JPS6397214A - Method for separating and recovering high-purity co2 from co2-containing gas - Google Patents
Method for separating and recovering high-purity co2 from co2-containing gasInfo
- Publication number
- JPS6397214A JPS6397214A JP61245103A JP24510386A JPS6397214A JP S6397214 A JPS6397214 A JP S6397214A JP 61245103 A JP61245103 A JP 61245103A JP 24510386 A JP24510386 A JP 24510386A JP S6397214 A JPS6397214 A JP S6397214A
- Authority
- JP
- Japan
- Prior art keywords
- adsorption
- gas
- adsorption tower
- pressure
- tower
- 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
- 238000000034 method Methods 0.000 title claims description 26
- 238000001179 sorption measurement Methods 0.000 claims abstract description 69
- 239000012535 impurity Substances 0.000 claims abstract description 10
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 239000003463 adsorbent Substances 0.000 claims description 18
- 230000001172 regenerating effect Effects 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 40
- 235000011089 carbon dioxide Nutrition 0.000 description 40
- 239000007789 gas Substances 0.000 description 39
- 238000003795 desorption Methods 0.000 description 9
- 239000010457 zeolite Substances 0.000 description 9
- 229910021536 Zeolite Inorganic materials 0.000 description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000002336 sorption--desorption measurement Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000009849 vacuum degassing Methods 0.000 description 2
- -1 and as in the past Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 235000014214 soft drink Nutrition 0.000 description 1
- 238000003466 welding Methods 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野コ
本発明は製鉄所で大量に副生ずる高炉ガス（以下ＢＦＧ
という）や転炉ガス（以下ＬＤＧという）等ＣＯ２含有
ガスに圧力スイング法（以下ＰＳＡ法という）を適用し
てＣＯ２を高純度で分離回収する方法に関するものであ
る。[Detailed Description of the Invention] [Industrial Field of Application] The present invention is directed to blast furnace gas (hereinafter referred to as BFG), which is produced in large quantities as a by-product in steel plants.
The present invention relates to a method for separating and recovering CO2 with high purity by applying a pressure swing method (hereinafter referred to as PSA method) to CO2-containing gas such as converter gas (hereinafter referred to as LDG) and converter gas (hereinafter referred to as LDG).
［従来の技術］
ＣＯ２の主な用途としては溶接シールド用、清涼飲料用
、ドライアイス用および底吹転炉用等がある。従来これ
らに用いられているＣＯ２源はアンモニア合成の際の副
生ガス、及び石油精製の際のオフガスから回収されるも
のが主であり、両者を合せると工業上生産されているＣ
Ｏ２の８０％以上を占めることになる。そしてその回収
方法としてはアルカノールアミン法、熱炭酸カリ法、カ
タカープ法等の液吸収法が利用されている。[Prior Art] Main uses of CO2 include welding shields, soft drinks, dry ice, and bottom blowing converters. Conventionally, the CO2 sources used in these systems are mainly those recovered from by-product gas during ammonia synthesis and off-gas during oil refining, and when these two are combined, industrially produced CO2
This accounts for over 80% of O2. Liquid absorption methods such as the alkanolamine method, the hot potassium carbonate method, and the Katakarp method are used as recovery methods.
［発明が解決しようとする問題点コ
しかしながら前記したこれらの方法はいずれも液吸収法
であり、設備費が高くつくこと、吸収液の再生や循環に
多大な蒸気や電力を必要としランニングコストが高くつ
くこと、また液体であるため取扱いが煩雑となる等問題
を有していた。[Problems to be solved by the invention] However, all of the above-mentioned methods are liquid absorption methods, which require high equipment costs and require a large amount of steam and electricity to regenerate and circulate the absorption liquid, resulting in high running costs. It has had problems such as being expensive and being complicated to handle because it is a liquid.
