JPH06211518A - Recovering equipment for carbon dioxide - Google Patents
Recovering equipment for carbon dioxideInfo
- Publication number
- JPH06211518A JPH06211518A JP5005426A JP542693A JPH06211518A JP H06211518 A JPH06211518 A JP H06211518A JP 5005426 A JP5005426 A JP 5005426A JP 542693 A JP542693 A JP 542693A JP H06211518 A JPH06211518 A JP H06211518A
- Authority
- JP
- Japan
- Prior art keywords
- water
- caco
- fed
- gas
- cyclone
- 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.)
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Carbon And Carbon Compounds (AREA)
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
Description
【０００１】本発明は、二酸化炭素の回収設備に関する
ものである。The present invention relates to carbon dioxide recovery equipment.
【０００２】二酸化炭素の吸着設備に関して、特開平４
−１８６１９９号公報や特開平４−１８６２００号公報
の技術が提案されている。これらの技術では、ＣＯ2 ガ
スとＣａ（ＯＨ）2 との化学反応によってＣａＣＯ3 を
生成させて、14Ｃを吸着固化するようにしている。Japanese Patent Application Laid-Open No. Hei.
The techniques disclosed in JP-A-186199 and JP-A-4-186200 are proposed. In these techniques, CaCO 3 is generated by a chemical reaction between CO 2 gas and Ca (OH) 2, and 14 C is adsorbed and solidified.
【０００３】[0003]
【発明が解決しようとする課題】しかし、14Ｃを吸着固
化させる場合にあって、供給されるＣａ（ＯＨ）2 の全
部がＣＯ2 ガスと反応してＣａＣＯ3 となるとは限ら
ず、未反応Ｃａ（ＯＨ）2が発生する。この未反応Ｃａ
（ＯＨ）2 がＣａＣＯ3 とともに固化処理されると、放
射性物質の二次廃棄物を増大させてしまうことになる。However, when 14 C is adsorbed and solidified, not all of the supplied Ca (OH) 2 reacts with CO 2 gas to become CaCO 3, and unreacted. Ca (OH) 2 is generated. This unreacted Ca
If (OH) 2 is solidified together with CaCO 3 , secondary waste of radioactive materials will be increased.
【０００４】[0004]
【発明が解決しようとする課題】本発明は、上記課題を
有効に解決するもので、ＣａＣＯ3 とＣａ（ＯＨ）2 と
の分離性を高めて、二次廃棄物の発生量を低減すること
及びＣａ（ＯＨ）2 の有効利用率の向上を図ることを目
的とするものである。DISCLOSURE OF THE INVENTION The present invention effectively solves the above-mentioned problems by increasing the separability of CaCO 3 and Ca (OH) 2 and reducing the amount of secondary waste generated. The purpose is to improve the effective utilization rate of Ca (OH) 2 .
【０００５】[0005]
【課題を解決するための手段】ＣＯ2 ガスとＣａ（Ｏ
Ｈ）2 との化学反応によりＣａＣＯ3 を生成させる回収
設備であって、Ｃａ（ＯＨ）2 投入量に対する飽和水量
の水を注入する給水量制御手段と、ＣＯ2 ，Ｃａ（Ｏ
Ｈ）2 ，Ｈ2 Ｏ混和物からＣａＣＯ3 を沈澱させるとと
もに未反応Ｃａ（ＯＨ）2 を水に溶解させる沈澱分離槽
と、該沈澱分離槽に接続されＣａ（ＯＨ）2 の溶解液を
回収する再循環手段とを具備する構成としている。[Means for Solving the Problems] CO 2 gas and Ca (O
A chemical reaction recovery equipment to produce CaCO 3 by the H) 2, and water supply amount control means for injecting water saturated water for Ca (OH) 2 dosages, CO 2, Ca (O
A precipitation separation tank for precipitating CaCO 3 from the H) 2 , H 2 O mixture and dissolving unreacted Ca (OH) 2 in water, and a Ca (OH) 2 solution which is connected to the precipitation separation tank and recovered And a recirculation means for
【０００６】[0006]
【作用】ＣＯ2 ガスとＣａ（ＯＨ）2 との化学反応によ
ってＣａＣＯ3 を生成させる際に、水の注入量がＣａ
（ＯＨ）2 の投入量に対する飽和水量で管理され、ＣＯ
2，Ｃａ（ＯＨ）2 ，Ｈ2 Ｏ混和物が、時間経過ととも
に Ｃａ（ＯＨ）2 ＋ＣＯ2 →ＣａＣＯ3 ＋Ｈ2 Ｏ のような化学反応が進行して、ＣＯ2 ガスがＣａＣＯ3
中に取り込まれて固化状態に導かれる。余剰のＣａ（Ｏ
Ｈ）2 は水への溶解度の差に基づいて、ＣａＣＯ3 沈澱
とともに分離して上澄み状態となり、溶解液として回収
されて再循環される。[Function] When CaCO 3 is produced by a chemical reaction between CO 2 gas and Ca (OH) 2 , the amount of water injected is Ca
It is controlled by the saturated water amount relative to the input amount of (OH) 2 , and CO
2 , the Ca (OH) 2 , H 2 O mixture undergoes a chemical reaction such as Ca (OH) 2 + CO 2 → CaCO 3 + H 2 O over time, and CO 2 gas becomes CaCO 3
It is taken in and led to a solidified state. Excess Ca (O
H) 2 is separated along with CaCO 3 precipitation into a supernatant based on the difference in solubility in water, and is recovered as a solution and recycled.
