JP2016148459A - Solution transfer cooling device and manufacturing method - Google Patents
Solution transfer cooling device and manufacturing method Download PDFInfo
- Publication number
- JP2016148459A JP2016148459A JP2015016275A JP2015016275A JP2016148459A JP 2016148459 A JP2016148459 A JP 2016148459A JP 2015016275 A JP2015016275 A JP 2015016275A JP 2015016275 A JP2015016275 A JP 2015016275A JP 2016148459 A JP2016148459 A JP 2016148459A
- Authority
- JP
- Japan
- Prior art keywords
- heat exchange
- cooling device
- exchange tube
- solution
- transfer cooling
- 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
本発明は、溶液移送冷却装置及びその製造方法に関する。さらに詳しくは、本発明は、以下に説明する重合体ファウリング等の発生を抑え、前記重合体反応を長期間にわたって効率的に継続させることができる溶液移送冷却装置及びその製造方法に関する。 The present invention relates to a solution transfer cooling device and a manufacturing method thereof. More specifically, the present invention relates to a solution transfer cooling device that can suppress the occurrence of polymer fouling and the like described below and can efficiently continue the polymer reaction over a long period of time, and a manufacturing method thereof.
ポリエチレン、ポリプロピレン等の重合体製品を製造する際、例えばノルマルヘキサン等の溶媒の中で触媒とエチレンとを反応させてポリエチレンをつくる重合体反応器の内壁へ、重合体が付着する。また、重合体反応器からペレット化等の後処理装置において、溶剤と重合生成物混合溶液を冷却しながら移送するための移送手段の内壁へ、重合体が析出付着する、いわゆる重合体ファウリングが発生する。 When polymer products such as polyethylene and polypropylene are produced, the polymer adheres to the inner wall of a polymer reactor in which polyethylene is produced by reacting a catalyst with ethylene in a solvent such as normal hexane. Further, in a post-treatment device such as pelletization from a polymer reactor, so-called polymer fouling, in which the polymer deposits and adheres to the inner wall of the transfer means for transferring the solvent and the polymerization product mixed solution while cooling, Occur.
ポリエチレン等の重合ではまた、重合体反応器内での重合反応によって反応熱が発生するという問題もある。この反応熱を効率的に除去するすなわち冷却しないと、運転条件のコントロールができず、重合反応物の物性が著しく変化し、重合体反応器の運転停止を余儀なくされる場合もある。 Polymerization of polyethylene or the like also has a problem that heat of reaction is generated by the polymerization reaction in the polymer reactor. If this heat of reaction is not efficiently removed, that is, if it is not cooled, the operating conditions cannot be controlled, the physical properties of the polymerization reaction product change significantly, and the operation of the polymer reactor may be forced to stop.
一方、反応熱を除去するために、重合体反応器の内壁及び重合体反応器からペレット化等の後処理装置に冷却しながら移送するための移送手段に、シェルアンドチューブ熱交換器を設定する場合がある。この場合、冷却剤と溶媒中に含まれる重合体とを離隔する金属管内壁に重合体ファウリングが形成される。
この重合体ファウリングは、熱伝導率が金属管に比し約二桁低いことから、重合体ファウリングが、前記反応熱の除去の除去すなわち冷却を著しく低下させる。同時に、実質的管径が細くなることにより、輸送ポンプの負荷が増加し、輸送ポンプの損傷や、流量低減による生産効率の低下という弊害が発生する。
On the other hand, in order to remove the reaction heat, a shell and tube heat exchanger is set in the inner wall of the polymer reactor and a transfer means for transferring the polymer reactor while cooling from the polymer reactor to a post-treatment device such as pelletizing. There is a case. In this case, a polymer fouling is formed on the inner wall of the metal tube that separates the coolant and the polymer contained in the solvent.
Since this polymer fouling has a thermal conductivity that is about two orders of magnitude lower than that of the metal tube, the polymer fouling significantly reduces the removal or cooling of the reaction heat. At the same time, since the substantial pipe diameter is reduced, the load on the transport pump is increased, and there is an adverse effect that the transport pump is damaged or the production efficiency is reduced due to the reduced flow rate.
この重合体ファウリングの発生増大を防止するために、
（１）反応器内及び移送管内の流速を上げること
（２）反応器内及び移送管内表面の凹凸をできるだけ小さくすること
（３）重合体ファウリングの起点が触媒及び重合体粒子の静電付着であるという説に基づく静電除去剤を添加すること
（４）エチレンフィードノズルの構造を改良すること
（５）フランジのギャップ等にポリマーが対流しないような構造を改良すること
が提案されている（例えば、非特許文献１参照）。
In order to prevent an increase in the occurrence of this polymer fouling,
(1) Increasing the flow velocity in the reactor and transfer pipe (2) Minimizing irregularities on the reactor and transfer pipe surface as much as possible (3) Starting point of polymer fouling is the electrostatic adhesion of catalyst and polymer particles (4) Improvement of the structure of the ethylene feed nozzle (5) Improvement of the structure that prevents the polymer from convection in the gap of the flange, etc. (For example, refer nonpatent literature 1).
従来技術の重合体ファウリング防止方法として、特定の一般式で表される平均分子量が、３００００以下のポリオキシレン系重合体を含むファウリング防止剤を、重合装置内又は後行程の溶剤重合物溶液内成分に添加することが提案されている（例えば、特許文献１参照）。 As a conventional polymer fouling prevention method, an antifouling agent containing a polyoxylene polymer having an average molecular weight represented by a specific general formula of 30000 or less is used as a solvent polymer solution in a polymerization apparatus or in a subsequent process. It has been proposed to add to internal components (see, for example, Patent Document 1).
他の従来技術の重合体ファウリング防止方法、すなわち重合反応器への触媒スラリー供給系の閉塞を防止し、連続運転を可能とするオレフィン重合方法として、オレフィン重合方法であって、固体に担持した予備重合触媒を含む触媒スラリーを、オレフィンの本重合を行う気相反応器に供給するに際して、該予備重合触媒１ｇに対して、０．３〜３．０ｍｇの有機アルミニウム化合物を同伴させることが提案されている（例えば、特許文献２参照）。 Another prior art polymer fouling prevention method, that is, an olefin polymerization method that prevents clogging of the catalyst slurry supply system to the polymerization reactor and enables continuous operation, is an olefin polymerization method, and is supported on a solid. When supplying a catalyst slurry containing a prepolymerization catalyst to a gas phase reactor for main polymerization of olefin, it is proposed that 0.3 g to 3.0 mg of an organoaluminum compound is accompanied with 1 g of the prepolymerization catalyst. (For example, refer to Patent Document 2).