さらに近年アンモニア合成プラントおよび石油精製プラ
ントは産業構造の変化に伴って縮小される傾向にあり、
新しいＣＯ２源の確保が必要となってきた。こうして着
目されたのが製鉄所から大量に副生されるＢＦＧやＬＤ
Ｇであり、これ等のＣＯ２含有ガスから高純度でＣＯ２
を分離回収できれば工業上大いに有益である。Furthermore, in recent years, ammonia synthesis plants and oil refinery plants have tended to be downsized due to changes in the industrial structure.
It has become necessary to secure new CO2 sources. In this way, attention was focused on BFG and LD, which are produced in large quantities by steel mills.
G, and CO2 can be extracted with high purity from these CO2-containing gases.
It would be of great industrial benefit if it could be separated and recovered.
本発明はこのような環境下で検討されたものであって本
発明の目的はＰＳＡ法を利用して、ＣＯ２含有ガス中の
ＣＯ２を高純度で安価に分離回収することのできるＣＯ
２含有ガスからのＣＯ２の分離回収方法を提供すること
にある。The present invention was studied under such an environment, and the purpose of the present invention is to create a CO2 system that can separate and recover CO2 in CO2-containing gas with high purity and at low cost by using the PSA method.
An object of the present invention is to provide a method for separating and recovering CO2 from a gas containing CO2.
［問題点を解決するための手段］
上記問題点を解決することのできた本発明とは吸着塔を
２基以上並列させた圧力スイング吸着装置にＣＯ２含有
ガスを導入してＣＯ２含有ガス中のＣＯ２を回収するに
当たり、湿分およびＳ分を含有した状態のＣＯ２含有ガ
スを加圧下にＣＯ２吸着塔内に導入した後、該吸着塔内
を減圧して該吸着塔内の死空間に充満している不純ガス
成分を排気し、さらに軽度に真空引きして吸着剤に吸着
されている不純物含有ＣＯ２を脱着させて更に高真空に
真空引きして高純度のＣＯ２を回収すると共に前記吸着
塔内に一部残留している湿分およびＳ分を他の吸着塔の
吸着サイクルにおける吸着塔通過ガスによって脱着し、
吸着剤を再生するとともにＣＯ２の回収率を向上させる
ことを構成要旨とするものである。[Means for Solving the Problems] The present invention that can solve the above problems is to introduce CO2-containing gas into a pressure swing adsorption device in which two or more adsorption towers are arranged in parallel. To recover CO2, a CO2-containing gas containing moisture and S is introduced into a CO2 adsorption tower under pressure, and then the pressure inside the adsorption tower is reduced to fill the dead space within the adsorption tower. The impurity gas components contained in the gas are evacuated, and the impurity-containing CO2 adsorbed by the adsorbent is further evacuated by a slight vacuum, and the impurity-containing CO2 adsorbed by the adsorbent is desorbed. Partially remaining moisture and S content are desorbed by the gas passing through the adsorption tower in the adsorption cycle of another adsorption tower,
The main purpose of this system is to regenerate the adsorbent and improve the CO2 recovery rate.
［作用コ
以下、ＣＯ２含有ガスの代表例としてＢＦＧの場合で説
明する。[Effects] Below, the case of BFG will be explained as a representative example of CO2-containing gas.
本発明方法を実施するための主要部は、第１図（ａ）〜
（ｅ）に示すように■ＢＦＧを圧縮して吸着塔１に導入
するための圧縮機２、■ＣＯ２を選択吸着する吸着剤の
充填された吸着塔１（第１図では３ （ＩＡ、ＩＢ、Ｉ
Ｃ）塔であるが、２塔以上を並列配置したものは全て本
発明に含まれる）、及び■選択眼着されたＣＯ２を減圧
脱着するための減圧機３より構成されこれらが配管によ
って接続される。The main parts for carrying out the method of the present invention are shown in FIGS.
As shown in (e), ■ A compressor 2 compresses BFG and introduces it into the adsorption tower 1, ■ An adsorption tower 1 filled with an adsorbent that selectively adsorbs CO2 (3 in Fig. 1 (IA, IB , I
(C) towers, but all towers in which two or more towers are arranged in parallel are included in the present invention); and (2) a pressure reducing machine 3 for depressurizing and desorbing CO2 that has been selectively deposited, and these are connected by piping. Ru.
