JPH0531301A - Continuous heat exchanger in heating concentrator - Google Patents
Continuous heat exchanger in heating concentratorInfo
- Publication number
- JPH0531301A JPH0531301A JP21312891A JP21312891A JPH0531301A JP H0531301 A JPH0531301 A JP H0531301A JP 21312891 A JP21312891 A JP 21312891A JP 21312891 A JP21312891 A JP 21312891A JP H0531301 A JPH0531301 A JP H0531301A
- Authority
- JP
- Japan
- Prior art keywords
- raw material
- heat exchanger
- pipe
- steam
- pressure
- 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
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、加熱濃縮機における連
続熱交換器に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a continuous heat exchanger in a heating concentrator.
【０００２】[0002]
【従来の技術】従来食品、有機薬剤などの濃縮工程にお
いて使用する熱交換器は、きわめて複雑な構造であり、
その製造工程にも多くの難点を持っていた。例えば、特
公昭２６−７８１１号公報に記載されたものは、加熱管
内にスケーリング及び閉塞をおこした場合、洗浄不可能
であり、長尺螺旋状管の取り替えが必要となり不経済で
ある。その構造は複雑であり、機能も良好とは言えない
ものであった。又、本発明者は、これを改良した特公昭
６０−２５５０２号のシリンダー型エバポレーターを開
発したが、これも構造が複雑であり、また中筒の廻転に
相当のエネルギーを要するものである。2. Description of the Related Art Conventionally, heat exchangers used in the process of concentrating foods, organic chemicals, etc. have extremely complicated structures,
The manufacturing process also had many difficulties. For example, the one disclosed in Japanese Examined Patent Publication No. 26781/1996 is uneconomical because it cannot be cleaned when the heating tube is scaled and blocked, and the long spiral tube must be replaced. Its structure was complicated and its function was not good. The inventor of the present invention has developed a cylinder type evaporator of JP-B-60-25502, which is an improved version of this, but it also has a complicated structure and requires a considerable amount of energy to rotate the middle cylinder.
【０００３】[0003]
【発明が解決しようとする課題】そこで本発明者は、出
来るだけシンプルな機構で、しかも効率がよく、特に粘
性のある物質でも支障なく連続加熱濃縮せしめるため、
原料供給管の内方と外方より加熱せしめ、効率よく短時
間で次工程の常圧もしくは減圧域は、加圧蒸発室に移行
せしめるような課題を追及して、本発明となったもので
ある。Therefore, the present inventor intends to continuously heat-concentrate even a viscous substance with no trouble by using a mechanism as simple as possible and efficient.
By heating from the inside and outside of the raw material supply pipe, and efficiently and in a short time, the normal pressure or reduced pressure region of the next step pursues the problem of shifting to the pressure evaporation chamber, which is the present invention. is there.
【０００４】[0004]
【課題を解決するための手段】中心にスチーム導入管を
設けたスチームコアーを内側加熱管とし、外側にスチー
ムジャケットで包囲した横断面が環状の原料上昇管と
し、その下方は、漏斗状に拡大した原料分配供給ボック
スとし、上方において合体して１本の排出管とし、その
先方に常圧もしくは減圧域は加圧蒸発室に通じるように
したもので、原料は環状の原料上昇管を上昇する間に加
熱、ペーパーライズし、被加熱原料の粘性の影響がおよ
び、発生ベーパーによる撹拌効果により超高速流とな
り、熱移動せしめ、連続的に加熱又は加圧し、これを直
ちに常圧もしくは減圧あるいは加圧蒸発室に移送するも
のである。[Means for Solving the Problems] A steam core having a steam introduction pipe in the center is used as an inner heating pipe, and a raw material rising pipe having an annular cross section surrounded by a steam jacket is formed on the outer side. This is a raw material distribution and supply box, which is united at the top to form a single discharge pipe, and the normal pressure or reduced pressure region is connected to the pressure vaporization chamber at the other end, and the raw material rises in an annular raw material rising pipe. During heating and paper rise, the influence of the viscosity of the raw material to be heated and the stirring effect of the generated vapor result in an ultra-high-speed flow, causing heat transfer and continuous heating or pressurization. It is transferred to the pressure evaporation chamber.