他の従来技術の重合体ファウリング防止方法として、高温のプロセスストリームに曝される金属チューブ熱交換装置に腐蝕および腐蝕に誘導されるファウリングに対する抵抗性を賦与するために、内側表面および外側表面を有するプロセスストリームを加熱又は冷却するための伝熱装置１０であって、前記伝熱装置１０は、Ｘ、ＹおよびＺを含むスチール合金で形成されるチューブであり、前記チューブは、４０マイクロインチ（１．１μｍ）未満の算術平均表面粗さを有するスチール合金からなる基材層、内側表面および外側表面の少なくとも一方の上に形成された１０〜４０重量％のクロムを含有するクロム富化酸化物層、硫化物、酸化物、酸硫化物またはそれらの混合物を含む前記クロム富化酸化物層、の３層を含む伝熱装置１０等の表面上に形成された表面保護層を設けることが提案されている（例えば、特許文献３参照）。 As another prior art polymer fouling prevention method, the inner surface and outer surface are used to impart resistance to corrosion and corrosion-induced fouling to metal tube heat exchangers exposed to high temperature process streams. A heat transfer device 10 for heating or cooling a process stream comprising: a heat transfer device 10 formed of a steel alloy containing X, Y and Z, wherein the tube is 40 microinches. Chromium-enriched oxidation containing 10-40% by weight chromium formed on at least one of a substrate layer, an inner surface and an outer surface comprising a steel alloy having an arithmetic average surface roughness of less than (1.1 μm) A heat transfer device 10 including three layers of a material layer, the chromium-enriched oxide layer including a sulfide, an oxide, an oxysulfide, or a mixture thereof. It has a surface protective layer formed on the surface has been proposed (e.g., see Patent Document 3).
上述した技術によっても重合体ファウリングの発生は、産業上の要求を満たす程度に有効に防止も減少もさせることができないため、さらに他の方法、技術が提案されている。すなわち、金属配管の内壁に、薬液又は所要のガスにより除去され得る薄膜を被着形成することが提案されている（例えば、特許文献４参照）。 Even with the techniques described above, the occurrence of polymer fouling cannot be effectively prevented or reduced to an extent that satisfies industrial requirements, and therefore other methods and techniques have been proposed. That is, it has been proposed to deposit and form a thin film that can be removed by a chemical solution or a required gas on the inner wall of a metal pipe (see, for example, Patent Document 4).
他の重合体ファウリング発生防止技術として、内壁に樹脂皮膜を形成させた容器を用いて化学的操作又は物理的操作を行い、該操作の工程中に容器内壁に生成したスケールを前記樹脂皮膜と共に除去するスケール除去方法が提案されている（例えば、特許文献５参照）。 As another polymer fouling prevention technique, chemical operation or physical operation is performed using a container having a resin film formed on the inner wall, and the scale formed on the inner wall of the container during the operation process is combined with the resin film. A scale removal method for removal has been proposed (see, for example, Patent Document 5).
さらに他の重合体ファウリング発生防止技術として、液体又はペースト状の流動物を送液する配管内に配設するチューブにおいて、チューブを配管内に貫通して載置し、一方の端辺を封鎖した該チューブの他端から該チューブ内に送気して該チューブを膨らませて管路内に密着させた後に該チューブ、両端をチューブの内側から配管の端部に密着固定する配管用インナーチューブの設置方法が提案されている（例えば、特許文献６参照）。 Furthermore, as another polymer fouling prevention technique, in a tube disposed in a pipe for feeding a liquid or paste-like fluid, the tube is placed through the pipe and one end is sealed. An inner tube for piping that is fed into the tube from the other end of the tube and inflates the tube so that the tube is brought into close contact with the inside of the pipe, and both ends of the tube are firmly fixed from the inside of the tube to the end of the pipe. An installation method has been proposed (see, for example, Patent Document 6).
重合体ファウリングは、非特許文献１に示されるように、物理的には高速で通過させること、接触面での保護層の形成、滞留発生阻止、化学的には静電気防止剤を添加すること等のよって解消できるように考えられている。
しかし、現実的には、前記特許の重合体ファウリング対策のいずれも不完全で、重合体ファウリングの発生による冷却効率の低下や、重合体ファウリングによる流路の狭隘化すなわち流量の減少が、産業界の大きな障害となったままである。
As shown in Non-Patent Document 1, the polymer fouling is physically passed at a high speed, the protective layer is formed on the contact surface, the retention is prevented, and the antistatic agent is chemically added. It is thought that it can be solved by.
However, in reality, none of the polymer fouling countermeasures of the above-mentioned patent is incomplete, resulting in a decrease in cooling efficiency due to the occurrence of polymer fouling, or a narrowing of the flow path due to polymer fouling, that is, a decrease in flow rate. It remains a major obstacle for industry.
一方、特許文献４及び５によって提案された技術は、既に内壁に形成された薄膜や樹脂皮膜が運転条件変更等により溶解したり剥離したりして、新しく生成した重合体中に混入する恐れが極めて高く、品質管理上受け入れられない問題を含んでいる。 On the other hand, in the techniques proposed by Patent Documents 4 and 5, the thin film or resin film already formed on the inner wall may be dissolved or peeled off due to a change in operating conditions or the like, and may be mixed into the newly formed polymer. It is extremely expensive and contains unacceptable problems in quality control.
特許文献６によって提案された技術は、柔軟で巻き状態で保管されたインナーチューブは、円柱筒を束ねた移送装置の各円柱筒、例えば、約１０メートルのものの全長に装着することが極めて困難であり、工業上の実施が実質上不可能であると判断される。 The technique proposed by Patent Document 6 is that it is extremely difficult to attach the inner tube stored in a flexible and wound state to the entire length of each cylindrical cylinder of the transfer device in which the cylindrical cylinders are bundled, for example, about 10 meters. It is judged that industrial implementation is practically impossible.