吸着塔１内に充填される吸着剤は、１０八以上の細孔径
を有し、且つ細孔容積の大きいものが望ましい。このよ
うな例として、Ｘ型ゼオライトＮａＸが挙げられる。こ
のゼオライトＮａＸは第２図に示した等部下の吸脱着圧
と吸脱着量の関係図から明らかである様に、ＣＯ２の吸
着量が多い反面ＣＯ、Ｎ２．Ｈ２の吸着量が少なく、ま
た脱着が吸着より容易であり、圧力スイングに好適な吸
着剤であることが分かる。またＢＦＧの主成分は第１表
に示すとおりであり、その他に湿分（Ｈ２０）と微量の
Ｓ分が含まれているがＣＯ２回収用資源として有用であ
ることが分かる。The adsorbent filled in the adsorption tower 1 preferably has a pore diameter of 108 or more and a large pore volume. An example of this is type X zeolite NaX. As is clear from the relationship between adsorption and desorption pressure and adsorption and desorption amount shown in Figure 2, this zeolite NaX has a large adsorption amount of CO2, but on the other hand, it has a high adsorption amount of CO2 and N2. It can be seen that the amount of H2 adsorbed is small, and desorption is easier than adsorption, making it a suitable adsorbent for pressure swings. The main components of BFG are as shown in Table 1, and it also contains moisture (H20) and a trace amount of S, but it is understood that it is useful as a resource for CO2 recovery.
第 １ 表
以下第１図（ａ）〜（ｅ）を参照しつつ本発明方法を構
成するプロセスについて具体的に述べる。Table 1 Below, the processes constituting the method of the present invention will be specifically described with reference to FIGS. 1(a) to (e).
（１）吸着工程；原料ＢＦＧを圧縮機２にて圧縮し、ア
フタークーラー４で温度を調整した後吸着塔ＩＡ内に導
入し所定圧力まで昇圧する。この際吸着塔ＩＡのガス排
出部から排出されてくる通過排ガス中のＣＯ□濃度を測
定しておき、吸着塔ＩＡのガス入口部における原料ＢＦ
Ｇ中のＣＯ３濃度と同じになるまでＢＦＧを導入し吸着
剤にＣＯ２を吸着させる［第１図（ａ）太線原料ＢＦＧ
から吸着塔ＩＡまでコ。(1) Adsorption step: Raw material BFG is compressed by the compressor 2, and after adjusting the temperature by the aftercooler 4, it is introduced into the adsorption tower IA and the pressure is increased to a predetermined pressure. At this time, the CO□ concentration in the passing exhaust gas discharged from the gas discharge part of the adsorption tower IA is measured, and the
BFG is introduced until the concentration of CO3 in G and the adsorbent adsorbs CO2 [Figure 1 (a) thick line raw material BFG
from adsorption tower IA.
吸着圧力は第２図（吸脱着平衡分圧と吸脱着量との関係
図）に示す吸脱着等温線から明らかなように高いほどＣ
Ｏ２分圧が高くなりＣＯ２の吸着量は増加するが、吸着
圧力を高くすることはガス圧縮のためのエネルギーコス
トが高くなるので吸着圧はＣＯ２吸脱着等混線と吸着量
から判断して（１，５〜２ ｋｇ／ｃ＋ｎ２・Ｇが望ま
しい。The higher the adsorption pressure is, the more C
As the O2 partial pressure increases, the adsorption amount of CO2 increases, but increasing the adsorption pressure increases the energy cost for gas compression, so the adsorption pressure is determined from the crosstalk such as CO2 adsorption and desorption and the adsorption amount (1 , 5 to 2 kg/c+n2·G is desirable.
吸着塔通過ガスは他塔の昇圧再生工程（後述する）を経
てレストガスとして排気（回収）される［第１図（ａ）
太線吸着塔ＩＡからＩＢを経てレストガスまで］。The gas passing through the adsorption tower is exhausted (recovered) as rest gas through a pressure raising regeneration process (described later) in other towers [Figure 1 (a)
thick line from adsorption tower IA to rest gas via IB].