【０００５】なお本発明を実施例である図面について説
明すると、１０は環状の原料上昇管であり、その下方は
下部が逆漏斗状に拡大した原料分配ボックスとなり、そ
の一部に原料入口８が設けられ、上部は合体して１本の
排出管１１に結合するようにする。この環状の原料上昇
管１０の外周は、スチームジャケット１により包囲され
ていて、上方の一端にスチーム入口４が設けられ、下方
にドレーン排出口５が設けられる。The present invention will now be described with reference to the drawings showing an embodiment of the present invention. Reference numeral 10 denotes a ring-shaped raw material rising pipe, and a lower portion thereof is a raw material distribution box whose lower part is expanded in a reverse funnel shape, and a raw material inlet 8 is provided in a part thereof. It is provided so that the upper part is united and connected to one discharge pipe 11. The outer circumference of the annular raw material rising pipe 10 is surrounded by the steam jacket 1, the steam inlet 4 is provided at one end on the upper side, and the drain discharge port 5 is provided on the lower side.
【０００６】また、環状の原料上昇管１０の内側中心に
周囲に細孔を有するスチーム導入管３が設けられ、下方
にはスチーム入口とその側方にドレーン出口７が設けら
れる。そして、このスチーム導入管は上部は閉塞されて
いるが、外周には上記のように細孔があるので、これか
ら加熱蒸気が原料上昇管１０内側加熱のためのスチーム
コア２に供給されるものである。Further, a steam introducing pipe 3 having pores in the periphery is provided at the center of the inside of the annular raw material rising pipe 10, and a steam inlet and a drain outlet 7 are provided at the lower side thereof. The steam introducing pipe is closed at the upper part, but since the outer periphery has pores as described above, the heating steam is supplied to the steam core 2 for heating the inside of the raw material rising pipe 10. is there.
【０００７】上述した本発明の熱交換器の原料上昇管の
上方先端は、合体して結合部１１となり、これより先方
の蒸発室（図１では減圧蒸発室１３となっており、その
先方にはコンデンサー１５を介して、真空ポンプ１６と
連結している。）The upper ends of the raw material rising pipes of the heat exchanger of the present invention described above are united to form a joint portion 11, and a vaporization chamber (a reduced pressure vaporization chamber 13 in FIG. 1) ahead of this is formed. Is connected to a vacuum pump 16 via a condenser 15.)
【０００８】しかして、上記は減圧蒸発室であるが、こ
れを図３及び図４に示す常圧濃縮又は加圧濃縮として使
用することも本発明の要旨とするものである。Although the above is the reduced pressure evaporation chamber, it is also the subject matter of the present invention to use it as the atmospheric concentration or the pressurized concentration shown in FIGS. 3 and 4.