【０００７】[0007]
【実施例】以下、本発明に係る二酸化炭素の回収設備の
一実施例について、図１ないし図３に基づき説明する。
各図において、符号１はＣＯ2 ガス供給系、２はＣａ
（ＯＨ）2 供給系、３は混合反応手段、４はサイクロ
ン、５は給水手段、６は給水量制御手段、７は沈澱分離
槽、８は固液分離器、９は固定化処理系、１０は再循環
手段、１１は濃縮器、１２はＣａ（ＯＨ）2 処理系、１
３は凝縮器、１４はオフガス処理系、１５は粉末化手段
である。EXAMPLES An example of carbon dioxide recovery equipment according to the present invention will be described below with reference to FIGS.
In each figure, reference numeral 1 is a CO 2 gas supply system, and 2 is Ca.
(OH) 2 supply system, 3 is a mixing reaction means, 4 is a cyclone, 5 is a water supply means, 6 is a water supply amount control means, 7 is a precipitation separation tank, 8 is a solid-liquid separator, 9 is an immobilization treatment system, 10 Is a recirculation means, 11 is a condenser, 12 is a Ca (OH) 2 treatment system, 1
3 is a condenser, 14 is an off-gas treatment system, and 15 is a powdering means.
【０００８】これらの詳細について説明すると、ＣＯ2
ガス供給系１にあっては、14Ｃ核種をＣＯ2 ガスに変換
した状態等の被処理ガスを、加圧状態にして下流に供給
するものであり、混合反応手段３に接続される。Explaining these details, CO 2
In the gas supply system 1, a gas to be treated in a state in which 14 C nuclides are converted into CO 2 gas is pressurized and supplied to the downstream side, and is connected to the mixing reaction means 3.
【０００９】前記Ｃａ（ＯＨ）2 供給系２にあっては、
Ｃａ（ＯＨ）2 を粉末化したものを下流に供給するもの
であり、混合反応手段３に接続される。In the Ca (OH) 2 supply system 2,
Powdered Ca (OH) 2 is supplied downstream and is connected to the mixing reaction means 3.
【００１０】前記混合反応手段３にあっては、ＣＯ2 ガ
ス流にＣａ（ＯＨ）2 粉末を重畳させることのよって混
合流とし、以下の化学反応を生じさせるものであり、サ
イクロン４に接続される。 ＣＯ2 ＋Ｃａ（ＯＨ）2 →ＣａＣＯ3 ＋Ｈ2 ＯIn the mixing reaction means 3, a mixture of Ca (OH) 2 powder is superposed on a CO 2 gas flow to form a mixed flow, which causes the following chemical reaction, and is connected to the cyclone 4. It CO 2 + Ca (OH) 2 → CaCO 3 + H 2 O
【００１１】前記サイクロン４にあっては、混合反応手
段３から送り込まれたＣＯ2 ，Ｃａ（ＯＨ）2 ，ＣａＣ
Ｏ3 等の混合流体中の未反応ＣＯ2 を、Ｃａ（ＯＨ）2
と引き続き反応させるとともに、密度差を利用して固体
分のＣａＣＯ3 及び未反応Ｃａ（ＯＨ）2 を分離するも
のであり、沈澱分離槽７に接続される。In the cyclone 4, CO 2 , Ca (OH) 2 , CaC sent from the mixing reaction means 3
Unreacted CO 2 in a mixed fluid such as O 3 is converted into Ca (OH) 2
And CaCO 3 and unreacted Ca (OH) 2 are separated by utilizing the density difference, and are connected to the precipitation separation tank 7.