（２）減圧工程：＠、着工程終了後、大気圧まで減圧し
て吸着塔ＩＡ内の死空間に充満している不純ガス成分を
吸着塔ＩＡから排気する［第１図（ｂ）太線］。(2) Pressure reduction step: After the completion of the deposition step, the pressure is reduced to atmospheric pressure and the impure gas components filling the dead space in the adsorption tower IA are exhausted from the adsorption tower IA [Figure 1 (b) thick line] .
（３）初期真空脱着工程：減圧工程終了後減圧機３にて
７ＣＯ ｔｏｒｒまで減圧するが、この初期真空脱着に
よって脱着されるガス（ＣＯ２を多量に含み不純物とし
てＮ２．ＣＯ、Ｈ２，、Ｓ分等を含むガス）は、吸着塔
ＩＡ内から排出される［第１図（ｃ）太線コ。(3) Initial vacuum desorption process: After the completion of the depressurization process, the pressure is reduced to 7CO torr using the pressure reducer 3, but the gas (containing a large amount of CO2 and containing N2, CO, H2, and S as impurities) is desorbed by this initial vacuum desorption. etc.) is discharged from the adsorption tower IA [Fig. 1(c) thick line C].
（４）真空脱着工程−減圧機３にて吸着塔内をさらに減
圧して吸着剤に吸着しているＣＯ２を脱着させ製品とし
て回収する。この際の真空度は３０〜２ＣＯ ｔｏｒｒ
が望ましい［第１図（ｄ）の太線］。(4) Vacuum desorption step - The pressure inside the adsorption tower is further reduced by the pressure reducer 3 to desorb the CO2 adsorbed on the adsorbent and recover it as a product. The degree of vacuum at this time is 30-2CO torr
is desirable [thick line in Figure 1(d)].
（５）昇圧再生工程：他塔ＩＣの吸着工程で排出される
吸着塔通過ガスを吸着塔通過ガス出口側から導入し、吸
着塔のＢＦＧ入口部に一部残留しているＨ２Ｏ及びＳ分
を脱着し吸着剤の再生を行なうと共に塔内を昇圧して次
回吸着工程に備える。また、前記吸着塔通過ガスはＣＯ
２を含んでおり、これを回収することによりＣＯ７回収
率を向上させる役目ももつ。吸着塔内を通過したガスは
レストガスとして排気あるいは回収される［第１図（ｅ
）太線吸着塔ＩＣから吸着塔ＩＡを経てレストガスまで
］。このレストガスはＣＯ２をわずかしか含まないので
単位量当たりのカロリーが高いものとして別途回収の対
象となり得る。(5) Pressure boosting regeneration step: The gas passing through the adsorption tower discharged in the adsorption process of the other tower IC is introduced from the outlet side of the gas passing through the adsorption tower, and the H2O and S components partially remaining at the BFG inlet of the adsorption tower are removed. The adsorbent is desorbed and regenerated, and the pressure inside the column is increased to prepare for the next adsorption step. Further, the gas passing through the adsorption tower is CO
It also has the role of improving the CO7 recovery rate by recovering it. The gas that has passed through the adsorption tower is exhausted or recovered as rest gas [Figure 1 (e
)Thick line from adsorption tower IC to rest gas via adsorption tower IA]. Since this rest gas contains only a small amount of CO2, it can be separately collected as having a high calorie per unit amount.
なお脱水、脱硫の効率を高めるため、ゼオライトＮａＸ
と異なる細孔を有するゼオライトや活性炭等の吸着剤を
吸着塔のＢＦＧ入口部に充填しても良い。In order to improve the efficiency of dehydration and desulfurization, zeolite NaX
The BFG inlet of the adsorption tower may be filled with an adsorbent such as zeolite or activated carbon having pores different from those of the adsorbent.
以上のようなＣＯ２回収を３塔の吸着塔を用いた場合の
サイクルパターンの例を第２表に示す。Table 2 shows an example of a cycle pattern when three adsorption towers are used for CO2 recovery as described above.
