JPH062984A - Adsorption type reactor module - Google Patents
Adsorption type reactor moduleInfo
- Publication number
- JPH062984A JPH062984A JP15930892A JP15930892A JPH062984A JP H062984 A JPH062984 A JP H062984A JP 15930892 A JP15930892 A JP 15930892A JP 15930892 A JP15930892 A JP 15930892A JP H062984 A JPH062984 A JP H062984A
- Authority
- JP
- Japan
- Prior art keywords
- adsorbent
- adsorption
- heat transfer
- fins
- module
- 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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Links
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- Sorption Type Refrigeration Machines (AREA)
Abstract
(57)【要約】
【目的】吸着式冷凍機の吸着式反応器を構成するモジュ
ールを小型化、高性能化する。
【構成】多数の伝熱管を共通の多数のフィンにより一体
に並設し、夫々のフィン間の間隙に固体吸着剤を充填す
ると共に、フィンの外側を通気性被覆材で被覆してパネ
ル型構造のモジュールを構成する。
【効果】 占有面積に対して有効な吸着剤の量が多
く、吸着式反応器の小型化、高性能化を図れる、 真
空容器内への所望の数の設置を容易に行うことができ、
吸着式冷凍機の所望の冷凍能力に応じた吸着式反応器を
構成することができる、 伝熱面積の適正化により伝
熱促進を図り、単位重量当りの冷媒駆動量を大きくする
ことができる、 吸着剤の粒度及びその充填層の厚さ
を適正化して冷媒の物質移動係数を大きくすることによ
りサイクル時間を短縮することができる。
(57) [Abstract] [Purpose] To reduce the size and performance of the modules that make up the adsorption reactor of an adsorption refrigerator. [Structure] A panel-type structure in which a large number of heat transfer tubes are integrally arranged side by side with a common large number of fins, the gap between the fins is filled with a solid adsorbent, and the fins are covered with a breathable covering material. Configure the module of. [Effect] The amount of adsorbent that is effective with respect to the occupied area is large, and the adsorption reactor can be downsized and the performance can be improved. It is possible to easily install a desired number in a vacuum container.
An adsorption reactor can be configured according to the desired refrigerating capacity of the adsorption refrigerator, heat transfer can be promoted by optimizing the heat transfer area, and the amount of refrigerant drive per unit weight can be increased. The cycle time can be shortened by optimizing the particle size of the adsorbent and the thickness of the packed layer thereof to increase the mass transfer coefficient of the refrigerant.
Description
【０００１】[0001]
【産業上の利用分野】本発明はゼオライト、活性炭、シ
リカゲル等の固体吸着剤の冷媒吸着、脱着作用を利用し
て冷水を発生させる吸着式冷凍機を構成する吸着式反応
器モジュールに関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an adsorption type reactor module which constitutes an adsorption type refrigerating machine for generating cold water by utilizing a refrigerant adsorption and desorption of a solid adsorbent such as zeolite, activated carbon and silica gel. .
【０００２】[0002]
【従来の技術】吸着式冷凍機に於ける従来の吸着式反応
器のモジュールは、銅製等の伝熱管の夫々の外周に多数
の円形または多角形のフィンを設けてフィンチューブを
構成し、夫々のフィン間の間隙に固体吸着剤を充填する
と共に、フィンの外側に脱落防止用の金網を張設して構
成している。このような構成に於いて、吸着式冷凍機の
吸着反応器として用いる場合には、所望の冷凍能力に応
じてフィンチューブの長さと本数を設定して、これらの
モジュールを真空容器内に並べて設置して構成してい
る。（例えば特開昭62-91763号公報参照のこと。）2. Description of the Related Art In a conventional adsorption reactor module in an adsorption refrigerator, a fin tube is constructed by providing a large number of circular or polygonal fins on the outer circumference of each heat transfer tube made of copper or the like. The gap between the fins is filled with a solid adsorbent, and a wire mesh for preventing falling is stretched outside the fins. In such a configuration, when used as an adsorption reactor of an adsorption refrigerator, the length and number of fin tubes are set according to the desired refrigerating capacity, and these modules are installed side by side in a vacuum container. Then configured. (See, for example, JP-A-62-91763.)
【０００３】[0003]
【発明が解決しようとする課題】このように複数の伝熱
管の夫々の外周に設けたフィン間に固体吸着剤を充填し
て構成するモジュールでは、吸着剤と伝熱管との熱伝達
は良好に行われるものの真空容器内に並べて設置した場
合に於いて、それらの並べたモジュールの輪郭内の面積
に対する吸着剤の占有面積が小さく、従って有効な吸着
剤の量が少ない。In the module constructed by filling the solid adsorbent between the fins provided on the outer periphery of each of the plurality of heat transfer tubes as described above, the heat transfer between the adsorbent and the heat transfer tube is excellent. When they are installed side by side in a vacuum container, the occupied area of the adsorbent with respect to the area within the contour of the arranged modules is small, and therefore the amount of effective adsorbent is small.
