギー活用型二酸化炭素ガス分離回収システムであることを特徴とする。The invention according to claim 12 is
A carbon dioxide gas separation and recovery system utilizing renewable energy, which separates and recovers carbon dioxide gas from the air using renewable energy by any one or more of the methods set forth in claims 1 to 8. characterized by something.
本発明によれば、エネルギー消費に係わるコストや二酸化炭素ガスの排出量を削減しながら、電力系統の停電影響を受けることなく、電力系統への接続困難な場所への適用や、二酸化炭素ガスのネガティブエミッションにも応用可能な、再生可能エネルギー活用によるガスの分離回収が可能となる。 According to the present invention, while reducing costs related to energy consumption and carbon dioxide gas emissions, it can be applied to places where it is difficult to connect to the power grid, and can be applied to places where it is difficult to connect to the power grid and reduce carbon dioxide gas emissions. This makes it possible to separate and recover gas using renewable energy, which can also be applied to negative emissions.
以下、図面を参照して本発明を実施するための最良の形態について説明する。なお、本発明の範囲は特許請求の範囲記載のものであって、本実施形態に限定されるものではない。 DESCRIPTION OF THE PREFERRED EMBODIMENTS The best mode for carrying out the present invention will be described below with reference to the drawings. Note that the scope of the present invention is defined in the claims, and is not limited to the present embodiment.
（第１実施形態）(First embodiment)
まず本発明の第１実施形態に係る、地熱蒸気を活用したバイオメタンとバイオマス起源二酸化炭素ガスの分離回収システムについて、図１に基づいて説明する。 First, a separation and recovery system for biomethane and biomass-derived carbon dioxide gas using geothermal steam according to a first embodiment of the present invention will be described based on FIG. 1.
図１に示すように、このシステムは、食品廃棄物や農水産非可食部等のバイオマス資源１をメタン発酵処理し、バイオガスを生成させるメタン発酵槽２から発生する、バイオメタンと二酸化炭素および硫化水素等の微量成分で構成されるバイオガスから、地熱蒸気３のエネルギーを利用して、バイオメタンと二酸化炭素ガスを分離して回収するものである。 As shown in Figure 1, this system processes biomass resources 1, such as food waste and inedible parts of agricultural and fishery products, through methane fermentation, and generates biomethane and carbon dioxide from a methane fermentation tank 2, which generates biogas. The energy of geothermal steam 3 is used to separate and recover biomethane and carbon dioxide gas from biogas composed of trace components such as hydrogen sulfide and hydrogen sulfide.
本システムでは、地熱蒸気によって駆動される蒸気タービン４に直結されたガス吸気圧縮機５によって、バイオガス中の硫化水素等の微量成分を除去するバイオガス浄化装置６を通過したバイオメタンと二酸化炭素の混合気が吸引圧縮され、二酸化炭素ガスを吸収するアミン水溶液等の化学吸収液７が収容された二酸化炭素ガス吸収設備８の吸収液中に、マイクロバブルやナノバブル等の微細気泡として供給する微細気泡化ガス供給管９を介して放出されるよう構成され、この容器内でバイオガス中の二酸化炭素ガスが化学吸収液によって吸収除去されるため、二酸化炭素ガス吸収設備上部のバイオメタン抽出管１０からは、二酸化炭素が除去されたバイオメタンガスを回収することが可能となっている。 In this system, biomethane and carbon dioxide are passed through a biogas purification device 6 that removes trace components such as hydrogen sulfide from biogas by a gas intake compressor 5 directly connected to a steam turbine 4 driven by geothermal steam. The air-fuel mixture is suctioned and compressed and supplied as fine bubbles such as microbubbles or nanobubbles into the absorption liquid of the carbon dioxide gas absorption equipment 8, which contains a chemical absorption liquid 7 such as an amine aqueous solution that absorbs carbon dioxide gas. The biomethane extraction pipe 10 in the upper part of the carbon dioxide gas absorption equipment is configured to be released through the aerated gas supply pipe 9, and the carbon dioxide gas in the biogas is absorbed and removed by the chemical absorption liquid in this container. It is now possible to recover biomethane gas from which carbon dioxide has been removed.