【０００９】そこで、図３及び図４の常圧及び加圧濃縮
について説明する。本発明の熱交換器より、原料上昇管
１０により上昇してきた原料を気液分離を行なう蒸発室
１３に移送せしめ、ここで気液分離を行ない、蒸気は上
方のブロワー１９又はエキゾストパイプ（煙突）２１に
より外方２０に移送され、被加工原料は濃縮乾燥され、
濃縮液または粉末状となって、下方の蒸発室出口１４よ
り適宜に取り出すことができる。また加圧方式にするに
は、本発明の熱交換器は、原料を一定圧力で供給し、原
料上昇管を急速に上昇し、加圧器と蒸発室の間のバルブ
を調整（絞る）することにより、上昇管中の原液が加圧
され、蒸発室１３に移行し、ここで気液分離されるとと
もに、蒸気は上方のブロワーまたは煙突２１により外気
に排出され、濃縮液又は乾燥粉末化された被加工物は、
排出口１４より取り出すものである。上述した様に本発
明熱交換器より先の蒸発室の形態は、被加工原料の性状
に応じて利用者の選択にまかされる。Therefore, the normal pressure and pressure concentration of FIGS. 3 and 4 will be described. From the heat exchanger of the present invention, the raw material rising by the raw material rising pipe 10 is transferred to an evaporation chamber 13 for gas-liquid separation, where vapor-liquid separation is performed, and steam is blower 19 above or an exhaust pipe (chimney stack). ) 21 is transferred to the outside 20 and the raw material to be processed is concentrated and dried,
It becomes a concentrated liquid or powder and can be appropriately taken out from the outlet 14 of the lower evaporation chamber. In order to use the pressurizing method, the heat exchanger of the present invention supplies the raw material at a constant pressure, rapidly raises the raw material rising pipe, and adjusts (throttles) the valve between the pressurizer and the evaporation chamber. As a result, the stock solution in the ascending pipe is pressurized and transferred to the evaporation chamber 13, where it is separated into gas and liquid, and the vapor is discharged to the outside air by the blower or chimney 21 at the upper side to be a concentrated liquid or a dry powder. The work piece is
It is taken out from the discharge port 14. As described above, the form of the evaporation chamber prior to the heat exchanger of the present invention is left to the user's selection depending on the properties of the raw material to be processed.
【００１０】[0010]
【作用】本発明の上記構成により、その使用法と作用を
説明すると、横断面（又は平面）環状原料上昇管１０の
下方に設けた原料入口８より被濃縮物原料を一定圧力に
より定量導入し、下方が拡大され漏斗状の原料分配供給
ボックス９において原料は一様に拡大され、次いで細め
られた原料上昇管１０に導かれ、その内外両側に設けた
スチームコアー２及びスチームジャケット１により急速
に加熱され、１５０ｍｍ〜２００ｍｍ上昇したところで
沸騰が始まり、被加熱原料の粘性及び発生ベーパーによ
り撹拌加速され、原料上昇管１０を上昇し、強力なクリ
ーニング効果をともない機械的掻き取りに近い状況を創
り出し、高い伝熱係数が得られた。一方、製品の加熱器
即ち熱交換器内の滞留時間は、平均３〜１５秒と非常に
短く、そのため製品の劣化が認められなかった。With the above-described structure of the present invention, its usage and operation will be described. The raw material to be concentrated is quantitatively introduced at a constant pressure from the raw material inlet 8 provided below the cross-section (or plane) annular raw material rising pipe 10. The raw material is uniformly expanded in the funnel-shaped raw material distribution / supply box 9 whose lower part is expanded, and then the raw material is guided to the narrowed raw material rising pipe 10 and rapidly by the steam core 2 and the steam jacket 1 provided on both inner and outer sides thereof. When heated, the boiling starts when the temperature rises by 150 mm to 200 mm, stirring is accelerated by the viscosity of the raw material to be heated and the generated vapor, the raw material rising pipe 10 is raised, and a situation close to mechanical scraping with a strong cleaning effect is created, A high heat transfer coefficient was obtained. On the other hand, the residence time of the product in the heater, that is, the heat exchanger was very short, on average, 3 to 15 seconds, so that no deterioration of the product was observed.
【００１１】そして、上方の合体点１１において一本の
排出管１２に連結して、次いでコンデンサー、真空ポン
プ等の真空発生装置により減圧された蒸発室１３の側方
又は上部に導入され、気液分離し、濃縮液又は乾燥状態
となり、下方の排出口から適時排出される。Then, it is connected to a single discharge pipe 12 at an upper joining point 11 and then introduced to a side or an upper part of an evaporation chamber 13 which is decompressed by a vacuum generator such as a condenser or a vacuum pump. Separated, it becomes a concentrated liquid or a dried state, and it is discharged from the lower discharge port at appropriate time.