【０００４】このため必要な冷凍能力を得るためには真
空容器内に設置する数を増やさなければならず、必然的
にモジュールの占有面積、そしてこれを設置する真空容
器が大型化するという課題があった。Therefore, in order to obtain the required refrigerating capacity, it is necessary to increase the number of modules to be installed in the vacuum container, which inevitably causes a problem that the occupied area of the module and the vacuum container in which the module is installed become large. there were.
【０００５】また従来の吸着式反応器のモジュールで
は、吸着剤の重量に対しての伝熱面積、吸着層の厚さ、
吸着剤の粒度等の条件を余り勘案していないため、これ
らの条件が必ずしも最適ではない。このため伝熱管に供
給される熱媒体の温度と吸着剤の温度差が10℃程度と比
較的大きくなり、従って必要な冷凍能力を得るのに必要
な吸着剤の量も多くなり、この点からもモジュールの占
有面積、そして真空容器の寸法が大きくなってしまうと
いう課題があった。本発明は、このような課題を解決す
ることを目的とするものである。In the conventional adsorption reactor module, the heat transfer area relative to the weight of the adsorbent, the thickness of the adsorption layer,
These conditions are not always optimal because conditions such as the particle size of the adsorbent are not taken into consideration. Therefore, the temperature difference between the heat medium supplied to the heat transfer tube and the temperature of the adsorbent becomes relatively large, about 10 ° C, and therefore the amount of adsorbent required to obtain the required refrigerating capacity also increases. However, there is a problem that the occupied area of the module and the size of the vacuum container become large. The present invention aims to solve such problems.
【０００６】[0006]
【課題を解決するための手段】上述した課題を解決する
ために、本発明では、多数の伝熱管を共通の多数のフィ
ンにより一体に並設し、夫々のフィン間の間隙に固体吸
着剤を充填すると共に、フィンの外側を通気性被覆材で
被覆して構成した吸着式反応器モジュールを提案する。In order to solve the above-mentioned problems, in the present invention, a large number of heat transfer tubes are integrally arranged in parallel by a large number of common fins, and a solid adsorbent is provided in the gaps between the respective fins. We propose an adsorption-type reactor module that is constructed by filling the fins and coating the outside of the fins with a breathable coating material.
【０００７】次に本発明では、上記の構成に於いて、多
数の伝熱管を千鳥状に配設することを提案する。Next, the present invention proposes arranging a large number of heat transfer tubes in a zigzag manner in the above structure.
【０００８】上記した構成に於いて、通気性被覆材は、
多孔板や網により構成することができる。In the above structure, the breathable covering material is
It can be composed of a perforated plate or a net.
【０００９】また本発明では上記した構成に於いて、フ
ィン間とチューブに挾まれる伝熱面積の、吸着剤の単位
重量当りの値が0.6〜1.0ｍ2/kgの範囲となるようにする
ことを提案する。Further, in the present invention, in the above-mentioned constitution, the value of the heat transfer area sandwiched between the fins and the tube per unit weight of the adsorbent is in the range of 0.6 to 1.0 m 2 / kg. I suggest that.
【００１０】更に本発明では上記した構成に於いて、吸
着剤の粒度は40〜12メッシュ（0.35〜1.5mm）の範囲と
すること、またモジュールの中心から、充填されている
吸着剤の表面までの距離を最大12mmに制限することを提
案する。Further, in the present invention, in the above constitution, the particle size of the adsorbent is in the range of 40 to 12 mesh (0.35 to 1.5 mm), and from the center of the module to the surface of the filled adsorbent. We propose to limit the distance to a maximum of 12 mm.
【００１１】[0011]
【作用】本発明のモジュールは、その適数を真空容器内
に並べて設置することにより、吸着式冷凍機の所望の冷
凍能力に応じた吸着式反応器を構成することができる。
かかる本発明のモジュールに於いては、固体吸着剤は、
多数の伝熱管を一体に並設する多数のフィン間、即ちモ
ジュールの輪郭内の全てに渡って充填するので、上述し
た従来の構成と比較してモジュールの占有面積に対して
有効な吸着剤の量が多い。In the module of the present invention, an appropriate number of the modules can be arranged side by side in a vacuum container to form an adsorption reactor according to the desired refrigerating capacity of the adsorption refrigerator.
In the module of the present invention, the solid adsorbent is
Since a large number of heat transfer tubes are filled in parallel between a large number of fins that are arranged side by side, that is, within the outline of the module, the adsorbent that is effective for the occupied area of the module is smaller than that of the conventional configuration described above. There is a large amount.
【００１２】伝熱管は千鳥状に配設することにより、各
吸着剤との距離を平均化することができ、全ての吸着剤
への伝熱を均一化して、その温度の一様化に寄与する。By arranging the heat transfer tubes in a zigzag manner, the distance from each adsorbent can be equalized, and the heat transfer to all adsorbents can be made uniform, contributing to the uniformization of the temperature. To do.
