JPS6351045B2 - - Google Patents
Info
- Publication number
- JPS6351045B2 JPS6351045B2 JP56119535A JP11953581A JPS6351045B2 JP S6351045 B2 JPS6351045 B2 JP S6351045B2 JP 56119535 A JP56119535 A JP 56119535A JP 11953581 A JP11953581 A JP 11953581A JP S6351045 B2 JPS6351045 B2 JP S6351045B2
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fluid
- chamber
- fiber bundle
- separation membrane
- 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.)
- Expired
Links
- 239000012510 hollow fiber Substances 0.000 claims description 57
- 239000012530 fluid Substances 0.000 claims description 44
- 238000000926 separation method Methods 0.000 claims description 36
- 239000012528 membrane Substances 0.000 claims description 33
- 238000005192 partition Methods 0.000 claims description 29
- 239000007788 liquid Substances 0.000 description 48
- 239000011550 stock solution Substances 0.000 description 34
- 238000000034 method Methods 0.000 description 29
- 238000011001 backwashing Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 17
- 239000012466 permeate Substances 0.000 description 15
- 239000000243 solution Substances 0.000 description 9
- 239000012141 concentrate Substances 0.000 description 7
- 239000012459 cleaning agent Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive effect Effects 0.000 description 2
- -1 etc.) Substances 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 230000001914 calming effect Effects 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920003229 poly(methyl methacrylate) Polymers 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000004926 polymethyl methacrylate Substances 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 239000004627 regenerated cellulose Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000003566 sealing material Substances 0.000 description 1
- 229920002379 silicone rubber Polymers 0.000 description 1
- 239000004945 silicone rubber Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000005720 sucrose Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】
本発明は分離膜装置に関するものであり、とく
に外圧循環式の分離・濃縮装置として適するもの
である。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a separation membrane device, and is particularly suitable as an external pressure circulation type separation/concentration device.
従来の中空糸膜による外圧循環式の分離・濃縮
システムとしては、中空糸束エレメント１個を筒
状の筐体に装着したいわゆるモジユールを単数あ
るいは複数個外部配管にて接続して構成したもの
が一般的である。 Conventional external pressure circulation separation/concentration systems using hollow fiber membranes are constructed by connecting one or more so-called modules with one hollow fiber bundle element installed in a cylindrical casing via external piping. Common.
しかし、上記従来方式は実用上多種の難点を有
する。とくに装置規模が大きく、モジユール数が
大なる場合、装置の占有スペースが大きくなり、
関連する建屋・基礎・付帯配管設備工事が増大
し、経済的にきわめて不都合である。また、分散
したモジユールの検査・補修作業のわずらわしさ
も一般的に論じられているところである。さらに
このような中空糸膜による分離・濃縮装置は処理
目的・被処理物の特性に応じて、多様なシステム
構成を要求されるが、いわゆるモジユールシステ
ムでは、このような要求に対処する際多くの難点
にそうぐうする。 However, the above conventional method has various practical difficulties. Especially when the scale of the equipment is large and the number of modules is large, the space occupied by the equipment becomes large.
The related construction of buildings, foundations, and ancillary piping equipment will increase, which is extremely inconvenient economically. In addition, the troublesomeness of inspection and repair work for dispersed modules is also commonly discussed. Furthermore, separation/concentration equipment using hollow fiber membranes requires various system configurations depending on the processing purpose and characteristics of the processed material, but so-called modular systems have many configurations to meet these requirements. Let's talk about the difficulties.
また中空糸束エレメント複数個を筐体に装着し
たものを外圧循環式の分離膜装置として使用する
ことも考えられるが、循環液によつて中空糸膜
が、絡んだり、また損傷する恐れがある。 It is also possible to use a device with multiple hollow fiber bundle elements attached to a housing as an external pressure circulation type separation membrane device, but there is a risk that the hollow fiber membranes may become tangled or damaged by the circulating fluid. .
本発明はこれらの欠点を改良したもので、筐体
内に単数または複数の中空糸束エレメントおよび
筐体内を流体処理室と透過流体補集室に隔離し、
かつ中空糸束エレメントの開口端部を装着するた
めの隔板とを備えた分離膜装置において、各中空
糸束エレメントを内包する両端の開口した案内筒
を設け、案内筒の上部開口端から流体が中空糸エ
レメントにそつて流動するように構成されたこと
を特徴とする分離膜装置である。また本発明のよ
り好ましい態様は流体処理室を上下に二分するウ
イープホールを有する仕切板を有し、上部流体処
理室に循環流体の流入口を、下部流体処理室に濃
縮流体または逆洗用流体の排出口および循環液の
流出口を有する分離膜装置である。 The present invention improves these drawbacks, and includes one or more hollow fiber bundle elements within the housing, and the housing is separated into a fluid treatment chamber and a permeate fluid collection chamber,
In the separation membrane device, the separation membrane device is equipped with a partition plate for attaching the open ends of the hollow fiber bundle elements, and a guide tube with open ends at both ends that encloses each hollow fiber bundle element is provided, and the fluid is supplied from the upper open end of the guide tube. This is a separation membrane device characterized in that it is configured such that the liquid flows along a hollow fiber element. A more preferred embodiment of the present invention has a partition plate having a sweep hole that divides the fluid treatment chamber into upper and lower halves, with an inlet for circulating fluid in the upper fluid treatment chamber and an inlet for concentrated fluid or backwashing fluid in the lower fluid treatment chamber. This is a separation membrane device having an outlet and an outlet for circulating fluid.