【００１２】前記給水量制御手段６は、Ｃａ（ＯＨ）2
供給系２、給水手段５及び沈澱分離槽７の間に介在状態
に配されるもので、Ｃａ（ＯＨ）2 供給系２に接続され
る制御部６ａと、該制御部６ａによって作動させられる
フロースイッチ６ｂと、該フロースイッチ６ｂによって
開閉制御される開閉弁６ｃとを有している。The water supply amount control means 6 uses Ca (OH) 2
A control unit 6a connected to the Ca (OH) 2 supply system 2 and a flow operated by the control unit 6a, which is disposed between the supply system 2, the water supply means 5, and the precipitation separation tank 7. It has a switch 6b and an on-off valve 6c whose opening and closing is controlled by the flow switch 6b.
【００１３】前記制御部６ａにあっては、Ｃａ（ＯＨ）
2 の供給重量を検出して、Ｃａ（ＯＨ）2 の飽和水量
と、前述した化学反応によって生成される水分とに基づ
いて、必要給水量（例えば供給重量の３０％程度の給水
量）を演算するとともに、その必要給水量を数分の１に
して少量ずつの給水を複数段階に分けて行なうように設
定される。In the control section 6a, Ca (OH)
By detecting the supply weight of 2, operations and Ca (OH) 2 saturated water, based on the moisture generated by the chemical reaction described above, require water supply amount (e.g. water supply of about 30% of the feed by weight) At the same time, the required amount of water supply is set to a fraction, and small amount of water supply is set in multiple stages.
【００１４】前記沈澱分離槽７にあっては、サイクロン
４の下流に、給水量制御手段６、固液分離器８及び凝縮
器１３に接続状態に配されるもので、サイクロン４から
送り込まれる固形分であるＣａＣＯ3 及び未反応Ｃａ
（ＯＨ）2 に水を加えて、水に対する溶解度の差を利用
して、ＣａＣＯ3 を固体分のまま沈澱させるとともに、
Ｃａ（ＯＨ）2 を水に溶解させた状態にするものであ
る。そして、沈澱分離槽７には、貯留流体の攪拌を行な
うための攪拌手段７ａが配され、攪拌後の沈澱によって
スラッジ層７ｂと液相（溶解液）７ｃとが形成される。The settling separation tank 7 is connected downstream of the cyclone 4 to the water supply amount control means 6, the solid-liquid separator 8 and the condenser 13, and is fed from the cyclone 4. CaCO 3 and unreacted Ca
By adding water to (OH) 2 and utilizing the difference in solubility in water, CaCO 3 is precipitated as a solid component, and
Ca (OH) 2 is dissolved in water. Then, the precipitation separation tank 7 is provided with a stirring means 7a for stirring the stored fluid, and a sludge layer 7b and a liquid phase (dissolved liquid) 7c are formed by the precipitation after stirring.
【００１５】前記固液分離器８は、沈澱分離槽７の底部
に接続されてスラッジ層７ｂを回収し、ＣａＣＯ3 等の
固形分と液分とを分離する機能を備えており、固形分が
固定化処理系９に送り込まれて、例えばドラム缶詰め等
の処分がなされ、液分が再循環手段１０に送り出され
る。The solid-liquid separator 8 is connected to the bottom of the sedimentation separation tank 7 to collect the sludge layer 7b and has a function of separating solid content such as CaCO 3 and liquid content. The liquid is sent to the immobilization processing system 9 and disposed of, for example, drum canned, and the liquid is sent to the recirculation means 10.
【００１６】前記再循環手段１０は、濃縮器１１、Ｃａ
（ＯＨ）2 処理系１２、凝縮器１３及び粉末化手段１５
によって構成される。The recirculation means 10 comprises a condenser 11, Ca
(OH) 2 processing system 12, condenser 13 and powdering means 15
Composed by.