また本システムでは、二酸化炭素ガスを吸収した化学吸収液が、吸収液循環供給ポンプ１１を介して化学吸収液の加熱再生による二酸化炭素の脱離回収を行う、化学吸収液再生設備１２に供給され、さらに再生設備内で化学吸収液の加熱再生を行う熱源として、地熱蒸気タービン４を駆動した後の地熱蒸気が供給されることで、加熱再生容器１３の中で化学吸収液が加熱されて二酸化炭素ガスが脱離放出されて、二酸化炭素ガス収集管１４を介して分離回収された後に、回収ガスを冷却して回収ガス中に含まれる水蒸気分や化学吸収液の凝縮液化成分を凝縮回収して化学吸収液の循環系統に還流させるための回収ガス冷却器１５を経て、二酸化炭素ガスが分離回収される構成となっている。 In addition, in this system, the chemical absorption liquid that has absorbed carbon dioxide gas is supplied via the absorption liquid circulation supply pump 11 to the chemical absorption liquid regeneration equipment 12 that desorbs and recovers carbon dioxide by heating and regenerating the chemical absorption liquid. Furthermore, the geothermal steam after driving the geothermal steam turbine 4 is supplied as a heat source for heating and regenerating the chemical absorption liquid in the regeneration equipment, so that the chemical absorption liquid is heated in the heating regeneration vessel 13 to produce carbon dioxide. After the carbon gas is desorbed and released and separated and recovered via the carbon dioxide gas collection pipe 14, the recovered gas is cooled to condense and recover the water vapor contained in the recovered gas and the condensed and liquefied components of the chemical absorption liquid. The carbon dioxide gas is separated and recovered through a recovered gas cooler 15 for refluxing into the chemical absorption liquid circulation system.
なお、前述の化学吸収液再生設備１２では、加熱再生容器１３の中で二酸化炭素ガスが脱離されて再生した化学吸収液は、再生化学吸収液の収集管１６で集められた後に、二酸化炭素ガス吸収設備８に供給されて、再び二酸化炭素ガスの吸収を行う、循環流路が構成されており、このような構成とすることで、地熱蒸気のエネルギーを利用して、連続的にバイオガスからバイオメタンと二酸化炭素ガスを分離して回収できる構成となっている。 In the above-mentioned chemical absorption liquid regeneration equipment 12, the chemical absorption liquid that has been regenerated by desorbing carbon dioxide gas in the heating regeneration vessel 13 is collected in the collection pipe 16 for the regenerated chemical absorption liquid, and then the carbon dioxide is collected. A circulation flow path is configured that is supplied to the gas absorption equipment 8 and absorbs carbon dioxide gas again. With this configuration, biogas is continuously produced using the energy of geothermal steam. The structure is such that biomethane and carbon dioxide gas can be separated and recovered from the gas.
さらに本システムでは、二酸化炭素ガスの分離回収効率向上と回収量の増加によって、システム全体のエネルギー効率向上と、正味の二酸化炭素回収量を増加させるため、地熱蒸気のエネルギーを多段階に活用する構成としている。すなわち、二酸化炭素ガスの吸収と脱離を行う化学吸収液において、二酸化炭素吸収後の化学吸収液（リッチ液）からの二酸化炭素ガスの加熱放出による再生を促進するため、二酸化炭素ガス吸収設備８の中で地熱蒸気の熱交換によって生じたドレン熱水を供給して予熱を行うリッチ液の予熱用熱交換器１７と、二酸化炭素を脱離して再生された化学吸収液（リーン液）との間で熱交換を行う化学吸収液熱交換器１８を介してリッチ液の予熱を促進する一方、リーン液については温度が低いほど二酸化炭素ガスの吸収性能と吸収容量が向上するため、二酸化炭素ガス吸収設備８に供給するリーン液を冷却するリーン液冷却用熱交換器１９が具備されている。 Furthermore, this system utilizes geothermal steam energy in multiple stages in order to improve the energy efficiency of the entire system and increase the net amount of carbon dioxide captured by improving the separation and recovery efficiency of carbon dioxide gas and increasing the amount recovered. It is said that That is, in a chemical absorption liquid that absorbs and desorbs carbon dioxide gas, in order to promote regeneration by heating and releasing carbon dioxide gas from the chemical absorption liquid (rich liquid) after carbon dioxide absorption, the carbon dioxide gas absorption equipment 8 is used. A rich liquid preheating heat exchanger 17 performs preheating by supplying condensate hot water generated by heat exchange with geothermal steam, and a chemical absorption liquid (lean liquid) regenerated by desorbing carbon dioxide. Preheating of the rich liquid is promoted through the chemical absorption liquid heat exchanger 18, which exchanges heat between A lean liquid cooling heat exchanger 19 that cools the lean liquid supplied to the absorption equipment 8 is provided.
