Experiments in gas absorption of pure sulfur dioxide and carbon dioxide by water were carried out in a 7.0cm packed tower to obtain liquid film coefficients directly, and the absorption mechanism for both the gases were compared.
Packings used were 25mm and 15mm Raschig rings and the packed heights were 30.0cm.
Liquid film coefficients of sulfur dioxide were lower than that predicted from the carbon dioxide data by the Sherwood-Holloway correlation⁶⁾ as shown in Fig. 1 and Fig. 2.
By means of the hydrolysis hypothesis suggested by Whitney and Vivian⁹⁾, pseudo liquid film coefficients of sulfur dioxide were calculated. These coefficients were in excellent agreement with the predicted values from carbon dioxide data as shown in Fig. 3 and Fig. 4.

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石炭ガスなどにふくまれる硫化水素を除去するために用いられる湿式脱硫法の研究の第一段として,水酸化第二鉄のアルカリ懸濁液を使用するいわゆるフェロックス法につき研究した。まず工場における実際使用液の分析をおこない,チオ硫酸ソーダおよびフェロシアン化合物の生成をたしかめた。
次にアルカリに対するH²Sの吸収につき実験しさらに,これに水酸化第二鉄の共存する場合につき吸収能を測定した。これよりフェロックス脱硫反応の機構を検討し次の結論を得た。
(1)液中のアルカリ度が大になるも脱硫速度はさほど増加しない。また再生速度はいちじるしくおそくなる。
(2)副生するフェロシアン化合物による脱硫反応を考慮にいれるべきである。
(7)式によって示される脱硫反応は,結局次の5段階に分けて考えられる。
(i) H₂Sの溶解 (ii) SH^-の液中の拡散 (iii) Fe(OH)₃よりFe…の溶解と拡散
(iv) Fe₂S₃の生成 (v) 生成せるFe₂S₃の反応系外の分離
このうち(i)と(v)とが律速的のようである。

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多孔板精溜塔の性能な追求する一手段として,純炭酸ガスの水による吸収の実験を行い,いわゆる液境膜抵抗のみが存在する場合の段効率が板の構造,塔内ガス速度,溢流液量,堰の高さなどによりいかに変化するかを考察するとともに一移動単位長さ,L_x³⁾を求める実験式を導いた。

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Absorption of pure carbon dioxide (97-99%) by the city water was carried out in the wetted-wall column, which was constructed of standard 1/2″ iron pipe. The liquid film height per transfer unit, H_L, based on the log. mean driving force was calculated from the data obtained over the range from 100 to 2, 000 of (Re)_L. (Re)_G was kept constant at about 700 for the majority of runs, since it was found by the preliminary runs that it had not any effect on the rate of absorption.
The length of tube was varied from 508 to 1856mm.
The discrepancy between the experiments and the theories by Hatta and Pigford was clearly recognized as already pointed out by Sherwood and Pigford in their book. While Emmert and Pigford tried to verify the theory by the interesting experiments using wetting agent, we attempted to explain the discrepancy by other theoretical relations derived here which were based on some added assumptions. These relations are not satisfactory, but they show somewhat better agreement than the previous theoretical lines.
We recommend the experimental equations presented here for practical purposes, until a more perfect theory with due regard to the effect of turbulence is established in future.

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Absorption of CO₂ was carried out with the mixed phase flow of CO₂-air mixture gas and KOH solution in vertical glass pipes of 12.8mm and 17.8mm i.d.
The K₂CO₃ concentrations in the flowing solution were measured at various points along the pipe. This reator was, for convenience' sake, considered separately in two sections as divided according to the concentration gradients: one was the accelerating section where the concentration gradient was curved by the mixing effect, and the other was the steady flow section where the gradient was nearly linear.
Mass transfer coefficients were calculated by the next equation:
The effects of various factors on K_Ga were investigated in each flow section as follows: -
1) for the accelerating section (0.17m)
2) for the steady flow section
3) for the whole section (1.26m)
4) K_Ga was inversely proportional to the pipe diameter.
5) K_Ga was increased with the KOH concentration within the Experimental range. (0.8-2.03 N KOH)

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The present paper deals with our study on the physical absorption by pure water made for the purpose of subsequently studying the capacity characteristics of CO₂ absorption byalkaline solutions in a packing tower.
10mm glass rings were packed in a glass column of 50mm i.d. by the height of 500mm, intowhich almost pure CO₂ gas was introduced to be absorbed by distilled water.
We obtained the following two series of the results, when the temperature was reduced to 15°C.
k_La=3.30L^0.79 (1)
i.e., (H.T.U.)_L=0.303L^0.21(1a)
and k_La=4.56L^0.79 (2)
i.e., (H.T.U.)_L=0.219L^0.21 (2a)
Eq. (1) represents the results derived with the stock rings which were water washed and newly packed, therefore considered as moderately clean; while eq. (2) represents those of the repeated experiments with the same rings without repacking, which, however, were alkaline washed by being kept overnight in the same column filled with 1N-KOH solution and then water washed.
The k_La values of eq. (2) were 1.38 times that of eq. (1), mainly due to the change of the effective area; at any rate k_La was proportional to L^0.79 in both the cases.
Great differences were observed among the data of many papers in the literature concerning the capacity coefficients and the active area of packing towers. Usually no particular references have been made to the cleanliness and the preliminary treatment of the packing. According to the experiments dealt with in this paper we found that we could not neglect the effect of the cleanliness of the packings.
Also, as observed in the literative, it was difficult to obtain satisfactory data for liquor whose rate was less than 5[m³/m²·hr].

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ガス中に含まれる成分を回収または除去する操作は,化学工業において重要な一分野を占め,これに関する研究は種々おこなわれている。われわれは先にベンチュリー・スクラッバーを試作し,これを高炉ガス中に浮游するダストの除去に使用してきわめて良好な結果を得た。3)4)ついでコークス炉ガス中のピリヂン塩基,およびナフタリンの回収並びに鉄鉱石の脱砒焼結装置の排ガス中に含まれる亜砒酸の除去に利用して一応の結果を得たのでこれらについて報告する。

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