【００１７】前記濃縮器１１は、沈澱分離槽７における
液相７ｃ、固液分離器８、Ｃａ（ＯＨ）2 処理系１２及
び凝縮器１３に接続され、送り込まれた液分等を加熱し
て蒸気化するための加熱源１１ａと、液分中のＣａ量を
分析するためのＣａ分析手段１１ｂとを有しており、液
分の濃縮によって生じたＣａ（ＯＨ）2 等の固形分は、
Ｃａ（ＯＨ）2 処理系１２に送り込まれて再利用され
る。The concentrator 11 is connected to the liquid phase 7c, the solid-liquid separator 8, the Ca (OH) 2 treatment system 12 and the condenser 13 in the precipitation separation tank 7, and heats the fed liquid components and the like. It has a heating source 11a for vaporizing and a Ca analysis means 11b for analyzing the amount of Ca in the liquid, and the solid content such as Ca (OH) 2 produced by the concentration of the liquid is
It is sent to the Ca (OH) 2 processing system 12 and reused.
【００１８】前記凝縮器１３は、沈澱分離槽７と濃縮器
１１との間に介在状態に配され、冷媒供給系１３ａから
冷却水等の供給を受けて蒸気を液体（水）に凝縮し、凝
縮液を沈澱分離槽７に戻して再利用するようにしてい
る。The condenser 13 is interposed between the precipitation separation tank 7 and the condenser 11, and receives cooling water or the like from the refrigerant supply system 13a to condense vapor into a liquid (water), The condensate is returned to the precipitation separation tank 7 for reuse.
【００１９】前記オフガス処理系１４は、図２及び図３
に示すように、サイクロン４の上部に接続され、ＣＯ2
ガスやＣａ（ＯＨ）2 に予め含まれていた空気や、前述
の化学反応時に生じたガス等のいわゆるオフガスが送り
込まれて、放射性物質の除去等の必要な処理を行なうも
のである。The off-gas processing system 14 is shown in FIGS.
As shown in, connected to an upper portion of the cyclone 4, CO 2
Gas or air previously contained in Ca (OH) 2 or so-called off-gas such as gas generated during the above-mentioned chemical reaction is fed to perform necessary processing such as removal of radioactive substances.
【００２０】前記混合反応手段３及び粉末化手段１５に
ついて以下説明を補足する。図２例の粉末化手段１５に
あっては、サイクロン４の下部と混合反応手段（エジェ
クタ）３との間に、介在状態にかつＣａ（ＯＨ）2 供給
系２に接続状態に配され、サイクロン４で生成されたス
ラッジ等を粉末にして、Ｃａ（ＯＨ）2 供給系２から供
給されるＣａ（ＯＨ）2 粉末に混合するようにしてい
る。図３例の粉末化手段１５にあっては、混合反応手段
３の部分に流動槽が適用され、ＣＯ2 ガス供給系１から
供給されるＣＯ2 ガス流によって、粉末化手段１５から
送り込まれる粉末をＣａ（ＯＨ）2 とともに流動化して
前述の化学反応を生じさせ、かつ、流動体をサイクロン
４に送り込んで分別を行なうようにしている。The following will supplement the description of the mixing reaction means 3 and the powdering means 15. In the powdering means 15 of the example in FIG. 2, the cyclone 4 is disposed between the lower part and the mixing reaction means (ejector) 3 in an intervening state and in a connected state to the Ca (OH) 2 supply system 2 to provide a cyclone. The sludge and the like produced in step 4 are made into powder and mixed with the Ca (OH) 2 powder supplied from the Ca (OH) 2 supply system 2. In the powdering means 15 of the example in FIG. 3, a fluidized tank is applied to the part of the mixing reaction means 3, and the powder fed from the powdering means 15 by the CO 2 gas flow supplied from the CO 2 gas supply system 1. Is fluidized with Ca (OH) 2 to cause the above-mentioned chemical reaction, and the fluid is sent to the cyclone 4 for separation.