本発明者が確認した重合体ファーリングが発生する実際の例として、重合体移送冷却装置は、直径１７０センチメートルの円形断面に、外直径２５．4ミリメートル、肉厚1．2ミリメートル、長さ１０メートルのＳＵＳ３０４製円筒管の約１５００本を均等ピッチで固定して円柱管束を形成している。
この円柱管束は、全体を耐圧シェル内に取付け、シェル内下部入口から冷媒を圧入することによって、冷媒が円柱管束の間に流入する。冷媒は、各円筒管の周囲を流れて各円筒管内の溶媒と重合物の混合溶液を冷却する。
As a practical example of the occurrence of the polymer furling confirmed by the present inventor, the polymer transfer cooling device has a circular cross section with a diameter of 170 centimeters, an outer diameter of 25.4 millimeters, a wall thickness of 1.2 millimeters, and a length. A cylindrical tube bundle is formed by fixing approximately 1500 SUS304 cylindrical tubes of 10 meters at an equal pitch.
The entire cylindrical tube bundle is mounted in a pressure-resistant shell, and the refrigerant flows in between the cylindrical tube bundles by press-fitting the refrigerant from the lower inlet in the shell. The refrigerant flows around each cylindrical tube to cool the mixed solution of the solvent and the polymer in each cylindrical tube.
冷却されることによって過飽和状態となった重合体は、溶媒から析出分離し、一部は管壁に付着成長し、ファウリングを形成する。その結果、液体固体の混合液は、流路が細った円筒管内を流動するようになり、定圧ポンプの流量が低下し、定常運転ができなくなってしまう。 The polymer that becomes supersaturated by cooling precipitates and separates from the solvent, and part of the polymer adheres to the tube wall and grows to form fouling. As a result, the liquid-solid mixed solution flows in a cylindrical tube with a narrow flow path, the flow rate of the constant pressure pump is reduced, and steady operation cannot be performed.
すなわち、前述した重合体溶液移送冷却装置は、通常２４時間連続運転される。その場合、約６ヶ月〜１年経過後には、円柱管内壁に析出堆積した重合体ファウリングが累乗的に増加し、重合体生成物溶液の流動を著しく妨げるようになる。その結果、定圧ポンプの吐出量が低下し、定常な運転条件が確保できなくなり、冷却装置の作動を停止して重合体ファウリングの除去をしなければならない。 That is, the polymer solution transfer cooling device described above is normally operated continuously for 24 hours. In that case, after about 6 months to 1 year, the polymer fouling deposited and deposited on the inner wall of the cylindrical tube increases progressively, and the flow of the polymer product solution is significantly hindered. As a result, the discharge amount of the constant pressure pump is reduced, and steady operating conditions cannot be ensured, and the operation of the cooling device must be stopped to remove the polymer fouling.
このような従来技術では避けることができない重合体移送装置の重合体ファーリングの除去作業は、産業上ほとんどの場合、高圧水洗浄で行なわれている。
高圧水洗浄は、往復動ポンプにより加圧した高圧水をノズルから噴射させ、噴射衝撃エネルギーにより堆積した重合体ファーリングを管壁から剥離し、粉砕し、排出・除去する。
In most cases in the industry, the removal work of the polymer furling of the polymer transfer device, which cannot be avoided by the prior art, is performed by high-pressure water washing.
In high-pressure water washing, high-pressure water pressurized by a reciprocating pump is jetted from a nozzle, and the polymer furling deposited by jet impact energy is peeled off from the tube wall, pulverized, discharged and removed.
該高圧の値は、例えば高圧７ＭＰａ以上３０ＭＰa、超高圧３０ＭＰa以上１００ＭＰa、超超高圧１００ＭＰa以上の２５０ＭＰaでも行われている。公益社団法人日本洗浄技術技能開発協会発行の「産業洗浄（高圧洗浄作業）安全衛生管理指針」によれば、高圧水洗浄は、特定の検定を受けた作業者が行い、監視者を置き、頑丈な足場を作らなければならない。 The value of the high pressure is, for example, also measured at a high pressure of 7 MPa to 30 MPa, an ultra high pressure of 30 MPa to 100 MPa, and an ultra ultra high pressure of 100 MPa to 250 MPa. According to the “Industrial Cleaning (High Pressure Cleaning Work) Safety and Health Management Guidelines” published by the Japan Cleaning Technology Skills Development Association, high pressure water cleaning is performed by a worker who has received a specific certification, and a supervisor is assigned to make it sturdy. Must make a good scaffold.
一つの重合体移送冷却装置の洗浄には、足場設置等から検査終了までに二週間以上を要する場合がある。その上、高圧水洗浄を行っている間は、重合体製造を停止しなければならないのであるから、不稼働損を生じ、産業活動上きわめて影響の大きな障害である。 In some cases, it takes two weeks or more for the cleaning of one polymer transfer cooling device from the installation of the scaffold to the end of the inspection. In addition, while the high-pressure water washing is being performed, the polymer production must be stopped, resulting in a loss of non-operation, which is a significant obstacle to industrial activities.
この重合体移送冷却装置は圧力容器であり、規則すなわち安全基準により定期点検が義務付けられている。 This polymer transfer cooling device is a pressure vessel and is required to be regularly inspected according to regulations, that is, safety standards.
（発明の目的）
本発明は、従来技術のいずれによっても解決されていない重合体製造ライン等における溶液移送冷却装置の上述した問題点に鑑みてなされたものであって、溶液移送冷却装置内の固形分の堆積を大幅に遅らせることができる溶液移送冷却装置を提供することを目的とする。
(Object of invention)
The present invention has been made in view of the above-mentioned problems of the solution transfer cooling device in a polymer production line or the like that has not been solved by any of the prior art, and is intended to deposit solids in the solution transfer cooling device. It is an object of the present invention to provide a solution transfer cooling device that can be greatly delayed.
本発明はさらに、溶液移送冷却装置内に固形分が堆積した場合にも、従来技術に比較して極めて簡易な作業設備によって、少数の現場作業者によって短時間に、しかも高圧水洗浄等の危険作業を行うことなく、ファウリング堆積物を除去することができる溶液移送冷却装置を提供することを目的とする。 In addition, the present invention also provides a simpler work facility as compared with the prior art even when solids are accumulated in the solution transfer cooling device, and can be used by a small number of on-site workers in a short time and with high-pressure water washing and other dangers. An object of the present invention is to provide a solution transfer cooling device capable of removing fouling deposits without performing work.