第 ２ 表
以上のように２塔以上の吸着塔を並列配置して交互に吸
着、脱着を行なうことにより製品ＣＯ２ガスを連続的に
回収することができる。As shown in Table 2, product CO2 gas can be continuously recovered by arranging two or more adsorption towers in parallel and performing adsorption and desorption alternately.
また、本発明においては、吸着剤として市販のゼオライ
トを使用するので吸着剤を安価にしかも容易に入手でき
る。また設備的にも主要部が圧縮機、吸着塔、減圧機で
構成され、従来のように不純物（特に水分および３分）
除去のための前処理をする必要がなく、また製品純度を
高めるための製品ガスによる洗浄工程を設けることもな
いので設備面積が小さくなり、建設費も安価になる。Furthermore, in the present invention, since commercially available zeolite is used as the adsorbent, the adsorbent can be obtained at low cost and easily. In addition, the main parts of the equipment are a compressor, an adsorption tower, and a pressure reducer, and as in the past, impurities (especially moisture and
There is no need for pretreatment for removal, and there is no need to provide a cleaning process using product gas to improve product purity, so the equipment area is small and construction costs are low.
また吸着工程での吸着圧も低圧で良くランニングコスト
の点でも有益でありＰＳＡ法を用いるので運転保持が容
易である。In addition, the adsorption pressure in the adsorption step is low, which is beneficial in terms of running costs, and since the PSA method is used, operation maintenance is easy.
尚本発明方法では原料ガスとしてＢＦＧを用いているが
、転炉ガスその他ＣＯ２含有混合ガスにも適用できる。Although BFG is used as the raw material gas in the method of the present invention, it can also be applied to converter gas and other CO2-containing mixed gases.
［実施例コ
市販ＮａＸ型ゼオライトＡ、Ｂ各１５０ｍＪｌを充填し
た内径２８ｍｍ、高さ３ＣＯｍｍの吸着塔に第３表に示
す組成の混合ガスを圧力１ ｋｇ／ｃｍ２・Ｇ流量ｉｎ
／ｍｉｎ、温度２０℃の条件で導入した。[Example] A mixed gas having the composition shown in Table 3 was charged into an adsorption tower with an inner diameter of 28 mm and a height of 3 CO mm filled with 150 mJl each of commercially available NaX type zeolites A and B at a pressure of 1 kg/cm2・G flow rate in
/min and the temperature was 20°C.
第 ３ 表
吸着塔内の吸着剤に吸着されたｃｏ２ｔｌＡ度が一定に
なった時点でガス導入を停止し、大気圧まで減圧した。Table 3 When the degree of co2tlA adsorbed on the adsorbent in the adsorption tower became constant, gas introduction was stopped and the pressure was reduced to atmospheric pressure.
次に真空ポンプを用いて７ＣＯ ｔｏｒｒまで段階的に
吸着塔内を減圧し初期真空脱気を行なったのち、吸着塔
内をさらに５０ ｔｏｒｒまで減圧してＣＯ２を脱着さ
せ製品ＣＯ２を回収した。ゼオライトＡおよびゼオライ
トＢにおける初期真空脱気量と回収製品ガス組成を第４
表および第５表に示す。Next, the pressure inside the adsorption tower was reduced stepwise to 7 CO torr using a vacuum pump to perform initial vacuum degassing, and then the pressure inside the adsorption tower was further reduced to 50 torr to desorb CO2 and recover product CO2. The initial vacuum degassing amount and recovered product gas composition in zeolite A and zeolite B were
It is shown in Table and Table 5.
第４表および第５表から明らかなように製品中のＣＯ３
濃度は高く、また初期真空脱着を行なう第 ４ 表
（ゼオライトＡ）
第 ５ 表 （ゼオライトＢ）
［発明の効果］
以上のように本発明方法によればＢＦＧをはじめとする
各種のＣＯ２含有ガスからＣＯ２を高純度かつ安価に分
離回収することができる。As is clear from Tables 4 and 5, CO3 in products
The concentration is high and initial vacuum desorption is performed.Table 4
(Zeolite A) Table 5 (Zeolite B) [Effects of the Invention] As described above, according to the method of the present invention, CO2 can be separated and recovered from various CO2-containing gases including BFG at high purity and at low cost. .