【００２１】このように構成されている放射化二酸化炭
素の吸着設備では、ＣＯ2 ガス供給系１及びＣａ（Ｏ
Ｈ）2 供給系２の作動によって、混合反応手段３からＣ
Ｏ2 ガス，Ｃａ（ＯＨ）2 粒体及び生成ＣａＣＯ3 の混
合流体がサイクロン４に送り込まれると、固体分である
ＣａＣＯ3 及び未反応Ｃａ（ＯＨ）2 が遠心力によって
分離分割されて、サイクロン４の内周面に集積した状態
となり、この際の攪拌作用によっても前述の化学反応が
生じて、ＣＯ2 ガスのＣａＣＯ3 への取り込みが行なわ
れる。そして、分別された固体分は、自身の重量によっ
てサイクロン４の底部に次第に集積する。In the activated carbon dioxide adsorption facility constructed in this way, the CO 2 gas supply system 1 and Ca (O
H) 2 supply system 2 is actuated so that C
When a mixed fluid of O 2 gas, Ca (OH) 2 granules and generated CaCO 3 is sent to the cyclone 4, solid components CaCO 3 and unreacted Ca (OH) 2 are separated and divided by the centrifugal force, and the cyclone is separated. In the state of being accumulated on the inner peripheral surface of No. 4, the above-mentioned chemical reaction also occurs due to the stirring action at this time, and CO 2 gas is taken into CaCO 3 . Then, the separated solid content gradually accumulates at the bottom of the cyclone 4 due to its own weight.
【００２２】給水量制御手段６を作動状態にすると、Ｃ
ａ（ＯＨ）2 供給系２から混合反応手段３へ供給された
Ｃａ（ＯＨ）2 の重量の検出信号に基づいて、前述した
ように、Ｃａ（ＯＨ）2 量に対応する飽和水量が求めら
れるとともに、化学反応によって生成される水分を考慮
し、かつ、必要水量を若干上回る給水量（例えば前述し
た如くＣａ（ＯＨ）2 重量の３０％見当の給水量）が演
算され、さらに、給水を複数段階に分けて行なうための
第１回目の給水量（例えばＣａ（ＯＨ）2 重量の１５％
見当の給水量）が演算される。When the water supply amount control means 6 is activated, C
As described above, the saturated water amount corresponding to the Ca (OH) 2 amount is obtained based on the detection signal of the weight of Ca (OH) 2 supplied from the a (OH) 2 supply system 2 to the mixing reaction means 3. At the same time, considering the water generated by the chemical reaction, and calculating a water supply amount slightly exceeding the required water amount (for example, the water supply amount of 30% of Ca (OH) 2 weight as described above) is calculated. Water supply for the first time (eg 15% of Ca (OH) 2 weight)
The estimated water supply amount) is calculated.
【００２３】この演算結果に基づいて、給水手段５から
沈澱分離槽７への給水がなされ、給水量の変化はフロー
スイッチ６ｂによって検出されて、その積算量が第１回
目の設定給水量に達すると、フロースイッチ６ｂの検出
信号によって開閉弁６ｃが閉塞状態とされ、第１回目の
給水が停止する。Based on the result of this calculation, water is supplied from the water supply means 5 to the settling separation tank 7, and a change in the water supply amount is detected by the flow switch 6b, and the accumulated amount reaches the first set water supply amount. Then, the open / close valve 6c is closed by the detection signal of the flow switch 6b, and the first water supply is stopped.
【００２４】給水後には、サイクロン４から粉末及びス
ラッジ状のＣａＣＯ3 等の固形分が沈澱分離槽７に供給
され、攪拌手段７ａの作動によって水との攪拌がなされ
る。ＣａＣＯ3 等の固形分が水に溶解する際には発熱を
伴うことになるが、固形分の量の調整や、前述のように
給水を複数段階に分けることによって対処される。After the water is supplied, solids such as powder and sludge-like CaCO 3 are supplied from the cyclone 4 to the precipitation separation tank 7, and are stirred with water by the operation of the stirring means 7a. When a solid content such as CaCO 3 is dissolved in water, heat is generated, which can be dealt with by adjusting the amount of the solid content or dividing the water supply into a plurality of stages as described above.
【００２５】攪拌後には、第２回目の給水がなされ、さ
らに攪拌される。これらの固形分と水との混合によっ
て、未反応状態のＣａ（ＯＨ）2 やＣａＣＯ3 等が水に
溶解する。水に対する溶解度は、Ｃａ（ＯＨ）2 の方が
ＣａＣＯ3 より著しく高い（温度によって差があるもの
の例えば数倍以上である）ために、スラッジ層７ｂには
主としてＣａＣＯ3 が集積し、液相７ｃには主としてＣ
ａ（ＯＨ）2 が溶解して分離状態となる。なお、水への
ＣａＣＯ3 の溶解度は、Ｃａ（ＯＨ）2 の溶解によって
抑制される傾向を生じる。After the stirring, the water is supplied for the second time and further stirred. By mixing these solids with water, unreacted Ca (OH) 2 and CaCO 3 are dissolved in water. Since the solubility in water of Ca (OH) 2 is significantly higher than that of CaCO 3 (for example, several times or more although there is a difference depending on temperature), CaCO 3 is mainly accumulated in the sludge layer 7b and the liquid phase 7c Mainly C
a (OH) 2 is dissolved and becomes a separated state. The solubility of CaCO 3 in water tends to be suppressed by the dissolution of Ca (OH) 2 .