【００１２】[0012]
（実施例１） 外筒（スチームジャケット）の内径 ４９．５ｍｍ 内筒（スチームコアー２）の内径 ４２．７ｍｍ 原料上昇管１０の間隙３．４ｍｍ 熱交換器の長さ ２０００ｍｍ 伝熱面積 ０．５８ｍ2 の実験機を使用して、 キャンデー材料 砂糖 ６０％ 水飴 ４０％ を溶解し、水分２５％に調整して下記の操作条件で実施
した。 蒸気圧 ７ｋｇ／ｃｍ2 Ｇ（１６９．６℃） 真空度 ３０〜４０Ｔｏｒｒ 蒸発室製品の出口温度 １２０℃〜１２５℃ 結果 原液組成 ２５％水分 原液量 １９８ｋｇ／ｈｒ を処理し、下記の製品が得られた。 製品組成 １〜１．５ｐｉｔ％ 製品量 １５０ｋｇ／ｈｒ 蒸発量 ４８ｋｇ／ｈｒ 従来の方法（特許第１８７６２２号）よりも生産能力２
０ｋｇ／ｈｒ以上多く、色彩も透明であり、非常によい
製品が得られた。 （実施例２）実施例１と同じ装置により、ＤＥ２０の低
濃度水飴を濃縮乾燥を行なった。 操作条件 蒸気圧 ７ｋｇ／ｃｍ2 Ｇ（１６９．６℃） 真空度 ２０Ｔｏｒｒ以下 蒸発室出口温度 １３５℃ 結果 原液組成 １８％（水分） 原液量 ２８．５ｋｇ／ｈｒ を処理し、下記の粉末状製品が得られた。 製品組成 １〜３％（水分） 製品量 ２４ｋｇ／ｈｒ 蒸発量 ４．５ｋｇ／ｈｒ 従来の装置では粉末化は不可能であったが白色でポーラ
スな（グラニオン状）溶解度のよい粉末製品が得られ
た。 （実施例３） 実施例１と同様の装置で実施したハードキャンデー原料 砂糖 ８０％ 水飴 ２０％ の配合比率で加水し溶解し、水分２５％に調整して下記
の操作条件で実施した。 スチーム圧力 ９ｋｇ／ｃｍ2 Ｇ（１７９℃） 蒸発室圧力 常圧（大気） 蒸発室製品出口温度 １６０℃〜１６５℃ 結果 １．原液量１５０ｋｇ／ｈｒを処理し、下記の製品が得
られた。 製品組成 １．５〜２％（水分） 製品量 １５０ｋｇ／ｈｒ 蒸発量 ３７ｋｇ／ｈｒ 従来の方法（特許第１８７６２２号）のコイル型の濃縮
機と比較し、着色も少なく透明度もよく、能力増加の非
常によい製品が得られた。(Example 1) Inner diameter of outer cylinder (steam jacket) 49.5 mm Inner diameter of inner cylinder (steam core 2) 42.7 mm Gap of raw material riser pipe 3.4 mm Length of heat exchanger 2000 mm Heat transfer area 0.58 m Using the experimental machine of No. 2 , the candy material, sugar 60%, starch syrup 40% was dissolved, the water content was adjusted to 25%, and the experiment was carried out under the following operating conditions. Vapor pressure 7 kg / cm 2 G (169.6 ° C.) Vacuum degree 30-40 Torr Evaporation chamber product outlet temperature 120 ° C.-125 ° C. Result Undiluted solution composition 25% Moisture Undiluted solution amount 198 kg / hr The following product was obtained It was Product composition 1-1.5 pit% Product amount 150 kg / hr Evaporation amount 48 kg / hr Production capacity 2 than the conventional method (Patent No. 187622)
It was more than 0 kg / hr and the color was transparent, and a very good product was obtained. (Example 2) Low-concentration starch syrup of DE20 was concentrated and dried by the same apparatus as in Example 1. Operating conditions Vapor pressure 7 kg / cm 2 G (169.6 ° C) Vacuum degree 20 Torr or less Evaporation chamber outlet temperature 135 ° C Result Stock solution composition 18% (water content) Stock solution amount of 28.5kg / hr Was obtained. Product composition 1-3% (water content) Product amount 24 kg / hr Evaporation amount 4.5 kg / hr Although powdering was not possible with conventional equipment, a white, porous (granion-like) powder product with good solubility was obtained. It was (Example 3) Hard candy raw material carried out in the same apparatus as in Example 1 Water was dissolved and dissolved at a compounding ratio of sugar 80% starch syrup 20%, water content was adjusted to 25%, and the operation was carried out under the following operating conditions. Steam pressure 9 kg / cm 2 G (179 ° C.) Evaporation chamber pressure Normal pressure (atmosphere) Evaporation chamber product outlet temperature 160 ° C. to 165 ° C. Result 1. A stock solution amount of 150 kg / hr was processed to obtain the following product. Product composition 1.5 to 2% (water content) Product amount 150 kg / hr Evaporation amount 37 kg / hr Compared with the coil type concentrator of the conventional method (Patent No. 187622), less coloring, better transparency, and increased capacity A very good product was obtained.