【００１３】一方、吸着剤は、フィン間とチューブに挾
まれる伝熱面積の、吸着剤の単位重量当りの値を0.6〜
1.0ｍ2/kgの範囲となるように充填すれば、伝熱が良好
となって、伝熱管を流れる熱媒体と吸着剤の温度との差
を小さくすることができ、従って単位重量当りの冷媒駆
動量を大きくすることができる。On the other hand, the adsorbent has a value of the heat transfer area between the fins and the tube per unit weight of the adsorbent of 0.6 to
If it is filled so as to be in the range of 1.0 m 2 / kg, the heat transfer becomes good, and the difference between the temperature of the heat medium flowing through the heat transfer tube and the temperature of the adsorbent can be made small, and therefore the refrigerant per unit weight. The driving amount can be increased.
【００１４】また、モジュールの中心から、充填されて
いる吸着剤の表面までの距離を最大12mmに制限し、また
吸着剤の粒度を40〜12メッシュ（0.35〜1.5mm）の範囲
とすることにより、冷媒の物質移動係数を大きくするこ
とができ、従って吸着剤による冷媒の吸着、脱着のサイ
クル時間の短縮化が図られ、単位時間当りの冷凍能力を
大きくすることができる。Further, by limiting the distance from the center of the module to the surface of the adsorbent filled therein to a maximum of 12 mm, and by setting the particle size of the adsorbent within the range of 40 to 12 mesh (0.35 to 1.5 mm). The mass transfer coefficient of the refrigerant can be increased, and therefore, the cycle time for adsorbing and desorbing the refrigerant by the adsorbent can be shortened, and the refrigerating capacity per unit time can be increased.
【００１５】[0015]
【実施例】次に本発明の実施例を図について説明する。
図１は本発明の吸着式反応器モジュールの実施例の要部
を説明するもので、符号１は伝熱管である。この伝熱管
１の多数を、共通の多数のフィン２により一体に並設し
ている。伝熱管１、フィン２は従来と同様に、夫々銅
管、アルミ板等で構成する。この実施例では、多数の伝
熱管１は一線状に一定のピッチＴｐで並設されており、
また多数のフィン２は一定のピッチＦｐで並設されてい
る。そして、夫々のフィン２間の間隙にゼオライト、活
性炭、シリカゲル等の固体吸着剤３を充填すると共に、
フィン２の外側を通気性被覆材４で被覆して吸着式反応
器のモジュールを構成している。後述する実施例に於い
ては、固体吸着剤３は、φ0.5mmの破砕状シリカゲルと
している。上記通気性被覆材４は、パンチングメタル等
の多孔板や金網等で構成することができる。尚、図中符
号Ｌはモジュールの中心から固体吸着剤３の表面までの
距離を表すものである。Embodiments of the present invention will now be described with reference to the drawings.
FIG. 1 illustrates an essential part of an embodiment of an adsorption type reactor module of the present invention, and reference numeral 1 is a heat transfer tube. A large number of common heat transfer tubes 1 are arranged in parallel by a large number of common fins 2. The heat transfer tube 1 and the fins 2 are each made of a copper tube, an aluminum plate or the like, as in the conventional case. In this embodiment, a large number of heat transfer tubes 1 are arranged in a line at a constant pitch Tp,
Further, a large number of fins 2 are arranged in parallel at a constant pitch Fp. Then, the space between the fins 2 is filled with a solid adsorbent 3 such as zeolite, activated carbon or silica gel,
The outer surface of the fin 2 is covered with a breathable coating material 4 to form a module of an adsorption reactor. In the examples described later, the solid adsorbent 3 is crushed silica gel having a diameter of 0.5 mm. The breathable covering material 4 can be composed of a perforated plate such as punching metal or a wire mesh. The symbol L in the figure represents the distance from the center of the module to the surface of the solid adsorbent 3.
【００１６】図２は他の構成のモジュールの実施例を示
すもので、この構成では、多数の伝熱管１は千鳥状に配
設されている。尚、このモジュールは本発明の効果を確
認するための実験に用いられた構成を示すもので、実験
条件は次の通りである。 実験条件： 温水入口 80℃ 伝熱面積／吸着剤量＝0.
87m2/kg 冷却水入口 26℃ フィンピッチ ＝5mm 凝縮器 26℃ 伝熱面積 ＝0.41m2 蒸発温度 12℃ 吸着剤の充填層（片側、
Ｌ）＝12mmFIG. 2 shows an embodiment of a module having another structure. In this structure, a large number of heat transfer tubes 1 are arranged in a staggered pattern. This module shows the configuration used in the experiment for confirming the effect of the present invention, and the experimental conditions are as follows. Experimental condition: Hot water inlet 80 ℃ Heat transfer area / Adsorbent amount = 0.