本発明において流体とは代表的には液体である
ので、以下流体処理室を原液室、透過流体補集室
を透過液室として説明を加える。 In the present invention, the fluid is typically a liquid, so the following description will be made assuming that the fluid processing chamber is the raw liquid chamber and the permeated fluid collection chamber is the permeated liquid chamber.
本装置は１個のコンパクトな筐体内へ多数本の
中空糸束エレメントを装着でき、また各エレメン
ト毎に高速循環流が実現でき、必要な大量循環流
による中空糸束エレメントの損傷の可能性を減ら
し、かつ、下記に示すような多様なシステム運転
法に対応できるような構造を有している。 This device allows multiple hollow fiber bundle elements to be installed in one compact housing, and can achieve high-speed circulating flow for each element, reducing the possibility of damage to the hollow fiber bundle elements due to the large amount of circulating flow required. It has a structure that can reduce the number of units and accommodate various system operation methods as shown below.
逆洗方法…透過液逆洗、気体（空気または
N2）逆洗
循環方法…大循環（原液タンク→原液ポンプ
→分離膜装置→原液タンク）
小循環（原液タンク→原液ポンプ→分離膜装
置→循環ポンプ ）
濃縮方法…バツチ濃縮、連続濃縮（フイール
ドおよびブリード法）
濃縮液排出方法…バツチ排出、連続および間
欠排出
薬液による膜再生…浸漬法、循環法、循環お
よび気体逆洗
次に本発明の装置の一例を第１図により説明す
る。 Backwashing method…Permeate backwashing, gas (air or
N 2 ) Backwashing Circulation method…large circulation (stock solution tank → stock solution pump → separation membrane device → stock solution tank) small circulation (stock solution tank → stock solution pump → separation membrane device → circulation pump) Concentration method…batch concentration, continuous concentration ( Field and bleed method) Concentrate discharge method: Batch discharge, continuous and intermittent discharge Membrane regeneration by chemical solution: Immersion method, circulation method, circulation and gas backwashing Next, an example of the apparatus of the present invention will be explained with reference to FIG.
本装置は円筒竪形の筐体１と筐体内に単数ある
いは複数の中空糸膜束エレメント２および該エレ
メントを固着すると同時に被処理流体を原液室と
透過液室に隔離する隔板３及び各エレメント毎に
原液の流路を構成するための案内筒４及び原液側
室を実質的に上部室６と下部室７，８とに分割す
る仕切板５および各種流体の流入・出用の複数個
の口１０，１１，１２，１３，１４，１５，１６
にて構成される。 This device consists of a cylindrical vertical casing 1, one or more hollow fiber membrane bundle elements 2 inside the casing, a partition plate 3 that fixes the elements, and at the same time isolates the fluid to be treated into a raw liquid chamber and a permeated liquid chamber, and each element. A guide cylinder 4 for forming a flow path for the concentrate, a partition plate 5 for substantially dividing the concentrate side chamber into an upper chamber 6 and lower chambers 7 and 8, and a plurality of ports for inflow and outflow of various fluids. 10, 11, 12, 13, 14, 15, 16
Consists of.
本発明の装置を構成する主な部材の説明をす
る。 The main members constituting the device of the present invention will be explained.
筐体１…一般的に円形断面を有する竪形
処理条件（圧力・温度・腐食性）に応じた材質
から構成される。Housing 1: Generally vertical with a circular cross section. Constructed of a material suitable for processing conditions (pressure, temperature, corrosivity).
隔板２…原液側と透過液側の最大差圧に耐えうる
強度を有する板で、中空糸束を装着する穿たれ
た孔を中空糸束エレメント数だけ、例えば特開
昭54−145380号に記載されているような正三角
形状に設ける。Partition plate 2: A plate that has the strength to withstand the maximum differential pressure between the raw liquid side and the permeated liquid side, and has holes drilled for attaching the hollow fiber bundles as many as the number of hollow fiber bundle elements, for example, in JP-A No. 54-145380 Set up in the shape of an equilateral triangle as shown.
透過液室３…各中空糸エレメントを透過した透過
液を透過液流出口１２へ導くと同時に、逆洗流
体を各エレメントへ分配する室であると同時
に、エレメントのリーク検査・補修を行なう室
である。Permeated liquid chamber 3...A chamber that guides the permeated liquid that has permeated through each hollow fiber element to the permeated liquid outlet 12, and at the same time distributes backwash fluid to each element, and at the same time, a chamber that performs leak inspection and repair of the elements. be.