【００１３】[0013]
【発明の効果】本発明は上記の構成とその操作により、
従来の加熱濃縮機に比較して、下記の機能と効果を有す
る。 （イ）加熱滞留時間が３−１０Ｓｅｃと非常に小さいの
で、比較的高温度の加熱でも、加熱濃縮物の変性及び分
子量の変化がない。従って、熱変性、高粘度液、発泡
性、液の濃縮乾燥が可能となった。又熱に弱い物質の濃
縮乾燥が可能となった。 （ロ）環状原液上昇管を両面加熱するので、従来装置の
１／２の大きさで足り、且つ簡単な構造であるので装置
の価額の低廉と、且つ効率の高い優れた濃縮機が得られ
る。 （ハ）原料上昇管の下端基部に逆漏斗状の原液分配供給
ボックスを有するので、原液は供給口より、まずこの分
配供給ボックスに集まり、次いで順次上部の細い上昇管
に移送されその間に加熱、ベーパーライズされ、被加熱
原料の粘性の影響も加わり、発生ペーパー撹拌効果が働
き、超高速流となり、熱移動せしめ、連続的に加熱、加
圧され、上部において合体結合されるので、原料の均一
性と濃縮効果は増加し、これを直ちに蒸発室に移送する
ので、ここで濃縮、乾燥が増進し、高濃度濃縮液及び乾
燥粉末化が可能となった。 （ニ）装置中の製品のホールド（残量）がきわめて少な
い効果を有する。The present invention has the following features and operations.
Compared with the conventional heating concentrator, it has the following functions and effects. (A) Since the heating residence time is as very short as 3-10 Sec, there is no denaturation of the heated concentrate and no change in the molecular weight even when heated at a relatively high temperature. Therefore, heat denaturation, high-viscosity liquid, foamability, and concentration / drying of the liquid became possible. In addition, it became possible to concentrate and dry heat-sensitive substances. (B) Since the annular stock solution ascending pipe is heated on both sides, 1/2 the size of the conventional device is sufficient, and the structure is simple, so the device price is low and an excellent concentrator with high efficiency can be obtained. .. (C) Since there is a reverse funnel-shaped undiluted solution distribution supply box at the lower end base of the raw material rising pipe, the undiluted solution is first collected in this distribution supply box from the supply port, and then sequentially transferred to the thin rising pipe at the upper part and heated during It is vaporized, and the effect of the viscosity of the raw material to be heated is added, the generated paper stirring effect works, it becomes an ultra-high speed flow, heat is transferred, it is continuously heated and pressurized, and it is united and joined at the top, so the raw material is uniform. Since the property and the concentration effect are increased and they are immediately transferred to the evaporation chamber, the concentration and the drying are promoted there, and the high-concentration concentrate and the dry powder can be obtained. (D) The hold (remaining amount) of the product in the device is extremely small.
【図１】本発明の一実施例であって、その縦断側面図。FIG. 1 is a longitudinal side view showing an embodiment of the present invention.
【図２】上記の要部（連続熱交換器）の×〜×線の横断
面図。FIG. 2 is a transverse cross-sectional view of the main part (continuous heat exchanger) along line X-X.