87m 2 / kg Cooling water inlet 26 ℃ Fin pitch ＝ 5mm Condenser 26 ℃ Heat transfer area ＝ 0.41m 2 Evaporation temperature 12 ℃ Adsorbent packed bed (one side,
L) = 12 mm
【００１７】以上の構成のモジュールは、適数を真空容
器内に並べて設置し（図示省略）、そして多数の伝熱管
１を直列及び／または並列に接続して熱媒体を流すよう
にして所望の冷凍能力の吸着式反応器を構成することが
できる。A suitable number of modules having the above-mentioned configuration are arranged in a vacuum container (not shown), and a large number of heat transfer tubes 1 are connected in series and / or in parallel to allow a heat medium to flow therethrough. An adsorption type reactor having a refrigerating capacity can be constructed.
【００１８】以上の構成に於いて、吸着式冷凍機の運転
に於ける再生工程では、モジュールの伝熱管１内に加熱
源としての熱媒体である温水等を流すことにより吸着剤
３の再生を行う。即ち、伝熱管１内に温水を流すことに
より、伝熱管１及びフィン２を介して吸着剤３が加熱さ
れて冷媒が脱着され、こうして吸着剤３から脱着された
冷媒蒸気が通気性被覆材４を通してモジュール外に排出
され、そして吸着式冷凍機を構成する凝縮器に於いて凝
縮される。In the above-described structure, in the regeneration process in the operation of the adsorption refrigerator, the adsorbent 3 is regenerated by flowing hot water, which is a heat medium as a heating source, into the heat transfer tube 1 of the module. To do. That is, by flowing hot water into the heat transfer tube 1, the adsorbent 3 is heated via the heat transfer tube 1 and the fins 2 to desorb the refrigerant, and thus the refrigerant vapor desorbed from the adsorbent 3 is passed through the breathable coating material 4 Is discharged to the outside of the module through and is condensed in the condenser that constitutes the adsorption refrigerator.
【００１９】一方、吸着工程では、伝熱管１内に冷却源
としての熱媒体である冷却水等を流すことにより吸着剤
３による冷媒の吸着を行う。即ち、伝熱管１及びフィン
２を介して吸着剤３を冷却することにより、吸着式冷凍
機を構成する蒸発器から真空容器内に供給される冷媒蒸
気は通気性被覆材４を通してモジュール内に流入して連
続的に吸着剤３に吸着される。On the other hand, in the adsorption step, the refrigerant is adsorbed by the adsorbent 3 by flowing cooling water, which is a heat medium as a cooling source, into the heat transfer tube 1. That is, by cooling the adsorbent 3 through the heat transfer tube 1 and the fins 2, the refrigerant vapor supplied from the evaporator constituting the adsorption refrigerator to the vacuum container flows into the module through the breathable coating material 4. And is continuously adsorbed on the adsorbent 3.
【００２０】尚、以上の吸着式反応器の動作を伴う吸着
式冷凍機の動作は、従来と同様であるので説明は省略す
る。The operation of the adsorption type refrigerator accompanied by the operation of the adsorption type reactor described above is the same as the conventional one, and therefore its explanation is omitted.
【００２１】次に、本発明の吸着式反応器モジュール
を、図３に示す一次元モデルにより伝熱解析シミュレー
ションを行った結果を示す。かかる伝熱解析は次のよう
な手法により、吸着剤３の充填層内の温度分布（後述す
るようにモジュールの中心位置から充填層の表面位置ま
での15点）を解析することにより行った。Next, the results of heat transfer analysis simulation of the adsorption reactor module of the present invention by the one-dimensional model shown in FIG. 3 are shown. The heat transfer analysis was performed by analyzing the temperature distribution in the packed bed of the adsorbent 3 (15 points from the center position of the module to the surface position of the packed bed as described later) by the following method.
【００２２】まず解析に当り、吸着剤の充填層内では、
以下のような条件の基で熱交換が行われているものと仮
定している。 吸着剤の粒子は十分に小さい。 吸着剤の粒子全体が常に飽和状態を維持しながら反
応が進む。 冷媒蒸気の拡散抵抗は無視できる程小さい。 吸着剤の充填層内の冷媒蒸気圧力は常に一定であ
る。 また、吸着剤による冷媒の吸着、脱着反応は、マクロに
みて内部発熱、吸熱を伴う熱伝導と規定し、吸着時に
は、吸着熱が吸着剤の温度上昇と熱伝導による放熱に分
配され、脱着時には、熱伝導で伝達された熱と吸着剤の
温度低下分の熱が脱着熱に当てられるものとした。First, in the analysis, in the packed bed of the adsorbent,
It is assumed that heat exchange is performed under the following conditions. The particles of adsorbent are small enough. The reaction proceeds while the entire particles of the adsorbent are always kept saturated. The diffusion resistance of the refrigerant vapor is so small that it can be ignored. The refrigerant vapor pressure in the packed bed of adsorbent is always constant. Also, the adsorption and desorption reaction of the refrigerant by the adsorbent is defined as heat conduction accompanied by internal heat generation and endotherm in macroscopic sense.At the time of adsorption, the heat of adsorption is distributed to the temperature rise of the adsorbent and heat dissipation due to heat conduction, and at the time of desorption It is assumed that the heat transferred by heat conduction and the heat corresponding to the temperature drop of the adsorbent are applied to the desorption heat.