本発明はまた、生成された液体固体混合物等の溶液に望ましくない重合物等の管付着物が混入する恐れの少ない溶液移送冷却装置を提供することを目的とする。 It is another object of the present invention to provide a solution transfer cooling apparatus that is less likely to cause undesirable tube deposits such as polymerized substances to be mixed into a solution such as a produced liquid solid mixture.
本発明はさらに、従来技術の高圧水洗浄によって発生する産業廃棄物の排出量に比較して極めて少ない産業廃棄物の排出量である溶液移送冷却装置を提供することを目的とする。 It is another object of the present invention to provide a solution transfer cooling device that has a very small amount of industrial waste discharged compared to the amount of industrial waste generated by high-pressure water washing according to the prior art.
本発明は、
冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置した溶液移送冷却装置において、
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する分離金属板材が、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする溶液移送冷却装置である。
The present invention
In the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
In the heat exchange tube, a separation metal plate that divides the cross section of the heat exchange tube into at least two equal parts is continuously spiraled along the entire length of the central axis of the heat exchange tube. The solution transfer cooling device.
本発明はまた、冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置した溶液移送冷却装置において、
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を配置し、該金属分離板状部材が、長手方向に延びた中心領域の引っ張り抵抗より長手方向へ延びた両縁領域の引っ張り抵抗が大きい板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする溶液移送冷却装置である。
The present invention also provides a solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell.
A metal separation plate member that divides the cross section of the heat exchange tube into at least two equal parts is disposed inside the heat exchange tube, and the metal separation plate member is longer in the longitudinal direction than the tensile resistance of the central region extending in the longitudinal direction. A plate-like member having a large tensile resistance in both edge regions extending in the direction is formed in a spiral shape continuously along the entire length of the central axis of the heat exchange tube.
本発明はまた、重合反応装置と、該重合反応装置の重合生成物出口部に連結されて熱交換機能を有する冷却流路部とを有する重合体製造装置であって、
前記冷却流路部は、冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置し、前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする重合体製造装置である。
The present invention is also a polymer production apparatus comprising a polymerization reaction apparatus and a cooling flow path section connected to the polymerization product outlet section of the polymerization reaction apparatus and having a heat exchange function,
The cooling channel section has a plurality of heat exchange tubes arranged in parallel with each other in the refrigerant shell, and a metal separation plate-like member that divides the cross section of the heat exchange tube into at least two equal parts in the heat exchange tube Is a polymer production device characterized in that it is continuously spiraled along the entire length of the central axis of the heat exchange tube.
本発明はまた、
冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置した溶液移送冷却装置の製造方法において、
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する分離金属板材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成することを特徴とする溶液移送冷却装置である。
The present invention also provides
In the manufacturing method of the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
A solution in which a separation metal plate that divides the cross section of the heat exchange tube into at least two equal parts is continuously formed spirally along the entire length of the central axis of the heat exchange tube inside the heat exchange tube. It is a transfer cooling device.
冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置した溶液移送冷却装置の製造方法において、
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を配置し、該金属分離板状部材が、長手方向に延びた中心領域の引っ張り抵抗より長手方向へ延びた両縁領域の引っ張り抵抗が大きい板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成することを特徴とする溶液移送冷却装置の製造方法である。
In the manufacturing method of the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
A metal separation plate member that divides the cross section of the heat exchange tube into at least two equal parts is disposed inside the heat exchange tube, and the metal separation plate member is longer in the longitudinal direction than the tensile resistance of the central region extending in the longitudinal direction. In the manufacturing method of the solution transfer cooling device, the plate-like member having a large tensile resistance in both edge regions extending in the direction of a spiral is continuously formed along the entire length of the central axis of the heat exchange tube.
本発明の液体移送冷却装置及びその製造方法によれば、液体移送装置内のポリマー等などの固形分の堆積を、従来技術に比較して極めて簡易な作業設備によって、少数作業者によって短時間に且つ安全に除去することができるという効果を得ることができる。 According to the liquid transfer cooling device and the method of manufacturing the same of the present invention, solids such as polymers in the liquid transfer device can be deposited in a short time by a small number of workers by a very simple work facility compared to the prior art. And the effect that it can remove safely can be acquired.
本発明の溶液移送冷却装置によればまた、新しく生成されたポリマー溶液等の被移送冷却流体に、管内面に付着した既存ポリマー等の望ましくない不純物が混入する恐れがないという効果を得ることができる。 According to the solution transfer cooling apparatus of the present invention, it is also possible to obtain an effect that there is no possibility that undesirable impurities such as existing polymer adhering to the inner surface of the pipe are not mixed in the transferred cooling fluid such as a newly generated polymer solution. it can.
本発明の液体移送装置及びその製造方法によればさらに、従来の高圧水洗浄技術に比較して産業廃棄物の排出が極めて少ないという効果を得ることができる。 Further, according to the liquid transfer device and the manufacturing method thereof of the present invention, it is possible to obtain an effect that the discharge of industrial waste is extremely small as compared with the conventional high-pressure water washing technique.
本発明の液体移送装置及びその製造方法を好適に実施できるものとして、重合体の製造における重合反応、架橋反応等の化学的操作、脱溶剤、混合等の物理的操作の工程中の溶液移送が挙げられる。また、塗料、接着剤等の重合体を主成分とする組成物の製造等における重合体と他の成分の混合、脱溶剤等の物理的操作の工程中の溶液移送等にも適用できる。
本発明は、例えば、ポリ（メタ）アクリル酸メチル、ポリ（メタ）アクリル酸エチル、ポリ（メタ）アクリル酸ブチル等の（メタ）アクリル酸エステル系重合体、ウレタン系重合体、塩化ビニル系重合体、塩化ビニリデン系重合体、ＳＢＲ、酢酸ビニル系重合体等の重合体、或いはこれらを構成する単量体の共重合体の製造時の溶液移送に適用され、ウレタンエマルジョン、アクリルエマルジョン等のマルジョンにおける溶液移送にも好ましく適用できるものである。
The liquid transfer device of the present invention and the production method thereof can be suitably implemented as a solution transfer during a chemical operation such as a polymerization reaction or a crosslinking reaction in the production of a polymer, a physical operation such as solvent removal or mixing. Can be mentioned. Further, the present invention can also be applied to solution transfer during physical operation processes such as mixing of a polymer and other components in the production of a composition mainly composed of a polymer such as paint and adhesive, and other solvents.