案内筒４…上・下両端共開孔した中空筒で、上端
部はラツパ状に開孔に向つて拡径し、下部へ向
つて滑らかに縮径している。縮径部以下は下端
迄同一口径の円筒状となつている。円筒内面は
全長にわたり滑らかである。上部拡径の目的は
装置へ中空糸束エレメントを装着する場合、装
入を容易にするため及び案内筒へ流入する液体
の狭小すぎない一定の流路断面積を確保するた
めである。縮径部以下の同一口径円筒部の内径
は中空糸束エレメントを容易に装入できる範囲
内でできるだけ小なる寸法としこれによつて円
筒内流路断面積をできるだけ小として循環流の
高速化および循環量の低減をはかつている。各
案内筒は各中空糸束エレメント毎に該エレメン
トと同心的に位置し、各案内筒の上端面は同一
水平面を構成するよう配置する。Guide cylinder 4: A hollow cylinder with holes at both the upper and lower ends, the upper end expanding in diameter toward the opening in a tulle shape, and decreasing smoothly toward the lower end. The part below the reduced diameter part is cylindrical with the same diameter up to the lower end. The inner surface of the cylinder is smooth over its entire length. The purpose of the upper diameter expansion is to facilitate the loading of the hollow fiber bundle element into the device and to ensure a constant flow path cross-sectional area that is not too narrow for the liquid flowing into the guide tube. The inner diameter of the cylindrical part of the same diameter below the reduced diameter part is made as small as possible within the range in which the hollow fiber bundle element can be easily inserted.Thereby, the cross-sectional area of the flow path in the cylinder is made as small as possible to increase the speed of circulation flow and Efforts are being made to reduce the amount of circulation. Each guide cylinder is located concentrically with each hollow fiber bundle element, and the upper end surfaces of each guide cylinder are arranged to form the same horizontal plane.
該上端面は隔板と一定の距離をもつて位置
し、案内筒上端・隔板・中空糸束エレメントの
３者にて形成される環状の案内筒流入流路を構
成する。各案内筒の全長は装置に中空糸束エレ
メントを装着した状態で、該エレメントの下端
より更に下方迄伸びているように設定して、案
内筒外部の流体の流動が中空糸に損傷を与える
ことの防止をはかる。すなわち、各案内筒は各
中空糸束エレメントの保護筒の役割りを併せ持
つものである。 The upper end surface is located at a certain distance from the partition plate, and constitutes an annular guide cylinder inflow channel formed by the upper end of the guide cylinder, the partition plate, and the hollow fiber bundle element. The total length of each guide tube is set so that when the hollow fiber bundle element is attached to the device, it extends further downward from the lower end of the element to prevent fluid flow outside the guide tube from damaging the hollow fibers. We aim to prevent this. That is, each guide tube also serves as a protection tube for each hollow fiber bundle element.
案内筒の平面配列すなわち中空糸束エレメン
トの平面配列は任意であるが、一般的に規則配
列が望ましい。案内筒中心軸間ピツチは装置の
コンパクト化及び案内筒外流体の上下方向平均
流速の観点より目的に応じた適正な値を選択す
ることができる。 Although the planar arrangement of the guide tubes, that is, the planar arrangement of the hollow fiber bundle elements, is arbitrary, a regular arrangement is generally desirable. The pitch between the center axes of the guide cylinder can be selected to be an appropriate value depending on the purpose from the viewpoint of compactness of the device and average vertical flow velocity of the fluid outside the guide cylinder.
仕切板５…仕切板５は原液室を実質的に上部原液
室と下部原液室に仕切る目的及び上記案内筒の
支持板の役割を果す。仕切板は上部原液室へ導
入された大量の循環液を実質的に仕切つて循環
液を各案内筒上部へ流動させると同時に仕切板
には１ケまたは複数ケのウイープホール１７を
有して、該上部原液室内の一部液又は残存液を
下部室へ流下させること及び原液または洗浄剤
のフイード時には下部室上部の気体を上部室へ
解放させる機能を有する必要上、及び後述の目
的のため完全なる隔絶板ではないことが好まし
い。該仕切り板を完全なる隔絶板とする場合
は、筐体の上部室下端部及び下部室上端部に片
口を設け両者を配管にて接続するのがよい。Partition plate 5: The partition plate 5 serves the purpose of substantially partitioning the stock solution chamber into an upper stock solution chamber and a lower stock solution chamber, and serves as a support plate for the guide cylinder. The partition plate substantially partitions a large amount of circulating liquid introduced into the upper stock liquid chamber and allows the circulating liquid to flow to the upper part of each guide cylinder.The partition plate has one or more weep holes 17 to It is necessary to have the function of allowing some liquid or residual liquid in the upper stock solution chamber to flow down to the lower room, and releasing the gas at the top of the lower room to the upper room when feeding the stock solution or cleaning agent, and for the purposes described below. Preferably, it is not a separator plate. If the partition plate is to be a complete isolation plate, it is preferable to provide one end at the lower end of the upper chamber and the upper end of the lower chamber of the casing and connect the two with piping.