【図３】本発明の最終工程の常圧又は加圧乾燥室の説明
図。FIG. 3 is an explanatory diagram of a normal pressure or pressure drying chamber in the final step of the present invention.
【図４】本発明の最終工程の加圧乾燥室の説明図。FIG. 4 is an explanatory view of a pressure drying chamber in the final step of the present invention.
１ スチームジャケット ２ スチームコアー ３ スチーム導入管 ４ スチーム入口（スチームジャケットへの） ５ ドレーン出口（スチームジャケットへの） ６ スチーム入口（スチーム導入管への） ７ ドレーン出口（スチーム導入管への） ８ 原液入口 ９ 原液分配供給ボックス １０ 原料上昇管 １１ 原料上昇管の合体部 １２ 原料排出管 １３ 蒸発室 １４ 蒸発室出口 １５ コンデンサー １６ 真空ポンプ １７ ドレーンタンク １８ 排気管 １９ ブロワー ２０ 排気孔 1 steam jacket 2 steam core 3 steam inlet pipe 4 steam inlet (to steam jacket) 5 drain outlet (to steam jacket) 6 steam inlet (to steam inlet pipe) 7 drain outlet (to steam inlet pipe) 8 stock solution Inlet 9 Undiluted solution distribution supply box 10 Raw material riser pipe 11 Combined raw material riser pipe 12 Raw material discharge pipe 13 Evaporation chamber 14 Evaporation chamber outlet 15 Condenser 16 Vacuum pump 17 Drain tank 18 Exhaust pipe 19 Blower 20 Exhaust hole
Claims (1)
チームジャケットで包囲された原料上昇管の下方を漏斗
状に拡大した原料分配供給ボックスとし、上方において
合体せしめ、その先方に常圧もしくは減圧或いは加圧蒸
発室に通じる排出管に連結したことを特徴とする加熱濃
縮機における連続熱交換器。Claim: What is claimed is: 1. A steam introducing pipe is provided in the center, and a lower part of a raw material rising pipe surrounded by a steam jacket is a funnel-shaped enlarged raw material distribution and supply box, and the raw material distribution and supply box is integrated at the upper side. A continuous heat exchanger in a heating concentrator, characterized in that it is connected to a discharge pipe leading to a normal pressure or reduced pressure or a pressure evaporation chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21312891A JPH0531301A (en) | 1991-07-31 | 1991-07-31 | Continuous heat exchanger in heating concentrator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21312891A JPH0531301A (en) | 1991-07-31 | 1991-07-31 | Continuous heat exchanger in heating concentrator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0531301A true JPH0531301A (en) | 1993-02-09 |
Family
ID=16634044
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21312891A Pending JPH0531301A (en) | 1991-07-31 | 1991-07-31 | Continuous heat exchanger in heating concentrator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0531301A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7218833B2 (en) | 2004-03-08 | 2007-05-15 | Nec Corporation | Wireless communication system and apparatus |
| CN103372324A (en) * | 2012-04-24 | 2013-10-30 | 都江堰市春盛中药饮片有限公司 | Vacuum decompression concentration system |
| CN108905243A (en) * | 2018-07-27 | 2018-11-30 | 浙江杭康检测技术有限公司 | A kind of herbal function constituents extraction inspissator and its application method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0243521A (en) * | 1988-08-03 | 1990-02-14 | Hitachi Ltd | Organic nonlinear optical element |
-
1991
- 1991-07-31 JP JP21312891A patent/JPH0531301A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0243521A (en) * | 1988-08-03 | 1990-02-14 | Hitachi Ltd | Organic nonlinear optical element |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7218833B2 (en) | 2004-03-08 | 2007-05-15 | Nec Corporation | Wireless communication system and apparatus |
| CN103372324A (en) * | 2012-04-24 | 2013-10-30 | 都江堰市春盛中药饮片有限公司 | Vacuum decompression concentration system |
| CN108905243A (en) * | 2018-07-27 | 2018-11-30 | 浙江杭康检测技术有限公司 | A kind of herbal function constituents extraction inspissator and its application method |
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