ここで、リーン液を冷却するための冷却水は、前記のリッチ液の予熱用熱交換器１７を通過した後の温水を熱源として駆動される吸着式冷凍機２０によって得られる循環冷却水を利用することで、再生可能エネルギーである地熱の温熱を利用してリーン液を冷却するように構成されている。 Here, as the cooling water for cooling the lean liquid, circulating cooling water obtained by an adsorption refrigerator 20 that is driven using the hot water that has passed through the rich liquid preheating heat exchanger 17 as a heat source is used. By doing so, it is configured to cool the lean liquid using the heat from geothermal heat, which is a renewable energy source.
また、本システムを構成する化学吸収液の循環ポンプ１１や吸着式冷凍機２０のほか、システムを構成するポンプや冷却塔などの電気機器は、全て再生可能エネルギー電力の供給によって賄われるように構成されている。すなわち、化学吸収液再生設備１２に供給される地熱蒸気のうち、汽液分離されて排出された高温の地熱蒸気を駆動源として発電を行うバイナリー発電システム２１から得られる再生可能エネルギー電力によって、システムを構成する電気機器が稼働する構成となっている。 Additionally, in addition to the chemical absorption liquid circulation pump 11 and adsorption chiller 20 that make up this system, the electrical equipment such as pumps and cooling towers that make up the system are all configured to be powered by renewable energy. has been done. That is, out of the geothermal steam supplied to the chemical absorption liquid regeneration equipment 12, the system is powered by renewable energy power obtained from the binary power generation system 21, which generates electricity using high temperature geothermal steam discharged after steam separation as a driving source. The electrical equipment that makes up the system is configured to operate.
このような構成とすることで、本システムは電力系統の接続が困難な地域でも系統と独立して運用することが可能であるほか、系統の連系して運転する場合に系統停電が発生しても、運転を継続することが可能となっている。 With this configuration, this system can be operated independently from the power grid even in areas where connection to the power grid is difficult, and can also be operated without grid power outages when connected to the grid. However, it is possible to continue operation.
なお、前記バイナリー発電システム２１を駆動した後に排水される温水は、ポンプを介して前記のメタン発酵槽２の加温や保温のための供給された後に排水されるような構成とすることで、寒冷地や冬季においても、バイオマスのメタン発酵を安定的に行えるように構成されている。 Note that the hot water drained after driving the binary power generation system 21 is configured such that it is supplied to the methane fermentation tank 2 through a pump for heating and keeping it warm, and then drained. The structure is designed to allow stable methane fermentation of biomass even in cold regions and winter.
以上の特長を有するシステム構成によって、本システムは電力系統の接続が困難な地域でも系統と独立して安定的にバイオマスからバイオメタンとバイオマス起源の二酸化炭素ガスを分離回収することが可能となっている。なお、分離回収したバイオメタンや二酸化炭素ガスは、前記バイナリー発電システム等から得られる電力によって圧縮機を駆動してボンベ等に圧縮貯蔵し、需要地でバイオメタンや工業用二酸化炭素ガスとして消費したり、二酸化炭素ガスは貯留サイトに輸送して圧入固定化すれば、バイオマス起源の二酸化炭素ガスを回収固定するネガティブエミッションを実現することも可能である。
（第２実施形態）The system configuration with the above features makes it possible for this system to stably separate and recover biomethane and biomass-derived carbon dioxide gas from biomass independently of the grid even in areas where connection to the power grid is difficult. There is. The separated and recovered biomethane and carbon dioxide gas are compressed and stored in cylinders by driving a compressor using electric power obtained from the binary power generation system, etc., and consumed as biomethane and industrial carbon dioxide gas at the point of demand. Alternatively, by transporting carbon dioxide gas to a storage site and injecting and fixing it, it is also possible to realize negative emissions in which biomass-derived carbon dioxide gas is recovered and fixed.