【００２３】このような条件の基では、以下の一連の式
が得られる。Under these conditions, the following series of equations are obtained.
【数１】 次に水の飽和蒸気圧の式（アントワーヌの方程式）は次
式の通りである。[Equation 1] Next, the equation of saturated vapor pressure of water (Antoine's equation) is as follows.
【数２】 [Equation 2]
【００２５】一方、静的平衡吸着量測定試験により得ら
れる吸着剤の平衡吸着量のデータをＤ−Ａ式に代入し整
理すると、含水率ｍとＰ−Ｔの関係を表す次式が得られ
る。On the other hand, by substituting the equilibrium adsorption amount data of the adsorbent obtained by the static equilibrium adsorption amount measurement test into the DA equation and rearranging it, the following equation expressing the relationship between the water content m and PT is obtained. .
【数３】 [Equation 3]
【００２６】更に、クラウシス・クラペーロンの式に上
記（２），（３）式を代入すると、吸着熱Ｈに関する次
式が得られる。Further, by substituting the above equations (2) and (3) into the Clausius-Klaperon equation, the following equation relating to the heat of adsorption H is obtained.
【数４】 [Equation 4]
【００２７】以上の式に於いて、フィン２のピッチＦｐ
を5mm、フィン２の厚さを0.15mm、吸着剤の充填層の厚
さ、即ちモジュールの中心から、充填されている吸着剤
の表面までの距離Ｌを12mm、吸着、脱着のサイクル時間
を7分とすると共に、各部の温度条件を以下のように設
定して後退差分法によりシミュレーションを行った。 再生温度Ｔｇ＝75℃ 吸着温度Ｔａ＝30℃ 凝縮温度Ｔｃ＝30℃ 蒸発温度Ｔｅ＝10℃ 但し、以上の式に於いて、各記号は以下に示す通りであ
る。 Ｃａ：吸着剤（シリカゲル）の比熱 0.22 （kcal/kg・Ｋ） ｍ ：含水率 （kg/kg） Ｃｗ：凝縮水の比熱 0.99 （kcal/kg・Ｋ） ρ ：吸着剤の比重量 2200 （kg/m3） Ｔ ：絶対温度 （Ｋ） Ｈ ：吸着熱 （kcal/kg・H2O） λ ：吸着剤の有効熱伝導率 0.25 （kcal/m・hr・℃） Ｐｓ：水蒸気の飽和蒸気圧 （mmHg） Ｔｖ：水蒸気温度 （Ｋ） Ｔａ：吸着剤温度 （Ｋ） Ｌｏ：水蒸気潜熱 （kcal/kg） Ｔｃ：冷却水、温水温度 303,353 （Ｋ） ｈ ：熱通過率 186 （kcal/m2・hr・℃） Ｅ ：吸着特性エネルギー 742.2 （cal/mol） Ｒ ：気体定数 1.192 （cal/mol・Ｋ） ｔ ：時間In the above equation, the pitch Fp of the fins 2
Is 5 mm, the thickness of the fin 2 is 0.15 mm, the thickness of the adsorbent packed layer, that is, the distance L from the center of the module to the surface of the adsorbent filled is 12 mm, and the cycle time of adsorption and desorption is 7 mm. In addition, the temperature condition of each part was set as follows and a simulation was performed by the backward difference method. Regeneration temperature Tg = 75 ° C. Adsorption temperature Ta = 30 ° C. Condensing temperature Tc = 30 ° C. Evaporation temperature Te = 10 ° C. However, in the above equation, each symbol is as shown below. Ca: Specific heat of adsorbent (silica gel) 0.22 (kcal / kgK) m: Water content (kg / kg) Cw: Specific heat of condensed water 0.99 (kcal / kgK) ρ: Specific weight of adsorbent 2200 (kg) / m 3 ) T: Absolute temperature (K) H: Heat of adsorption (kcal / kg · H 2 O) λ: Effective thermal conductivity of adsorbent 0.25 (kcal / m · hr · ° C) Ps: Saturated vapor pressure of water vapor (MmHg) Tv: Water vapor temperature (K) Ta: Adsorbent temperature (K) Lo: Latent steam heat (kcal / kg) Tc: Cooling water, hot water temperature 303,353 (K) h: Heat transfer rate 186 (kcal / m 2 · hr ・ ℃) E: Adsorption characteristic energy 742.2 (cal / mol) R: Gas constant 1.192 (cal / mol ・ K) t: Time
【００２８】図４、図５は以上のシミュレーションによ
り得られた吸着工程時の吸着剤３の充填層内の温度分布
と含水率の変化を示すものであり、横軸のメッシュは、
吸着剤３の充填層の表面（メッシュ＝1）からモジュー
ルの中心位置（表面からＬ＝12mmの位置、メッシュ＝1
5）までを14等分して成る15点の夫々の位置を示すもの
である。FIGS. 4 and 5 show changes in temperature distribution and water content in the packed bed of the adsorbent 3 during the adsorption step obtained by the above simulation.