上部原液室６…原液室６は仕切板上部の原液室
で、その下部の仕切板５の比較的近辺に一般に
大口径の循環液流入口１４と、上部の隔板３の
比較的近辺に流体オーバーフロー及び外気吸込
用の口１１を有する。循環液流入口より導入さ
れた大量・高速の流体は該室内で激しく乱れる
が、案内筒外部を降速された実質的な上昇流と
なつて案内筒上端へ達し、案内筒内で再び増速
された下降流となつて中空糸束表面を流動下降
する。循環液流入口１４を仕切板５の比較的近
辺（すなわち上部原液室の下部）に設ける理由
は案内筒４の上部開口端から原液が案内筒内部
に流動する場合の流動性の均一をはかるためで
ある。Upper stock solution chamber 6...The stock solution chamber 6 is a stock solution chamber at the top of the partition plate, and there is generally a large-diameter circulating fluid inlet 14 relatively near the partition plate 5 at the bottom, and a fluid inlet relatively near the partition plate 3 at the top. It has a port 11 for overflow and outside air intake. A large amount of high-speed fluid introduced from the circulating fluid inlet is violently turbulent in the chamber, but the flow is slowed down outside the guide cylinder, reaches the upper end of the guide cylinder, and speeds up again inside the guide cylinder. The fibers form a downward flow that flows down the surface of the hollow fiber bundle. The reason why the circulating fluid inlet 14 is provided relatively near the partition plate 5 (that is, at the bottom of the upper stock solution chamber) is to ensure uniform fluidity when the stock solution flows into the guide pipe from the upper open end of the guide pipe 4. It is.
下部原液室７…原液室７は仕切板下部の原液側室
で、中央部に原液導入用口１０及び下端に循環
液流出用口１３及び仕切板近辺に余剰の濃縮液
及び逆洗流体の排出口１５を有する。排出口１
５を仕切板５の近辺（すなわち下部原液室の上
部）に設ける理由は空気または液により逆洗
する場合、好都合になしうるからである。案内
筒下端面より下部の空胴部は装置の使用目的に
よつて多少構造の差を有するが、いずれにしろ
該空胴部は案内筒下端より噴出した濃縮液及び
逆洗流体の流動鎮静機能を果す。例えば後述の
気体逆洗方式で使用する場合、該空胴部を気液
分離場所に利用するため、空胴部の直径・高さ
を使用条件に見合つたものに変形したり、積極
的な気液分離部品を取り付けることもできる。Lower stock solution chamber 7...The stock solution chamber 7 is a stock solution side chamber at the bottom of the partition plate, and has a stock solution introduction port 10 at the center, a circulating fluid outflow port 13 at the lower end, and an outlet for excess concentrated liquid and backwash fluid near the partition plate. It has 15. Outlet 1
5 in the vicinity of the partition plate 5 (that is, in the upper part of the lower stock solution chamber) is that backwashing with air or liquid can be carried out conveniently. The structure of the cavity below the lower end of the guide tube varies depending on the purpose of use of the device, but in any case, the cavity has a function of calming the flow of the concentrated liquid and backwash fluid spouted from the lower end of the guide tube. fulfill. For example, when using the gas backwashing method described below, the cavity is used as a gas-liquid separation site, so the diameter and height of the cavity may be modified to match the usage conditions, or active air purification may be required. Liquid separation components can also be installed.
中空糸束エレメント２…本発明による装置に適用
する中空糸束エレメントは下記の如きである。Hollow fiber bundle element 2: The hollow fiber bundle element applicable to the apparatus according to the present invention is as follows.
中空糸として再生セルロース系、セルロース
誘導体、ポリビニルアルコール系、ポリアクリ
ロニトリル系、ポリメチルメタクリレート系、
ポリアミド系、ポリオレフイン系、ポリ塩化ビ
ニル系、シリコンゴム系、ポリサルフオン系等
各種ポリマーが使用できる。中空糸膜は外径が
50ないし4000μ、膜厚が数ないし500μ程度のも
のである。中空糸長は500ないし2000mm程度で
ある。これら中空糸は数百本から数十万本程度
とりまとめ束とされる。これを中空糸束とす
る。中空糸束は、一端を接着剤又は集束具にて
一体化し、中空糸孔を開孔させ、他端は単位中
空糸毎に中空糸孔を閉塞し、中空糸間は一体化
せず自由にする。接着端はハウジングへ装着す
るための任意の構造と流体をシールするシール
材を密着させるシール面を有する。すなわち、
一端を固定端とし、実質的に真直な中空糸束か
らなるいわゆる片持ち型のエレメントが本発明
による装置に適用する中空糸束エレメントとな
る。 As hollow fibers, regenerated cellulose, cellulose derivatives, polyvinyl alcohol, polyacrylonitrile, polymethyl methacrylate,
Various polymers can be used, such as polyamide, polyolefin, polyvinyl chloride, silicone rubber, and polysulfone. Hollow fiber membrane has an outer diameter of
The film thickness is about 50 to 4000μ, and the film thickness is about 500μ. The hollow fiber length is about 500 to 2000 mm. Several hundred to several hundred thousand of these hollow fibers are grouped together into a bundle. This is called a hollow fiber bundle. The hollow fiber bundle is made by combining one end with adhesive or a binding tool and opening the hollow fiber holes, and closing the hollow fiber holes for each unit hollow fiber at the other end, leaving the hollow fibers free without being unified. do. The adhesive end has an optional structure for attachment to the housing and a sealing surface for contacting a fluid sealing material. That is,
A so-called cantilevered element consisting of a substantially straight hollow fiber bundle with one end fixed is the hollow fiber bundle element applied to the device according to the present invention.