(Second embodiment)
次に、本発明の第２実施形態に係る、バイオマスメタン発酵発電時のバイオマス起源二酸化炭素ガスの分離回収システムについて、図２に基づいて説明する。 Next, a separation and recovery system for biomass-derived carbon dioxide gas during biomass methane fermentation power generation according to a second embodiment of the present invention will be described based on FIG. 2.
図２に示すように、第２実施形態のシステムでは、メタン発酵槽２から発生するバイオガスを燃料とする、バイオガス発電システム２２によって発電利用し、得られる発電電力によって二酸化炭素ガスの分離回収システムを稼働させるとともに、発電システムから得られる高温排気ガスの熱を利用して、排ガス熱交換器２３を介して二酸化炭素ガスの吸収を行う化学吸収液を加熱再生と、吸着式冷凍機を駆動させる熱源媒体の供給、およびメタン発酵槽の加温とを段階的に行う、熱媒循環系統における熱媒の熱回収を行う構成としている点が第１実施形態と異なっている。 As shown in FIG. 2, in the system of the second embodiment, the biogas generated from the methane fermenter 2 is used as fuel to generate electricity by a biogas power generation system 22, and the generated power is used to separate and recover carbon dioxide gas. In addition to operating the system, the heat of high-temperature exhaust gas obtained from the power generation system is used to heat and regenerate the chemical absorption liquid that absorbs carbon dioxide gas through the exhaust gas heat exchanger 23, and to drive the adsorption refrigerator. This embodiment is different from the first embodiment in that the heat medium circulation system is configured to supply a heat source medium for the methane fermentation and to heat the methane fermentation tank in stages, and to recover heat from the heat medium in the heat medium circulation system.
また、前記バイオガス発電システムの高温排気ガスは、熱交換器２３で循環熱媒を加熱する際に凝縮水ドレンＤが発生するが、このドレン水は排水され、二酸化炭素ガスを含む排気ガスを圧縮して二酸化炭素ガス吸収設備８に供給する、排気ガスの吸気圧縮機５が、前記のバイオガス発電システムの発電電力によって稼働される点と、バイオガス発電システムから余剰電力が発生する際に、電力系統Ｇに供給できるように構成されている点も第１実施形態と異なっているが、その他の特徴は第１実施形態と同様である。 In addition, when the high-temperature exhaust gas of the biogas power generation system heats the circulating heat medium in the heat exchanger 23, condensed water drain D is generated, but this drain water is drained and the exhaust gas containing carbon dioxide gas is generated. The exhaust gas intake compressor 5, which compresses and supplies it to the carbon dioxide gas absorption equipment 8, is operated by the power generated by the biogas power generation system, and when surplus power is generated from the biogas power generation system. , the second embodiment differs from the first embodiment in that it is configured to be able to be supplied to the power system G, but other features are the same as the first embodiment.
このような構成とすることにより、第一実施形態のように地熱蒸気が得られない場所、すなわちバイオマスのメタン発酵プラントや下水処理場等のバイオガス発生地においても、設置場所で得られるバイオガスを利用して、バイオガス発電を行いながら、バイオマス起源の二酸化炭素ガスを分離回収することが可能である。
（第３実施形態）With this configuration, even in places where geothermal steam cannot be obtained as in the first embodiment, that is, biogas generation sites such as biomass methane fermentation plants and sewage treatment plants, the biogas obtained at the installation site can be used. It is possible to separate and recover biomass-derived carbon dioxide gas while generating biogas power using this method.
(Third embodiment)
次に、本発明の第３実施形態に係る、地熱蒸気を活用した大気中の二酸化炭素ガスの分離回収システムについて、図３に基づいて説明する。 Next, a separation and recovery system for atmospheric carbon dioxide gas using geothermal steam according to a third embodiment of the present invention will be described based on FIG. 3.