From the surface of the packed bed of adsorbent 3 (mesh = 1) to the center position of the module (position L = 12 mm from the surface, mesh = 1)
It shows the position of each of 15 points, which is obtained by dividing 5) into 14 equal parts.
【００２９】この解析結果から、本発明のモジュールで
は、冷媒駆動量が100cc/kg-吸着剤の負荷、吸着剤温度
と熱媒体入口温度との温度差ΔＴ＝5℃がサイクルタイ
ム7分で達成し得る可能性が得られた。From the analysis results, in the module of the present invention, the refrigerant driving amount was 100 cc / kg-the load of the adsorbent, and the temperature difference ΔT = 5 ° C. between the adsorbent temperature and the heat medium inlet temperature was achieved in a cycle time of 7 minutes. The possibility was obtained.
【００３０】次に図６は、図２のモジュールに於いて、
伝熱管１とフィン２間に挾まれる伝熱面積の、吸着剤３
の単位重量当りの値に対する伝熱性を確認するために上
述した実験条件の基に各部の温度を測定した結果を示す
もので、この実験条件では、吸着、脱着時の吸着剤の温
度はΔＴ＝5℃以内にあることがわかる。この実験条件
に於ける伝熱面積／吸着剤量は、上述したように0.87m2
/kgであり、従って本発明のモジュールに於いては、上
記伝熱面積の、吸着剤３の単位重量当りの値を、例えば
上記した値を含む範囲である、0.6〜1.0ｍ2/kgの範囲と
なるようにすることにより、伝熱性を良好にすることが
できることがわかる。Next, FIG. 6 shows the module of FIG.
Adsorbent 3 having a heat transfer area sandwiched between heat transfer tube 1 and fins 2
In order to confirm the heat conductivity with respect to the value per unit weight of, the results of measuring the temperature of each part based on the experimental conditions described above are shown. Under this experimental condition, the temperature of the adsorbent during adsorption and desorption is ΔT = It can be seen that the temperature is within 5 ° C. The heat transfer area / adsorbent amount under these experimental conditions was 0.87 m 2 as described above.
Therefore, in the module of the present invention, the value of the heat transfer area per unit weight of the adsorbent 3 is, for example, 0.6 to 1.0 m 2 / kg which is a range including the above value. It can be seen that the heat conductivity can be improved by setting the content within the range.
【００３１】また図７は、静的駆動量に対する動的駆動
量の割合を確認するために、上述した理論計算と共に一
部の条件に於いて実測を行った結果を示すものである。
図に示されるように、粒径が0.5φに於いて、7分のサイ
クルタイムでは動的駆動量が90％以上となる。0.4mm〜
0.9mm（40メッシュ〜20メッシュ）の範囲に分布する破
砕状シリカゲルを用いて、下記の温度条件での実験を行
った結果、静的駆動量に対する動的駆動量の割合は、8
7.5％となった。 再生温度Ｔｇ＝70℃ 凝縮温度Ｔｃ＝30℃ 吸着温度Ｔａ＝34℃ 蒸発温度Ｔｅ＝10℃ これらのことから吸着剤３の粒度を40〜12メッシュ（0.
35〜1.5mm）の範囲とすることにより、冷媒の物質移動
係数を大きくすることができることがわかる。Further, FIG. 7 shows the result of actual measurement under some conditions together with the above-described theoretical calculation in order to confirm the ratio of the dynamic drive amount to the static drive amount.
As shown in the figure, when the particle size is 0.5φ, the dynamic driving amount becomes 90% or more in the cycle time of 7 minutes. 0.4 mm ~
As a result of an experiment under the following temperature conditions using crushed silica gel distributed in the range of 0.9 mm (40 mesh to 20 mesh), the ratio of the dynamic drive amount to the static drive amount was 8
It was 7.5%. Regeneration temperature Tg = 70 ° C. Condensing temperature Tc = 30 ° C. Adsorption temperature Ta = 34 ° C. Evaporation temperature Te = 10 ° C. Therefore, the particle size of the adsorbent 3 is 40 to 12 mesh (0.
It can be seen that the mass transfer coefficient of the refrigerant can be increased by setting the range to 35 to 1.5 mm).