The present invention includes, for example, poly (meth) acrylates, poly (meth) ethyl acrylate, poly (meth) acrylate polymers such as poly (meth) acrylate, urethane polymers, vinyl chloride heavy polymers. Applied to solution transfer during the production of polymers such as polymers, vinylidene chloride polymers, SBR, vinyl acetate polymers, or copolymers of monomers constituting these, such as urethane emulsions and acrylic emulsions. It can be preferably applied to solution transfer in
（発明の実施態様）
本発明は、前記金属分離板状部材が、長手方向において波状であり横手方向において凹凸のない板部材を螺旋状に形成されていることを特徴とする。
(Embodiment of the Invention)
The present invention is characterized in that the metal separating plate-like member is formed in a spiral shape with a wave-like member in the longitudinal direction and no unevenness in the transverse direction.
本発明はまた、前記金属分離板状部材が、前記熱交換チューブの中心軸線方向に延びたる両縁領域に切り込みを入れていることを特徴とする。 The present invention is also characterized in that the metal separating plate-like member is cut into both edge regions extending in the central axis direction of the heat exchange tube.
本発明はまた、前記金属分離板部材が、メッシュシートであり、該メッシュシートは、長手方向に延びた中心領域の引っ張り抵抗より長手方向へ延びた両縁領域の引っ張り抵抗が大きくなるように編まれていることを特徴とする。 According to the present invention, the metal separation plate member is a mesh sheet, and the mesh sheet is knitted so that the tensile resistance of both edge regions extending in the longitudinal direction is larger than the tensile resistance of the central region extending in the longitudinal direction. It is characterized by being rare.
本発明はまた、前記金属分離板状部材が、少なくとも前記熱交換チューブの中心軸線方向に延びた両縁領域にディンプルを有することを特徴とする。 The present invention is also characterized in that the metal separating plate member has dimples at least at both edge regions extending in the direction of the central axis of the heat exchange tube.
本発明はまた、前記金属分離板状部材が、ステンレス鋼によって製造されていることを特徴とする。 The present invention is also characterized in that the metal separating plate member is made of stainless steel.
本発明はまた、前記金属分離板状部材が、アルミニュウム合金によって製造されていることを特徴とする。 The present invention is also characterized in that the metal separating plate member is made of an aluminum alloy.
本発明はまた、前記金属分離板状部材が、銅合金によって製造されていることを特徴とする。 The present invention is also characterized in that the metal separation plate member is made of a copper alloy.
本発明はまた、前記金属分離板状部材が、チタン合金によって製造されていることを特徴とする。 The present invention is also characterized in that the metal separation plate member is made of a titanium alloy.
本発明はまた、前記金属分離板状部材が、ニッケル合金によって製造されていることを特徴とする。 The present invention is also characterized in that the metal separation plate member is made of a nickel alloy.
本発明はまた、前記金属分離板状部材が，その端部を前記剛性溶液外筒にかしめられていることを特徴とする。 The present invention is also characterized in that the end portion of the metal separation plate member is caulked to the rigid solution outer cylinder.
本発明はさらに、前記溶液が、溶剤と重合生成物の混合溶液であることを特徴とする。 The present invention is further characterized in that the solution is a mixed solution of a solvent and a polymerization product.
（第１実施形態）
本発明の第１実施形態の溶液移送冷却装置を図に基づいて説明する。実施形態の説明における数値は、全て例示である。
(First embodiment)
A solution transfer cooling apparatus according to a first embodiment of the present invention will be described with reference to the drawings. All numerical values in the description of the embodiments are examples.
本発明の実施形態の溶液移送冷却装置１は、熱交換機能を有し、ポリエチレン中低圧重合法を実施する圧力容器に使用するシェルアンドチューブ型の装置である。シェルアンドチューブ型の熱交換器としては、固定管板式、遊動頭式、Ｕ字管式の３タイプが知られている。溶液移送冷却装置１は、遊動頭式であって、被熱交換流体の高温・高圧による長尺の熱交換チューブの伸縮を遊動頭蓋の移動によって吸収する。 The solution transfer cooling device 1 according to the embodiment of the present invention is a shell and tube type device having a heat exchange function and used for a pressure vessel for performing a low pressure polymerization method in polyethylene. Three types of shell-and-tube heat exchangers are known: a fixed tube plate type, a floating head type, and a U-shaped tube type. The solution transfer cooling device 1 is a floating head type, and absorbs the expansion and contraction of the long heat exchange tube due to the high temperature and high pressure of the heat exchange fluid by the movement of the floating skull.
溶液移送冷却装置１は、図１に示すように、胴体すなわち冷媒シェル１０内を熱交換チューブ支持板１２によって区切ることによって、被熱交換流体室すなわち溶液室１４と冷媒室１６を形成している。
被熱交換流体すなわち溶液Ｒを収容する溶液室１４は、冷媒シェル１０の端部をシェルカバー２０によって塞いで形成されている。冷媒シェル１０の溶液室１４のある部分において、下側に溶液入口２２が配置され、上側に溶液出口２４が形成されている。溶液室１４は、区切り板４０によって、下側の溶液室高温部１４ａと下側の溶液室低温部１４ｂとに分けられている。
溶液Ｒとして、ノルマヘキサンと重合体の溶液が例示される。
As shown in FIG. 1, the solution transfer cooling device 1 forms a heat exchange fluid chamber, that is, a solution chamber 14 and a refrigerant chamber 16 by dividing the body, that is, the inside of the refrigerant shell 10 by a heat exchange tube support plate 12. .
The solution chamber 14 that stores the heat exchange fluid, that is, the solution R, is formed by closing the end of the refrigerant shell 10 with the shell cover 20. In a portion of the refrigerant shell 10 where the solution chamber 14 is located, a solution inlet 22 is disposed on the lower side, and a solution outlet 24 is formed on the upper side. The solution chamber 14 is divided into a lower solution chamber high temperature portion 14 a and a lower solution chamber low temperature portion 14 b by a partition plate 40.
Examples of the solution R include a solution of normal hexane and a polymer.