またこれらの膜は本発明の装置を適用する用
途によつて均一微細構造膜（平均孔径0.01〜1μ
程度のもの）、非対称構造を有する各種限外
過膜などを適宜選択して用いることができる。 In addition, these membranes may have a uniform microstructure (average pore size of 0.01 to 1μ) depending on the application of the device of the present invention.
various ultrafiltration membranes having an asymmetric structure can be appropriately selected and used.
次に本発明の実施例を示す第１図を組み込んだ
分離濃縮システムを示す第２図を参照しつつ説明
する。 Next, an explanation will be given with reference to FIG. 2, which shows a separation and concentration system incorporating FIG. 1, which shows an embodiment of the present invention.
(1) フイード工程
全バルブ閉止状態よりバルブ５，３，２，１
を開き原液ポンプ１５により原液を装置２６の
原液側下部室内へフイードする。フイードされ
た原液は案内筒に衝突しながら装置底部へ流下
し、次第に装置２６、循環ポンプ１６、循環パ
イプ１７を充満してゆく、その際この系内の残
存空気はバルブ３より排出される。充満したら
バルブ３を閉じる、この状態で系内は所定圧に
加圧されている。(1) Feed process Valve 5, 3, 2, 1 from all valves closed state
is opened and the stock solution pump 15 feeds the stock solution into the lower chamber on the stock solution side of the device 26. The fed stock solution flows down to the bottom of the device while colliding with the guide cylinder, and gradually fills the device 26, circulation pump 16, and circulation pipe 17. At this time, residual air in this system is discharged from the valve 3. When the system is full, the valve 3 is closed. In this state, the inside of the system is pressurized to a predetermined pressure.
(2) 分離・濃縮工程
この状態で循環ポンプ１６を作動させると、
原液は循環ポンプ１６により昇圧され、装置２
６の原液側上部室へ流入する。該室内案内筒外
部が循環液の上昇流路となり、この上昇流は各
案内筒上端隔板・中空糸束固定端で形成された
同心環状流となり案内筒内部へ流入し、中空糸
の軸方向に中空糸外側表面を高速流となつて流
下し、案内筒先端に達する。この間に中空糸膜
を透過できる流体成分は選択的に中空糸内へ透
過し中空糸内を上昇し、透過液室へ達し、バル
ブ２を通つて透過液タンク１９へ達する。一
方、中空糸膜を透過しない流体成分は原液側下
部室へ集められ、あらたにフイードされる原液
と混合され濃縮された循環液となり、上記の作
用を繰り返し、分離・濃縮が進行する。上部と
下部室の圧力差によりウイープホール内は上か
ら下への少液流が存在するから、何らかの理由
で混入・発生した気泡は仕切板下面に停滞し、
上部室へ上昇することがないから気体が循環系
を繰り返し流動することによる弊害は阻止され
る。ウイープホールは通常１〜５mmの孔径のも
のが設けられる。(2) Separation/concentration process When the circulation pump 16 is operated in this state,
The stock solution is pressurized by the circulation pump 16 and transferred to the device 2.
It flows into the upper chamber on the stock solution side of No. 6. The outside of the guide cylinder in the interior becomes an upward flow path for the circulating fluid, and this upward flow becomes a concentric annular flow formed by the partition plate at the upper end of each guide cylinder and the fixed end of the hollow fiber bundle, flows into the inside of the guide cylinder, and flows in the axial direction of the hollow fibers. Then, it flows down the outer surface of the hollow fiber as a high-speed flow and reaches the tip of the guide cylinder. During this time, fluid components that can permeate through the hollow fiber membranes selectively permeate into the hollow fibers, rise within the hollow fibers, reach the permeate chamber, and reach the permeate tank 19 through the valve 2. On the other hand, fluid components that do not pass through the hollow fiber membrane are collected in the lower chamber on the stock solution side, mixed with the newly fed stock solution to become a concentrated circulating fluid, and the above actions are repeated to advance separation and concentration. Due to the pressure difference between the upper and lower chambers, there is a small flow of liquid from the top to the bottom inside the weep hole, so air bubbles that get mixed in or occur for some reason stagnate on the bottom surface of the partition plate.
Since the gas does not rise to the upper chamber, the adverse effects of repeated flow of gas through the circulation system are prevented. The weep hole is usually provided with a hole diameter of 1 to 5 mm.