【００３２】一方、吸着剤３の充填層の厚さを増すと、
蒸気の脱着により充填層表面での吸着剤３の有効熱伝達
率λが減少することと、脱着熱として使用されるために
温度が中心部より低くなり、充填層内の吸着剤の平均温
度の低下をもたらす。このことは充填層表面の吸着剤の
残存含水率の上昇、従って冷媒駆動量の低下を招いた
り、充填層の吸着剤の空隙間を通る冷媒流路抵抗も増す
ため、余り大きくすることはできず、上述した実験条件
に於ける距離Ｌ、即ちモジュールの中心から、充填され
ている吸着剤３の表面までの距離を最大12mmに制限する
ことが好ましい。On the other hand, if the thickness of the packed bed of the adsorbent 3 is increased,
The effective heat transfer coefficient λ of the adsorbent 3 on the surface of the packed bed decreases due to the desorption of vapor, and the temperature becomes lower than the central part because it is used as the heat of desorption, and the average temperature of the adsorbent in the packed bed Bring about a decline. This leads to an increase in the residual water content of the adsorbent on the surface of the packed bed, and thus a reduction in the amount of refrigerant drive, and also an increase in the resistance of the refrigerant flow path through the voids of the adsorbent in the packed bed, so it cannot be made too large. First, it is preferable to limit the distance L under the above-mentioned experimental conditions, that is, the distance from the center of the module to the surface of the adsorbent 3 filled to a maximum of 12 mm.
【００３３】[0033]
【発明の効果】本発明は以上の通りであるので、以下の
ような効果がある。 モジュールの占有面積に対して有効な吸着剤の量が
多く、吸着式反応器の小型化、高性能化を図れる。 モジュールがパネル型構造であるから、真空容器内
への所望の数の設置を容易に行うことができ、吸着式冷
凍機の所望の冷凍能力に応じた吸着式反応器を構成する
ことができる。 伝熱面積の適正化により伝熱促進を図り、単位重量
当りの冷媒駆動量を大きくすることができる。 吸着剤の粒度及びその充填層の厚さを適正化して冷
媒の物質移動係数を大きくすることによりサイクル時間
を短縮することができる。As described above, the present invention has the following effects. Since the amount of the adsorbent effective for the area occupied by the module is large, the adsorption reactor can be downsized and its performance can be improved. Since the module has a panel-type structure, a desired number of modules can be easily installed in a vacuum container, and an adsorption reactor according to a desired refrigerating capacity of the adsorption refrigerator can be configured. By optimizing the heat transfer area, heat transfer can be promoted, and the amount of driven refrigerant per unit weight can be increased. The cycle time can be shortened by optimizing the particle size of the adsorbent and the thickness of the packed layer thereof to increase the mass transfer coefficient of the refrigerant.
【図１】本発明の吸着式反応器モジュールの実施例の構
成の要部を表した説明的斜視図である。FIG. 1 is an explanatory perspective view showing a main part of a configuration of an embodiment of an adsorption reactor module of the present invention.
【図２】本発明の吸着式反応器モジュールの他の実施例
の構成の要部を表した説明的斜視図である。FIG. 2 is an explanatory perspective view showing the main part of the configuration of another embodiment of the adsorption reactor module of the present invention.
【図３】本発明の吸着式反応器モジュールの伝熱解析に
於ける一次元モデルである。FIG. 3 is a one-dimensional model in heat transfer analysis of the adsorption reactor module of the present invention.
【図４】本発明の吸着式反応器モジュールの伝熱解析の
結果を吸着剤の充填層内の温度分布として表した説明図
である。FIG. 4 is an explanatory diagram showing a result of heat transfer analysis of the adsorption reactor module of the present invention as a temperature distribution in a packed bed of an adsorbent.
【図５】本発明の吸着式反応器モジュールの伝熱解析の
結果を吸着剤の充填層内の含水率の変化として表した説
明図である。FIG. 5 is an explanatory diagram showing the results of heat transfer analysis of the adsorption reactor module of the present invention as changes in water content in a packed bed of adsorbent.
【図６】図２のモジュールに於ける各部の温度測定結果
を示すものである。FIG. 6 shows the temperature measurement result of each part in the module of FIG.
【図７】静的駆動量に対する動的駆動量の割合を確認す
るため理論解析及び実験結果を示すものである。FIG. 7 shows theoretical analysis and experimental results for confirming the ratio of the dynamic drive amount to the static drive amount.