【００２６】したがって、上澄み状態の液相７ｃにあっ
ては、濃縮器１１に移送して蒸発、凝縮によって得られ
る水分を沈澱分離槽７に戻す再循環を行ない、水分を除
去した固形分、主としてＣａ（ＯＨ）2 にあっては、固
体状態のものをＣａ（ＯＨ）2 処理系１２で回収して、
Ｃａ（ＯＨ）2 供給系２からのＣａ（ＯＨ）2 供給ライ
ンに合流させる等の処理がなされる。これらの処理によ
って、分離沈澱に使用されたＣａ（ＯＨ）2 の未反応及
び水は、繰り返し利用されることになる。Therefore, in the liquid phase 7c in the supernatant state, the water obtained by transferring to the concentrator 11 and evaporating and condensing is returned to the settling separation tank 7 for recirculation, and the solid content from which water is removed, mainly For Ca (OH) 2 , the solid state is recovered by the Ca (OH) 2 processing system 12,
Processing such as joining the Ca (OH) 2 supply line from the Ca (OH) 2 supply system 2 is performed. By these treatments, the unreacted Ca (OH) 2 and water used for the separation and precipitation are reused.
【００２７】〔他の実施態様〕本発明に係る二酸化炭素
の回収設備にあっては、実施例に代えて次の技術を採用
することができる。 ａ）沈澱分離槽７への給水分割数を任意とすること。 ｂ）沈澱分離槽７への給水及び固形分の供給を、発熱量
が許容される範囲で少量ずつ連続的に行なうこと。[Other Embodiments] In the carbon dioxide recovery equipment according to the present invention, the following technique can be adopted instead of the embodiment. a) The number of divisions of water supply to the precipitation separation tank 7 is arbitrary. b) The water supply and the solid content supply to the precipitation separation tank 7 are continuously carried out little by little within a range where the calorific value is allowed.
【００２８】[0028]
【発明の効果】本発明に係る二酸化炭素の回収設備によ
れば、以下の効果を奏する。 （１） Ｃａ（ＯＨ）2 量に対応して飽和水量に基づく
給水がなされて、沈澱分離槽において主として固形分で
あるＣａＣＯ3 と未反応のＣａ（ＯＨ）2 の水溶液とを
分離させるものであるから、未反応Ｃａ（ＯＨ）2 の大
部分を液状態で回収して再利用することができる。 （２） 沈澱分離槽からＣａＣＯ3 をスラッジ状態で回
収することにより、ＣａＣＯ3 を固体として回収処分す
ることが容易となる。The carbon dioxide recovery facility according to the present invention has the following effects. (1) Water is supplied based on the amount of saturated water corresponding to the amount of Ca (OH) 2 to separate mainly CaCO 3 which is a solid content and an unreacted aqueous solution of Ca (OH) 2 in a precipitation separation tank. Therefore, most of unreacted Ca (OH) 2 can be recovered in a liquid state and reused. (2) By recovering CaCO 3 in the form of sludge from the precipitation separation tank, it becomes easy to recover and dispose of CaCO 3 as a solid.
【図１】本発明に係る二酸化炭素の回収設備の一実施例
を示す配管系統図である。FIG. 1 is a piping system diagram showing an embodiment of a carbon dioxide recovery facility according to the present invention.
【図２】図１の混合反応手段の例を示す配管系統図であ
る。FIG. 2 is a piping system diagram showing an example of the mixing reaction means of FIG.
【図３】図２の他の例を示す配管系統図である。FIG. 3 is a piping system diagram showing another example of FIG.