システムによつては、循環液濃度を事実上一
定に維持して分離を進行させる場合がある。こ
の際は、バルブ４を介して循環液の一部を透過
液量・フイード原液量に見合つた量だけ濃縮液
として連続的に排出しながら工程を進めること
ができる。 In some systems, the circulating fluid concentration may be maintained virtually constant to allow separation to proceed. At this time, the process can proceed while continuously discharging a part of the circulating liquid as a concentrated liquid through the valve 4 in an amount commensurate with the amount of permeated liquid and the amount of raw feed liquid.
(3) 逆洗工程
所定時間または所定濃縮倍率まで分離・濃縮
が進行した時、膜性能を回復させるため、透過
液・他の清澄な液体・気体（空気あるいは窒素
など）による逆洗作用を中空糸膜に対して行な
うことが有効な場合には下記のように行なう。(3) Backwashing process When separation and concentration have progressed for a specified time or to a specified concentration ratio, the backwashing action using permeate, other clear liquids, and gases (air or nitrogen, etc.) is performed in order to restore membrane performance. If it is effective to perform the procedure on the thread membrane, perform it as follows.
(1) 透過液逆洗
各バルブ類を分離濃縮状態から、４，１３
を開、２，１を閉とし、逆洗ポンプ２４を作
動させると装置２６内の循環液は分離濃縮状
態より低い圧力レベルとなつて循環しなが
ら、透過液が透過液室→中空糸内部→案内筒
内の方向に流れ、逆洗作用を行なう、装置２
６内に持ち込まれた透過液に相当する量の濃
縮液がバルブ４より装置外に排出される。一
般に透過液逆洗時間は数〜十数秒の短時間で
終了することが多いから、引き続き分離・濃
縮工程へ入るためにはバルブ４，１３を閉、
２，１を開とするだけで十分である。 (1) Backwashing of permeated liquid Separate and concentrate each valve from 4, 13
When 2 and 1 are opened, 2 and 1 are closed, and the backwash pump 24 is operated, the circulating liquid in the device 26 is circulated at a pressure level lower than that in the separation and concentration state, and the permeate flows from the permeate chamber → inside the hollow fiber → Device 2 that flows in the direction inside the guide cylinder and performs a backwashing action
An amount of concentrated liquid corresponding to the permeated liquid brought into the chamber 6 is discharged from the apparatus through the valve 4. Generally, the permeate backwashing time often ends in a short period of several to ten seconds, so in order to continue the separation and concentration process, close the valves 4 and 13.
It is sufficient to open 2.1.
(2) 気体逆洗
各バルブ類を分離濃縮状態から、４，１４
を開、２，１を閉とすると装置２６内の循環
液は上記同様循環しながら、逆洗気体が透過
液室→中空糸中部→案内筒内の方向に流れ、
更に膜面より噴出した微細気泡は一部気塊に
成長しながら案内筒内を高速循環液と混合し
ながら案内筒下端へ向つて流下しながら、中
空糸膜の洗浄を行なう。一般に気体逆洗は原
液側の中空糸不透過成分にSS分が多い場合
に多用され、中空糸膜外表面へ付着堆積する
SS分を除去する目的に効果的である。逆洗
時間は数十秒〜数分程度である。案内筒下端
より流下した気液混合物は原液側下部室の空
胴部で流動が鎮静化しながら、気体は上昇し
案内筒外部を通つて仕切板下部に達しバルブ
４より装置外に排出される。この際一般的に
は該気体に同伴して濃縮液の一部が装置外へ
排出されることが多い。従つて逆洗終了後、
仕切板下部には、濃縮液の液面低下によつて
気体が占める空間が発生することが多いか
ら、引き続き分離・濃縮工程へ入る前には下
記(5)の補液工程を経ることになる。 (2) Gas backwashing Separate and concentrate each valve from 4, 14
When 2 and 1 are opened and 2 and 1 are closed, the circulating liquid in the device 26 circulates in the same manner as described above, and the backwash gas flows in the direction of the permeate chamber → the hollow fiber middle → the inside of the guide cylinder.
Furthermore, some of the fine bubbles ejected from the membrane surface grow into air masses inside the guide tube, mixing with the high-speed circulating liquid and flowing down toward the lower end of the guide tube, thereby cleaning the hollow fiber membrane. In general, gas backwashing is often used when there is a large amount of SS in the hollow fiber impermeable component on the raw solution side, and it adheres and accumulates on the outer surface of the hollow fiber membrane.
Effective for removing SS content. The backwashing time is about several tens of seconds to several minutes. While the flow of the gas-liquid mixture flowing down from the lower end of the guide tube is stabilized in the cavity of the lower chamber on the raw solution side, the gas rises, passes through the outside of the guide tube, reaches the lower part of the partition plate, and is discharged from the apparatus through the valve 4. At this time, a part of the concentrated liquid is generally discharged out of the apparatus together with the gas. Therefore, after backwashing,
Since a space occupied by gas is often generated at the bottom of the partition plate due to a drop in the liquid level of the concentrated liquid, the liquid replacement process described in (5) below must be performed before proceeding to the subsequent separation and concentration process.