１ 伝熱管 ２ フィン ３ 吸着剤 ４ 通気性被覆材 1 Heat transfer tube 2 Fin 3 Adsorbent 4 Breathable coating material
フロントページの続き (72)発明者 小松 富士夫 茨城県北相馬郡守谷町御所ケ丘２−19−10 グレースハイツ 102号 (72)発明者 小倉 正雄 東京都立川市若葉町２−８−105 (72)発明者 寺沢 秀彰 埼玉県大宮市盆栽町478Front page continued (72) Inventor Fujio Fujio 2-19-10 Grace Heights, Morishoka, Moriya-cho, Kitasoma-gun, Ibaraki Prefecture No. 102 Grace Heights 102 (72) Masao Ogura 2-8-105 Wakaba-cho, Tachikawa, Tokyo (72) Invention Hideaki Terasawa 478 Bonsai Town, Omiya City, Saitama Prefecture
Claims (7)
り一体に並設し、夫々のフィン間の間隙に固体吸着剤を
充填すると共に、フィンの外側を通気性被覆材で被覆し
て構成したことを特徴とする吸着式反応器モジュール1. A structure in which a large number of heat transfer tubes are integrally arranged in parallel by a large number of common fins, a gap between the fins is filled with a solid adsorbent, and the fins are covered with a breathable coating material. Adsorption type reactor module characterized by
伝熱管は千鳥状に配設されていることを特徴とする吸着
式反応器モジュール2. The adsorption reactor module according to claim 1, wherein the plurality of heat transfer tubes are arranged in a staggered pattern.
被覆材は多孔板により構成したことを特徴とする吸着式
反応器モジュール3. The adsorption reactor module according to claim 1, wherein the gas permeable covering material is a porous plate.
被覆材は網により構成したことを特徴とする吸着式反応
器モジュール4. The adsorption reactor module according to claim 1, wherein the gas permeable covering material is a net.
間とチューブに挾まれる伝熱面積の、吸着剤の単位重量
当りの値は0.6〜1.0ｍ2/kgの範囲となるように吸着剤を
充填することを特徴とする吸着式反応器モジュール5. The module according to claim 1, wherein the heat transfer area sandwiched between the fins and the tubes is adsorbed so that the value per unit weight of the adsorbent is in the range of 0.6 to 1.0 m 2 / kg. Adsorption reactor module characterized by being filled with agent
の粒度は40〜12メッシュ（0.35〜1.5mm）の範囲とする
ことを特徴とする吸着式反応器モジュール6. The adsorption reactor module according to claim 1, wherein the adsorbent has a particle size in the range of 40 to 12 mesh (0.35 to 1.5 mm).
ールの中心から、充填されている吸着剤の表面までの距
離は最大12mmに制限することを特徴とする吸着式反応器
モジュール7. The adsorption reactor module according to claim 1, wherein the distance from the center of the module to the surface of the adsorbent filled is limited to 12 mm at maximum.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15930892A JP3322316B2 (en) | 1992-06-18 | 1992-06-18 | Adsorption type reactor module |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15930892A JP3322316B2 (en) | 1992-06-18 | 1992-06-18 | Adsorption type reactor module |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH062984A true JPH062984A (en) | 1994-01-11 |
| JP3322316B2 JP3322316B2 (en) | 2002-09-09 |
Family
ID=15690969
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15930892A Expired - Lifetime JP3322316B2 (en) | 1992-06-18 | 1992-06-18 | Adsorption type reactor module |
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| Country | Link |
|---|---|
| JP (1) | JP3322316B2 (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995014898A1 (en) * | 1993-11-29 | 1995-06-01 | Mayekawa Mfg. Co., Ltd. | Adsorption type cooling apparatus, method of controlling cold output of same, and fin type adsorbent heat exchanger for use in same |
| US6102107A (en) * | 1998-12-11 | 2000-08-15 | Uop Llc | Apparatus for use in sorption cooling processes |
| JP2006200850A (en) * | 2005-01-21 | 2006-08-03 | Japan Exlan Co Ltd | Sorptive heat exchange module and method for producing the same |
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Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0462226B1 (en) | 1989-03-08 | 1995-05-10 | Rocky Research | Method and apparatus for achieving high reaction rates in solid-gas reactor systems |
-
1992
- 1992-06-18 JP JP15930892A patent/JP3322316B2/en not_active Expired - Lifetime
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| US6041617A (en) * | 1993-11-29 | 2000-03-28 | Mayekawa Mfg. Co., Ltd. | Adsorption type cooling apparatus, method of controlling cold output of same, and fin type adsorbent heat exchanger for use in same |
| WO1995014898A1 (en) * | 1993-11-29 | 1995-06-01 | Mayekawa Mfg. Co., Ltd. | Adsorption type cooling apparatus, method of controlling cold output of same, and fin type adsorbent heat exchanger for use in same |
| US6102107A (en) * | 1998-12-11 | 2000-08-15 | Uop Llc | Apparatus for use in sorption cooling processes |
| JP2006200850A (en) * | 2005-01-21 | 2006-08-03 | Japan Exlan Co Ltd | Sorptive heat exchange module and method for producing the same |
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| US8221532B2 (en) | 2006-01-30 | 2012-07-17 | Carruthers J Donald | Nanoporous articles and methods of making same |
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| WO2009002893A3 (en) * | 2007-06-22 | 2009-02-19 | Advanced Tech Materials | Component for solar adsorption refrigeration system and method of making such component |
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