図３に示すように、第３実施形態のシステムでは、地熱蒸気３が直接、化学吸収液再生設備１２に供給されて化学吸収液の加熱再生に利用されるとともに、前記設備内で汽液分離されて生じた地熱蒸気によって発電を行う地熱発電システム２４から得られる電力によって、二酸化炭素ガスを含有する大気（外気）を吸気送風するガス吸気送風ブロワ２５と、再生後の化学吸収液を冷却するためのターボ冷凍機２６が稼働され、吸引された外気が除塵除湿フィルタ２７を介して供給され、充填剤表面上を流下される化学吸収液が空気中の二酸化炭素ガスを吸収するように構成されている二酸化炭素ガス吸収塔２８となっている点が、第１実施形態と異なっているが、その他の特徴は第１実施形態と同様である。 As shown in FIG. 3, in the system of the third embodiment, geothermal steam 3 is directly supplied to the chemical absorption liquid regeneration equipment 12 and used for heating and regeneration of the chemical absorption liquid, and the steam liquid is separated in the equipment. The gas intake air blower 25 that takes in and blows the atmosphere (outside air) containing carbon dioxide gas and the chemical absorption liquid after regeneration are cooled by the electric power obtained from the geothermal power generation system 24 that generates electricity using the geothermal steam generated by the geothermal steam. The turbo chiller 26 is operated, the outside air is sucked in and supplied through the dust removal and dehumidification filter 27, and the chemical absorption liquid flowing down on the surface of the filler is configured to absorb carbon dioxide gas in the air. This embodiment differs from the first embodiment in that a carbon dioxide gas absorption tower 28 is used, but other features are the same as in the first embodiment.
このような構成とすることにより、第一実施形態のようにバイオマスの収集とメタン発酵が困難な場所、すなわち電力系統の接続が困難な地熱地帯や温泉湧出地帯においても、設置場所で得られる地熱のエネルギーを利用して、大気中の二酸化炭素ガスを分離回収することが可能である。
（第４実施形態）With this configuration, even in places where biomass collection and methane fermentation are difficult as in the first embodiment, i.e. geothermal areas and hot spring gushing areas where it is difficult to connect to the electric power system, geothermal heat obtained at the installation site can be used. Using this energy, it is possible to separate and recover carbon dioxide gas from the atmosphere.
(Fourth embodiment)
次に、本発明の第４実施形態に係る、太陽熱集熱と太陽光発電を活用した、大気中の二酸化炭素ガスの分離回収システムについて、図４に基づいて説明する。 Next, a separation and recovery system for carbon dioxide gas in the atmosphere, which utilizes solar heat collection and solar power generation, according to a fourth embodiment of the present invention will be described based on FIG. 4.
図４に示すように、第４実施形態では、化学吸収液の加熱再生や冷却に利用する再生可能エネルギー熱が、太陽熱集熱器２９によって得られる高温の熱媒流体循環によって供給される点と、システムを稼働する電気設備が、太陽光発電システム３０によって発電された電力が蓄電される蓄電システム３１から供給される再生可能エネルギー電力により賄われる点が第３実施形態と異なっているが、その他の特徴は第３実施形態と同様である。 As shown in FIG. 4, in the fourth embodiment, the renewable energy heat used for heating regeneration and cooling of the chemical absorption liquid is supplied by high temperature heat medium fluid circulation obtained by the solar heat collector 29. , differs from the third embodiment in that the electrical equipment that operates the system is supplied with renewable energy power supplied from a power storage system 31 in which power generated by a solar power generation system 30 is stored, but in other respects. The features of this embodiment are the same as those of the third embodiment.
このような構成とすることにより、第１実施形態や第２実施形態および第３実施形態のように、地熱資源やバイオマス資源がなく、電力系統の接続が困難な場所においても、設置場所で得られる太陽のエネルギーを利用して、大気中の二酸化炭素ガスを分離回収することが可能である。 With this configuration, as in the first, second, and third embodiments, even in places where there are no geothermal resources or biomass resources and where it is difficult to connect to the electric power system, it is possible to obtain benefits at the installation site. It is possible to separate and recover carbon dioxide gas from the atmosphere by using the energy of the sun.