(4) 部分排出工程
逆洗工程の機会に濃縮液を装置外へ積極的に
排出することが好都合な場合がある。前記の気
体逆洗による逆同伴を積極的に利用するのもそ
の一例であるが、一般的には逆洗後、循環ポン
プ１６を停止し、バルブ４，３を開き、バルブ
３より外気を吸込みながら濃縮液をバルブ４よ
り装置外へ排出する。装置の構造上、液の自然
流下を利用して、原液側上部室容積にほぼ相当
する濃縮液を定量的に装置外へ排出することが
できる。(4) Partial draining process It may be convenient to actively drain the concentrated liquid out of the device during the backwashing process. One example of this is to actively utilize the back entrainment through gas backwashing, but generally after backwashing, the circulation pump 16 is stopped, valves 4 and 3 are opened, and outside air is sucked in through valve 3. While doing so, the concentrated liquid is discharged from the device through valve 4. Due to the structure of the device, by utilizing the natural flow of the liquid, it is possible to quantitatively discharge the concentrated liquid approximately equivalent to the volume of the upper chamber on the undiluted solution side out of the device.
(5) 補修及び分離・濃縮工程
逆洗後、再び分離濃縮工程へ入る為には、上
記(1)フイールド工程の動作により補液を行な
い、ついで上記(2)分離・濃縮工程の動作を繰り
返す。(5) Repair and separation/concentration process After backwashing, in order to enter the separation/concentration process again, replace the fluid by performing the above (1) field process, and then repeat the above (2) separation/concentration process.
(6) 排出工程
装置２６および循環系１６，１７内の全濃縮
液を排出するには、全バルブ閉、循環ポンプ１
６停止の状態にし、外気吸込用にバルブ３を開
とし循環系最下部に位置するバルブ７を開い
て、該液を流下させる。この際、装置内に残存
する透過液の完全排出を必要とする場合は、逆
洗弁１４より気体を導入していわゆる押抜きを
実施することもできる。(6) Discharge process To discharge all the concentrated liquid in the device 26 and the circulation systems 16 and 17, close all valves and close the circulation pump 1.
6, the system is stopped, valve 3 is opened to take in outside air, and valve 7 located at the lowest part of the circulation system is opened to allow the liquid to flow down. At this time, if it is necessary to completely discharge the permeate remaining in the apparatus, it is also possible to introduce gas from the backwash valve 14 to perform so-called punching.
(7) 洗浄・再生工程
使用により汚染あるいは性能低下した中空糸
膜の洗浄・再生には、洗浄水・洗剤・酸又はア
ルカリ等の薬液を用いる。洗浄・再生法は極め
て多用な方式が採用できるが、本装置では原液
側室へ原液に代え、上記洗浄剤を導入すること
によつて、充満・浸漬・循環・気体逆洗の併用
等の多くの組合せから任意の方法を選択するこ
とが可能である。動作は上記各工程説明により
容易に推察されよう。(7) Cleaning and regeneration process To clean and regenerate hollow fiber membranes that have become contaminated or have deteriorated in performance due to use, cleaning water, detergents, and chemicals such as acids or alkalis are used. A wide variety of methods can be used for cleaning and regeneration, but with this device, by introducing the above-mentioned cleaning agent into the undiluted solution side chamber instead of the undiluted solution, many methods such as filling, immersion, circulation, and gas backwashing can be used. It is possible to select any method from the combination. The operation can be easily inferred from the above description of each step.
以下のとおり本発明の分離膜装置はコンパクト
な装置でもつて効率よくしかも中空糸膜の損傷な
く大量の液を外圧循環式により処理できるので、
各種工業用、たとえばでんぷん糖化液（異性化
糖、グルコース糖化液など）、庶糖液、などの食
品工業用、河川、水、および水道水などの洗化
用、廃水処理用として有効に使用できる。 As described below, the separation membrane device of the present invention is a compact device that can process a large amount of liquid efficiently and without damaging the hollow fiber membrane by external pressure circulation.
It can be effectively used for various industrial purposes, for example, for the food industry such as starch saccharification solutions (isomerized sugar, glucose saccharification solutions, etc.), sucrose solutions, for washing rivers, water, tap water, etc., and for wastewater treatment.