冷却水等の冷媒Ｗを収容する冷媒室１６は、図１及び図２に示すように、シェル１０の端部を冷媒室蓋３０によって塞がれている。冷媒シェル１０の内部には、例えば約２０００本の熱交換チューブ１０２が互いに平行に配置されている。冷媒室１６内において、チューブシート１２の反対側には、遊動頭蓋３４が配置されている。冷媒室１６には、冷媒Ｗを攪拌するための邪魔板３６が配置されている。
熱交換チューブ１０２は、冷媒流通部分の長さは１０メートルであり、外径が２５．４ミリメートル、肉厚が２．０ミリメートルであり、内径が２１．４ミリメートルである。
As shown in FIGS. 1 and 2, the coolant chamber 16 that stores the coolant W such as cooling water is closed at the end of the shell 10 by a coolant chamber lid 30. For example, about 2000 heat exchange tubes 102 are arranged in parallel in the refrigerant shell 10. In the refrigerant chamber 16, an idle skull 34 is disposed on the opposite side of the tube sheet 12. A baffle plate 36 for agitating the refrigerant W is disposed in the refrigerant chamber 16.
The heat exchange tube 102 has a refrigerant circulation portion length of 10 meters, an outer diameter of 25.4 millimeters, a wall thickness of 2.0 millimeters, and an inner diameter of 21.4 millimeters.
熱交換チューブ１０２は、図３に示すように、冷媒シェル１０の両端部近傍の内部に固着された熱交換チューブ支持板１２に溶接１０６によって固着されている。 As shown in FIG. 3, the heat exchange tube 102 is fixed by welding 106 to the heat exchange tube support plate 12 fixed inside the vicinity of both ends of the refrigerant shell 10.
熱交換チューブ１０２のそれぞれの内部には、図３に示すように、螺旋部材２０２ｃが配置されている。螺旋部材２０２ｃの幅は、２１．３０ミリメートルである。螺旋部材２０２ｃの少なくとも一端部は、図３に示すように、熱交換チューブ１０２の端部に固着するためにかしめられている。 As shown in FIG. 3, a spiral member 202 c is disposed inside each of the heat exchange tubes 102. The width of the spiral member 202c is 21.30 millimeters. As shown in FIG. 3, at least one end of the spiral member 202 c is caulked to be fixed to the end of the heat exchange tube 102.
螺旋部材２０２ｃは、図４（ａ）に示すように、ＳＵＳ３００系等のステンレス鋼，アルミニュウム合金、銅合金、チタン合金、ニッケル合金等の平板状部材２０２ａによって製造される。 As shown in FIG. 4A, the spiral member 202c is manufactured by a flat plate member 202a made of stainless steel such as SUS300, aluminum alloy, copper alloy, titanium alloy, nickel alloy or the like.
平板状部材２０２ａは、図４（ｂ）に示すように、長手方向すなわち中心軸線Ｏ方向に延びた方向に、例えばサインカーブをなすような繰り返し凹凸を設ける波板加工を施されて、波板部材２０２ｂになる。 As shown in FIG. 4 (b), the flat plate member 202a is subjected to corrugated processing to provide, for example, repeated irregularities that form a sine curve in the longitudinal direction, that is, the direction extending in the central axis O direction. It becomes the member 202b.
波板部材２０２ｂは、図４（ｃ）に示すように、長手方向に延びる中心軸線Ｏを中心に捻って、螺旋状にして、螺旋部材２０２ｃにする。このとき、中心軸線Ｏ上の部分２０２ｍは、中心軸線Ｏ方向にはほとんど伸びず、他方中心軸線Ｏ方向に延びた両縁領域２０２ｎは伸びて、全体的に直線状に延びた螺旋状の螺旋部材２０２ｃになる。 As shown in FIG. 4C, the corrugated plate member 202b is twisted around the central axis O extending in the longitudinal direction to form a spiral member 202c. At this time, the portion 202m on the central axis O hardly extends in the direction of the central axis O, and both edge regions 202n extending in the direction of the central axis O extend to form a spiral spiral that extends linearly as a whole. It becomes the member 202c.
以下に、熱交換チューブ１０２の内部に、螺旋部材２０２ｃ、すなわち該熱交換チューブ１０２の断面を少なくとも２等分割する金属製の板状部材を、前記熱交換チューブ１０２の中心軸線Ｏ全長に沿って連続して螺旋状に形成したものを配置した場合における、溶液の攪拌状況及び冷却状況について演算によって説明する。 Hereinafter, the spiral member 202c, that is, a metal plate-like member that divides the cross section of the heat exchange tube 102 into at least two equal parts along the central axis O length of the heat exchange tube 102 is disposed inside the heat exchange tube 102. The state of stirring and cooling of the solution in the case where the spirally formed ones are arranged will be described by calculation.
熱交換チューブ１０２内に螺旋部材２０２ｃを配置したすなわち螺旋部材有りの場合と、螺旋部材無しすなわち螺旋部材２０２ｃを配置しない場合の熱交換チューブ内の剪断速度を演算する。演算の条件は、公知の熱交換器用チューブを使用し、該熱交換チューブの内径は２１．４ｍｍ、全長４００ｍｍ、被冷却溶液はｎ−ｈｅｘａｎ、入口温度７０℃、流速０．６ｍ／ｓ、冷却水温度１８℃、螺旋部材２０２ｃは厚さ１ｍｍのＳＵＳ３０４である。溶液Ｒは、熱交換チューブ１０２内に自由放出される。 The shear rate in the heat exchange tube is calculated when the spiral member 202c is disposed in the heat exchange tube 102, that is, when the spiral member is present, and when there is no spiral member, that is, when the spiral member 202c is not disposed. The calculation conditions are as follows: a known heat exchanger tube is used, the inner diameter of the heat exchange tube is 21.4 mm, the total length is 400 mm, the solution to be cooled is n-hexan, the inlet temperature is 70 ° C., the flow rate is 0.6 m / s, and the cooling is performed. The water temperature is 18 ° C., and the spiral member 202c is SUS304 having a thickness of 1 mm. The solution R is released freely into the heat exchange tube 102.