第１図（ａ） 、 （ｂ） 、 （ｃ） 、 （ｄ
） 、 （ｅ）は本発明方法を行なうための構成図例
、第２図は等温におりる吸脱着平衡分圧と吸脱着量との
関係図である。Figure 1 (a), (b), (c), (d
) and (e) are examples of the configuration for carrying out the method of the present invention, and FIG. 2 is a diagram showing the relationship between the adsorption/desorption equilibrium partial pressure and the amount of adsorption/desorption at an isothermal state.
Claims (1)
Ｏ＿２含有ガスを導入してＣＯ＿２含有ガス中のＣＯ＿
２を回収するに当たり、湿分およびＳ分を含有した状態
のＣＯ＿２含有ガスを加圧下にＣＯ＿２吸着塔内に導入
した後、該吸着塔内を減圧して該吸着塔内の死空間に充
満している不純ガス成分を排気し、さらに軽度に真空引
きして吸着剤に吸着されている不純物含有ＣＯ＿２を脱
着させて更に高真空に真空引きして高純度のＣＯ＿２を
回収すると共に前記吸着塔内に一部残留している湿分お
よびＳ分を他の吸着塔の吸着サイクルにおける吸着塔通
過ガスによって脱着し、吸着剤を再生するとともにＣＯ
＿２回収率を向上させることを特徴とするＣＯ＿２含有
ガスからＣＯ＿２を高純度で分離回収する方法。C in a pressure swing adsorption device with two or more adsorption towers arranged in parallel.
CO_2 in the CO_2-containing gas by introducing O_2-containing gas
2, a CO_2-containing gas containing moisture and S content is introduced into a CO_2 adsorption tower under pressure, and then the pressure inside the adsorption tower is reduced to fill the dead space within the adsorption tower. The impurity gas components contained in the adsorbent are evacuated, and the impurity-containing CO_2 adsorbed by the adsorbent is further evacuated by a slight vacuum, and the impurity-containing CO_2 adsorbed by the adsorbent is desorbed, and the highly purified CO_2 is recovered by further evacuation to a high vacuum. The moisture and S content partially remaining in the adsorption tower are desorbed by the gas passing through the adsorption tower in the adsorption cycle of other adsorption towers, regenerating the adsorbent and CO
A method for separating and recovering CO_2 with high purity from a CO_2-containing gas, which is characterized by improving the recovery rate of CO_2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61245103A JPS6397214A (en) | 1986-10-15 | 1986-10-15 | Method for separating and recovering high-purity co2 from co2-containing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61245103A JPS6397214A (en) | 1986-10-15 | 1986-10-15 | Method for separating and recovering high-purity co2 from co2-containing gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6397214A true JPS6397214A (en) | 1988-04-27 |
Family
ID=17128658
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61245103A Pending JPS6397214A (en) | 1986-10-15 | 1986-10-15 | Method for separating and recovering high-purity co2 from co2-containing gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6397214A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2020163247A (en) * | 2019-03-28 | 2020-10-08 | 株式会社豊田中央研究所 | Carbon dioxide recovery device, hydrocarbon manufacturing device, and carbon dioxide recovery method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6197124A (en) * | 1984-10-18 | 1986-05-15 | インペリアル・ケミカル・インダストリーズ・ピーエルシー | Collection of carbon dioxide |
-
1986
- 1986-10-15 JP JP61245103A patent/JPS6397214A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6197124A (en) * | 1984-10-18 | 1986-05-15 | インペリアル・ケミカル・インダストリーズ・ピーエルシー | Collection of carbon dioxide |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2020163247A (en) * | 2019-03-28 | 2020-10-08 | 株式会社豊田中央研究所 | Carbon dioxide recovery device, hydrocarbon manufacturing device, and carbon dioxide recovery method |
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