なお本発明は、前記の実施形態に限定されるものではなく、例えば図示した実施形態は二酸化炭素ガスの分離回収に限定されず、化学吸収液の成分等を変更することによって、空気中の窒素や酸素など、他のガスを分離回収して工業用原料ガスとして利用しても良い。 The present invention is not limited to the above-described embodiments. For example, the illustrated embodiment is not limited to the separation and recovery of carbon dioxide gas, and by changing the components of the chemical absorption liquid, nitrogen in the air can be removed. Other gases such as gas and oxygen may be separated and recovered and used as industrial raw material gases.
また、分離回収したバイオメタンは燃料や工業用原料ガスとして利用しても良いし、分離回収した二酸化炭素ガスは、工業用原料ガスとして利用するほか、公知の固定化手段によって固定化することで、化石燃料利用時の排気ガスに含まれる二酸化炭素の回収固定化だけでなく、大気中やバイオマス起源の二酸化炭素を回収して固定化することも可能である。 In addition, the separated and recovered biomethane can be used as fuel or industrial raw material gas, and the separated and recovered carbon dioxide gas can be used as industrial raw material gas or can be fixed by known fixation means. In addition to capturing and fixing carbon dioxide contained in exhaust gas when fossil fuels are used, it is also possible to capture and fix carbon dioxide from the atmosphere and biomass.
このように前記の実施形態は例示であり、本発明の特許請求範囲に記載された技術的思想と実質的に同一な構成を有し、同様な作用効果を奏するものは、いかなるものであっても本発明の技術的範囲に包含される。 As described above, the above-described embodiments are illustrative, and any embodiments having substantially the same configuration as the technical idea stated in the claims of the present invention and producing similar effects may be used. Also included within the technical scope of the present invention.
１・・・・バイオマス資源
２・・・・メタン発酵槽
３・・・・地熱蒸気
４・・・・蒸気タービン
５・・・・ガス吸気圧縮機
６・・・・バイオガス浄化装置
７・・・・化学吸収液
８・・・・二酸化炭素ガス吸収設備
９・・・・微細気泡化ガス供給管
１０・・・バイオメタン抽出管
１１・・・吸収液循環供給ポンプ
１２・・・化学吸収液再生設備
１３・・・加熱再生容器
１４・・・二酸化炭素ガス収集管
１５・・・回収ガス冷却器
１６・・・再生化学吸収液の収集管
１７・・・リッチ液予熱用熱交換器
１８・・・化学吸収液熱交換器
１９・・・リーン液冷却用熱交換器
２０・・・吸着式冷凍機
２１・・・バイナリー発電システム
２２・・・バイオガス発電システム
２３・・・排ガス熱交換器
２４・・・地熱発電システム
２５・・・ガス吸気送風ブロワ
２６・・・ターボ冷凍機
２７・・・除塵除湿フィルタ
２８・・・二酸化炭素ガス吸収塔
２９・・・太陽熱集熱器
３０・・・太陽光発電システム
３１・・・蓄電システム1... Biomass resources 2... Methane fermentation tank 3... Geothermal steam 4... Steam turbine 5... Gas intake compressor 6... Biogas purification device 7... ...Chemical absorption liquid 8...Carbon dioxide gas absorption equipment 9...Fine bubble gas supply pipe 10...Biomethane extraction pipe 11...Absorption liquid circulation supply pump 12...Chemical absorption liquid Regeneration equipment 13... Heating regeneration container 14... Carbon dioxide gas collection pipe 15... Recovered gas cooler 16... Regeneration chemical absorption liquid collection pipe 17... Rich liquid preheating heat exchanger 18. ...Chemical absorption liquid heat exchanger 19...Lean liquid cooling heat exchanger 20...Adsorption refrigerator 21...Binary power generation system 22...Biogas power generation system 23...Exhaust gas heat exchanger 24... Geothermal power generation system 25... Gas intake air blower 26... Turbo chiller 27... Dust removal and dehumidification filter 28... Carbon dioxide gas absorption tower 29... Solar heat collector 30... Solar power generation system 31...Electricity storage system
Claims (12)
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