剪断速度の測定点は、図５に示す５個のポイント１ないし５である。測定点の位置座標（ｍｍ）は、表１に示される。
（表１）
ポイント Ｘ Ｙ Ｚ
ポイント１ １．１ ０ ３７．５
ポイント２ ２．６７５ ０ ３７．５
ポイント３ ５．３５ ０ ３７．５
ポイント４ ８．０２５ ０ ３７．５
ポイント５ １０．６ ０ ３７．５
Ｘは熱交換チューブ１０２の中心からの水平横方向の座標値を示し、Ｙは熱交換チューブ１０２の中心からの垂直縦方向の座標値を示し、Ｚは熱交換チューブ１０２内の溶液流れ方向の入口からの座標値を示す。
The measurement points of the shear rate are the five points 1 to 5 shown in FIG. Table 1 shows the position coordinates (mm) of the measurement points.
(Table 1)
Point X Y Z
Point 1 1.10 37.5
Point 2 2.675 0 37.5
Point 3 5.35 0 37.5
Point 4 8.025 0 37.5
Point 5 10.6 0 37.5
X represents the horizontal and horizontal coordinate values from the center of the heat exchange tube 102, Y represents the vertical and vertical coordinate values from the center of the heat exchange tube 102, and Z represents the solution flow direction in the heat exchange tube 102. Indicates the coordinate value from the entrance.
熱交換チューブ１０２に溶液を流し始めてから２０秒後の各ポイントの剪断速度（１／ｓｅｃ）は、表２に示され、そのグラフは図６に示される。
（表２）
ポイント 螺旋部材無し 螺旋部材有り
ポイント１ １０９ ０
ポイント２ ３６ ７
ポイント３ １９ １２
ポイント４ １０ １９
ポイント５ ２２８ １９３
The shear rate (1 / sec) at each point 20 seconds after starting to flow the solution through the heat exchange tube 102 is shown in Table 2, and the graph is shown in FIG.
(Table 2)
Point Without spiral member With spiral member Point 1 109 0
Point 2 36 7
Point 3 19 12
Point 4 10 19
Point 5 228 193
この場合の図６における螺旋部材有りのグラフと横軸の挟む面積（左下がり斜線で示す）は、螺旋部材なしのグラフと横軸の挟む面積（右下がり斜線で示す）の１．５３倍となる。 In this case, the area sandwiched between the graph with the spiral member in FIG. 6 and the horizontal axis (indicated by the diagonally slanted left line) is 1.53 times the area between the graph without the spiral member and the axis of horizontal axis (indicated by the diagonally downward slanted line) Become.
一方、螺旋部材の有無の剪断速度（１／ｓｅｃ）に与える影響をさらに詳細に比較するため、螺旋部材の厚さ１．０ｍｍを考慮して、螺旋部材の表面から０．１ｍｍ離れた位置（Ｘ＝０．６、Ｙ＝０、Ｚ＝３７．５）のポイントＰ を、図６のグラフから推定すると、図７に示すようになる。
図７において、螺旋部材有りのグラフと横軸の挟む面積（左下がり斜線で示す）は、螺旋部材無しのグラフと横軸の挟む面積（右下がり斜線で示す）の２．０倍となると推定される。この結果から、本発明の螺旋部材有りの構造は、従来の螺旋部材無しの構造に比較して、熱交換チューブ１０２内の溶液は、熱交換チューブ１０２内面近くの領域と螺旋部材表面近くの溶液が入れ替わる作用の発生により攪拌され、熱交換チューブ１０２内壁への溶液の堆積がより減少することが推定できる。
On the other hand, in order to compare the influence of the presence or absence of the spiral member on the shear rate (1 / sec) in more detail, taking into consideration the thickness of the spiral member of 1.0 mm, a position 0.1 mm away from the surface of the spiral member ( If the point P 1 of X = 0.6, Y = 0, Z = 37.5) is estimated from the graph of FIG. 6, it is as shown in FIG.
In FIG. 7, the area sandwiched between the graph with the spiral member and the horizontal axis (indicated by the slanting left slanted line) is estimated to be 2.0 times the area between the graph without the spiral member and the horizontal axis (indicated by the slanting right slanting line). Is done. From this result, in the structure with the spiral member of the present invention, the solution in the heat exchange tube 102 is in the region near the inner surface of the heat exchange tube 102 and the solution near the surface of the spiral member as compared with the structure without the conventional spiral member. It can be presumed that the accumulation of the solution on the inner wall of the heat exchange tube 102 is further reduced by the occurrence of the action of switching.
次に、溶液の冷却効果に演算する。溶液を交換チューブ１０２に流入開始してから２０秒後のＺ＝４０．０（ｍｍ）の断面の温度分布は、図８に示される。図８（ａ）は螺旋部材有りの場合を示し、図８（ｂ）は螺旋部材無しの場合を示す。図８（ａ）の螺旋部材は、１８℃であるとして演算した。 Next, it calculates to the cooling effect of a solution. FIG. 8 shows the temperature distribution of the cross section of Z = 40.0 (mm) 20 seconds after the solution starts flowing into the exchange tube 102. FIG. 8A shows a case with a spiral member, and FIG. 8B shows a case without a spiral member. The helical member in FIG. 8A was calculated as 18 ° C.
次に、溶液の冷却効果について、溶液の平均温度を比較する。冷媒の温度は、１８．０℃である。溶液の入口温度は、７０℃である。熱交換チューブ１０２の出口位置すなわちＺ＝４００ｍｍにおける溶液の平均温度は、表３に示す通りである。
（表３）
螺旋部材有り 螺旋部材無し
平均溶液温度 ６３．９℃ ６６．８℃
温度差 （２．９℃）
Next, the average temperature of a solution is compared about the cooling effect of a solution. The temperature of the refrigerant is 18.0 ° C. The inlet temperature of the solution is 70 ° C. Table 3 shows the average temperature of the solution at the outlet position of the heat exchange tube 102, that is, Z = 400 mm.
(Table 3)
With spiral member Without spiral member Average solution temperature 63.9 ° C 66.8 ° C
Temperature difference (2.9 ℃)
この結果から、本発明の螺旋部材有りの構造は、従来の螺旋部材無しの構造に比較して、熱交換チューブ１０２内の溶液がより効率的に冷却され、生産効率が高くなり、かつ熱交換チューブ１０２内壁への溶液の堆積がより減少することが推定できる。 From this result, the structure with the spiral member of the present invention cools the solution in the heat exchange tube 102 more efficiently, increases the production efficiency, and heat exchange compared to the structure without the conventional spiral member. It can be estimated that the deposition of the solution on the inner wall of the tube 102 is further reduced.