第１図は本発明による分離濃縮装置の構造の一
例を示す縦断面図である。
１は筐体、２は中空糸束エレメント、３は隔
板、４は案内筒、５は仕切板、６は上部原液室、
７は下部原液室、８は下部原液室空胴部、９は透
過液室、１０は原液流入口、１１は原液オーバー
フロー・外気取入口、１２は透過液流出・逆洗流
体流入口、１３は濃縮液流出口、１４は循環濃縮
液流入口、１５は濃縮液または逆洗流体排出口、
１６は透過液室エアー抜口、１７はウイープホー
ルを示す。
第２図は本発明による分離濃縮装置を用いた分
離濃縮システムの一例を示す説明図である。
１，２，３，４，５，６，７，８，９，１０，
１１，１２，１３，１４はバルブ、１５は原液ポ
ンプ、１６は循環ポンプ、１７は循環パイプ、１
８は原液タンク、１９は透過液タンク、２０は濃
縮液タンク、２１は逆洗気体タンク、２２は洗浄
剤タンク、２３は廃洗浄剤タンク、２４は逆洗ポ
ンプ、２５は洗浄剤ポンプ、２６は分離濃縮装置
を示す。
FIG. 1 is a longitudinal sectional view showing an example of the structure of a separation and concentration apparatus according to the present invention. 1 is a housing, 2 is a hollow fiber bundle element, 3 is a partition plate, 4 is a guide cylinder, 5 is a partition plate, 6 is an upper stock solution chamber,
7 is the lower stock solution chamber, 8 is the lower stock solution chamber cavity, 9 is the permeate chamber, 10 is the stock solution inlet, 11 is the stock solution overflow/outside air intake port, 12 is the permeate outflow/backwash fluid inlet, 13 is the 14 is a circulating concentrate inlet; 15 is a concentrate or backwash fluid outlet;
Reference numeral 16 indicates a permeated liquid chamber air outlet, and reference numeral 17 indicates a weep hole. FIG. 2 is an explanatory diagram showing an example of a separation and concentration system using the separation and concentration apparatus according to the present invention. 1, 2, 3, 4, 5, 6, 7, 8, 9, 10,
11, 12, 13, 14 are valves, 15 is a stock pump, 16 is a circulation pump, 17 is a circulation pipe, 1
8 is a stock solution tank, 19 is a permeate tank, 20 is a concentrated liquid tank, 21 is a backwash gas tank, 22 is a cleaning agent tank, 23 is a waste cleaning agent tank, 24 is a backwashing pump, 25 is a cleaning agent pump, 26 indicates a separation/concentration device.
Claims (1)
トを有し、さらに筐体内を流体処理室と透過流体
補集室に隔離し、かつ中空糸束エレメントの開口
端部を装着するための隔板とを備えた分離膜装置
において、各中空糸束エレメントを内包する両端
の開口した、内面が全長にわたり滑らかな案内筒
を設け、案内筒の上部開口端から流体が中空糸束
エレメントにそつて流動するように構成されたこ
とを特徴とする分離膜装置。 ２ 流体処理室を上下に二分する仕切板を有し、
上部流体処理室に循環流体の流入口を、下部流体
処理室に循環流体の流出口を有する特許請求の範
囲第１項記載の分離膜装置。 ３ 仕切板がウイープホールを有する特許請求の
範囲第２項記載の分離膜装置。 ４ 分離膜装置が外圧循環式分離膜装置である特
許請求の範囲第１、第２または第３項記載の分離
膜装置。[Scope of Claims] 1. A housing having one or more hollow fiber bundle elements, further separating the inside of the housing into a fluid treatment chamber and a permeated fluid collection chamber, and mounting an open end of the hollow fiber bundle element. In a separation membrane device equipped with a partition plate for separating each hollow fiber bundle element, a guide tube with open ends and a smooth inner surface over the entire length is provided, and the fluid flows from the upper open end of the guide tube into the hollow fiber bundle. A separation membrane device characterized in that it is configured to flow along an element. 2. It has a partition plate that divides the fluid treatment chamber into upper and lower halves,
The separation membrane device according to claim 1, wherein the upper fluid treatment chamber has an inlet for circulating fluid, and the lower fluid treatment chamber has an outlet for circulating fluid. 3. The separation membrane device according to claim 2, wherein the partition plate has a weep hole. 4. The separation membrane device according to claim 1, 2 or 3, wherein the separation membrane device is an external pressure circulation type separation membrane device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11953581A JPS5820206A (en) | 1981-07-29 | 1981-07-29 | Separation membrane apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11953581A JPS5820206A (en) | 1981-07-29 | 1981-07-29 | Separation membrane apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5820206A JPS5820206A (en) | 1983-02-05 |
| JPS6351045B2 true JPS6351045B2 (en) | 1988-10-12 |
Family
ID=14763684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11953581A Granted JPS5820206A (en) | 1981-07-29 | 1981-07-29 | Separation membrane apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5820206A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017070915A (en) * | 2015-10-08 | 2017-04-13 | 株式会社クラレ | Washing method of hollow fiber membrane module and filtration device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02265627A (en) * | 1989-11-21 | 1990-10-30 | Toshiba Corp | Filter device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55324U (en) * | 1978-05-19 | 1980-01-05 |
-
1981
- 1981-07-29 JP JP11953581A patent/JPS5820206A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55324U (en) * | 1978-05-19 | 1980-01-05 |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017070915A (en) * | 2015-10-08 | 2017-04-13 | 株式会社クラレ | Washing method of hollow fiber membrane module and filtration device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5820206A (en) | 1983-02-05 |
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