１ ＣＯ2 ガス供給系 ２ Ｃａ（ＯＨ）2 供給系 ３ 混合反応手段 ４ サイクロン ５ 給水手段 ６ 給水量制御手段 ６ａ 制御部 ６ｂ フロースイッチ ６ｃ 開閉弁 ７ 沈澱分離槽 ７ａ 攪拌手段 ７ｂ スラッジ ７ｃ 液相（溶解液） ８ 固液分離器 ９ 固定化処理系 １０ 再循環手段 １１ 濃縮器 １１ａ 加熱源 １１ｂ Ｃａ分析手段 １２ Ｃａ（ＯＨ）2 処理系 １３ 凝縮器 １３ａ 冷媒供給系 １４ オフガス処理系 １５ 粉末化手段1 CO 2 gas supply system 2 Ca (OH) 2 supply system 3 mixing reaction means 4 cyclone 5 water supply means 6 water supply amount control means 6a control section 6b flow switch 6c open / close valve 7 precipitation separation tank 7a stirring means 7b sludge 7c liquid phase ( Solution) 8 Solid-liquid separator 9 Immobilization treatment system 10 Recirculation means 11 Concentrator 11a Heat source 11b Ca analysis means 12 Ca (OH) 2 treatment system 13 Condenser 13a Refrigerant supply system 14 Off-gas treatment system 15 Powderization means
Claims (1)
応によりＣａＣＯ3を生成させる回収設備であって、Ｃ
ａ（ＯＨ）2 投入量に対する飽和水量の水を注入する給
水量制御手段と、ＣＯ2 ，Ｃａ（ＯＨ）2 ，Ｈ2 Ｏ混和
物からＣａＣＯ3 を沈澱させるとともに未反応Ｃａ（Ｏ
Ｈ）2 を水に溶解させる沈澱分離槽と、該沈澱分離槽に
接続されＣａ（ＯＨ）2 の溶解液を回収する再循環手段
とを具備することを特徴とする二酸化炭素の回収設備。1. A recovery facility for producing CaCO 3 by a chemical reaction between CO 2 gas and Ca (OH) 2 , which comprises C
A water supply amount control means for injecting a saturated amount of water with respect to the a (OH) 2 input amount, CaCO 3 is precipitated from the CO 2 , Ca (OH) 2 , H 2 O mixture, and unreacted Ca (O
A carbon dioxide recovery facility, comprising: a precipitation separation tank for dissolving H) 2 in water; and a recirculation unit connected to the precipitation separation tank for recovering a Ca (OH) 2 solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP00542693A JP3395228B2 (en) | 1993-01-14 | 1993-01-14 | Carbon dioxide capture facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP00542693A JP3395228B2 (en) | 1993-01-14 | 1993-01-14 | Carbon dioxide capture facility |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06211518A true JPH06211518A (en) | 1994-08-02 |
| JP3395228B2 JP3395228B2 (en) | 2003-04-07 |
Family
ID=11610851
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP00542693A Expired - Fee Related JP3395228B2 (en) | 1993-01-14 | 1993-01-14 | Carbon dioxide capture facility |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3395228B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2002007858A1 (en) * | 2000-07-25 | 2002-01-31 | Oliveira Rodrigues Jose Manuel | Center for purifying, washing and treating fumes ashes |
| WO2004113226A1 (en) * | 2003-06-18 | 2004-12-29 | Kabushiki Kaisha Toshiba | System and method for collecting carbon dioxide in exhaust gas |
| JP2009274893A (en) * | 2008-05-13 | 2009-11-26 | Hideki Yamamoto | METHOD FOR DETOXIFYING HFC-134a AND PREPARATION METHOD OF CALCIUM CARBONATE |
| JP2010202433A (en) * | 2009-03-02 | 2010-09-16 | Hideki Yamamoto | Method for recovering calcium fluoride |
-
1993
- 1993-01-14 JP JP00542693A patent/JP3395228B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2002007858A1 (en) * | 2000-07-25 | 2002-01-31 | Oliveira Rodrigues Jose Manuel | Center for purifying, washing and treating fumes ashes |
| WO2004113226A1 (en) * | 2003-06-18 | 2004-12-29 | Kabushiki Kaisha Toshiba | System and method for collecting carbon dioxide in exhaust gas |
| JP2009274893A (en) * | 2008-05-13 | 2009-11-26 | Hideki Yamamoto | METHOD FOR DETOXIFYING HFC-134a AND PREPARATION METHOD OF CALCIUM CARBONATE |
| JP2010202433A (en) * | 2009-03-02 | 2010-09-16 | Hideki Yamamoto | Method for recovering calcium fluoride |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3395228B2 (en) | 2003-04-07 |
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