次に、螺旋部材による溶液圧力損失について演算する。熱交換チューブ１０２の入口から２４．５ｍｍの位置すなわちＺ＝２４．５ｍｍの第１位置と、熱交換チューブ１０２の入口から３７５ｍｍの位置すなわちＺ＝３７５ｍｍの第２位置の圧力は、表４に示す通りである。
（表４）
螺旋部材有り 螺旋部材無し
第１位置の圧力 １３５３０パスカル ３１３１パスカル
第２位置の圧力 １３３９９パスカル ３０６９パスカル
第１及び第２位置の圧力差 １３１パスカル ６２パスカル
Next, the solution pressure loss due to the spiral member is calculated. Table 4 shows the pressure at a position 24.5 mm from the inlet of the heat exchange tube 102, that is, a first position at Z = 24.5 mm, and at a position 375 mm from the inlet of the heat exchange tube 102, that is, a second position at Z = 375 mm. Street.
(Table 4)
With spiral member Without spiral member Pressure at first position 13530 Pascal 3131 Pascal Pressure at second position 13399 Pascal 3069 Pascal Pressure difference between first and second positions 131 Pascal 62 Pascal
この圧力差のエネルギーは、溶液攪乱すなわち溶液攪乱及び溶液冷却に作用していると推定される。従って、同一の溶液攪乱及び溶液冷却を実現するために、熱交換チューブ１０２の長さは、螺旋部材有りの場合は、螺旋部材無しの場合の６２／１３１すなわち約半分の長さにすることができ、設備投資を大きく抑制することができる。 The energy of this pressure difference is presumed to act on solution perturbation or solution perturbation and solution cooling. Therefore, in order to achieve the same solution disturbance and solution cooling, the length of the heat exchange tube 102 with the helical member can be 62/131 or about half that without the helical member. This can greatly reduce capital investment.
（変形例）
上述した波板部材２０２ｂは、図９に示すように、波板折り返し部分の折り返し曲率が、波板部材２０２ｂの波板折り返し部分の折り返し曲率よりも小さい、角張った形状の折り曲げ波板２０６に替えることもできる。
(Modification)
As shown in FIG. 9, the corrugated plate member 202b described above is replaced with a folded corrugated plate 206 having an angular shape in which the folded curvature of the corrugated plate folded portion is smaller than the folded curvature of the folded corrugated portion of the corrugated plate member 202b. You can also.
平板状部材２０２ａは、図１０に示すように、平板状部材２０２ａの中心軸線Ｏ方向に延びた両縁領域２１０に切り込み２１２を入れた切り込み平板状部材２１４に替えることもできる。 As shown in FIG. 10, the flat plate member 202a can be replaced with a cut flat plate member 214 in which cuts 212 are formed in both edge regions 210 extending in the direction of the central axis O of the flat plate member 202a.
平板状部材２０２ａは、また、図１１(ａ)に示すように、平板状部材２０２ａの全面にエンボス加工により複数のエンボス２２１を設けた第１エンボス平板状部材２２０、あるいは、図１１(ｂ)に示すように、少なくとも中心軸線Ｏの両側領域で中心軸線Ｏ方向に延びた両縁領域２２６にエンボス加工によって複数のスエンボス２１１を施した第２エンボス平板状部材２２２に替えることもできる。 As shown in FIG. 11A, the flat plate member 202a is a first embossed flat plate member 220 in which a plurality of embosses 221 are provided by embossing on the entire surface of the flat plate member 202a, or FIG. As shown in FIG. 6, the second embossed plate-like member 222 can be replaced with a plurality of embossed portions 211 by embossing at both edge regions 226 extending in the direction of the central axis O in both side regions of the central axis O.
これらの第１エンボス平板状部材２２０及び第２エンボス２２２において、中心軸線Ｏ上の部分２２４は、エンボス２１１が変形せず、中心軸線Ｏ方向にはほとんど伸びない。他方、中心軸線Ｏ方向に延びた両縁領域２２６は、エンボス２１１が変形して伸び、全体的に直線状に延びた螺旋状のエンボス螺旋部材になる。 In the first embossed flat plate member 220 and the second emboss 222, the portion 224 on the central axis O does not deform the emboss 211 and hardly extends in the direction of the central axis O. On the other hand, both edge regions 226 extending in the direction of the central axis O become a spiral embossed spiral member extending in a straight line as a whole by deforming and extending the emboss 211.
平板状部材２０２ａは、また、図１２に示すように、メッシュ平板状部材２３０に替えることもできる。メッシュ平板状部材２３０は、図１２(ａ)に示すように、平板状のメッシュ板を使用する。メッシュ平板状部材２３０は、図１２(ｂ)に示すように、長手方向すなわち中心軸線Ｏ方向に延びた方向に繰り返し凹凸を設ける波板加工を施されて、メッシュ波板部材２３２にする。 The flat plate member 202a can also be replaced with a mesh flat plate member 230 as shown in FIG. As the mesh flat plate member 230, a flat mesh plate is used as shown in FIG. As shown in FIG. 12 (b), the mesh flat plate member 230 is subjected to corrugated processing in which unevenness is repeatedly provided in the longitudinal direction, that is, the direction extending in the central axis O direction, so that the mesh corrugated plate member 232 is obtained.
メッシュ波板部材２３２は、長手方向に延びる中心軸線Ｏを中心に捻って、螺旋状にして、メッシュ螺旋板にする。このとき、中心軸線Ｏ上の部分２３４は、中心軸線Ｏ方向にはその部分の編み目が変わらずほとんど伸びず、他方中心軸線Ｏ方向に延びた両縁領域２３６の編み目が拡大して延び、直線状に延びた螺旋状になる。 The mesh corrugated plate member 232 is twisted about a central axis O extending in the longitudinal direction to be a spiral shape, thereby forming a mesh spiral plate. At this time, the portion 234 on the central axis O extends in the direction of the central axis O with little change in the stitches of the portion, while the stitches of both edge regions 236 extending in the direction of the central axis O extend and extend straight. It becomes a spiral extending in a shape.
（第２実施形態）
本発明の第２実施形態の溶液移送冷却装置を図に基づいて説明する。
第２実施形態の溶液移送冷却装置の熱交換チューブ３０２は、図１３に示すように、冷媒を流通させるための鉄製の剛性冷媒外筒３００の内部に、溶媒の中に生成物を含む混合溶液を流通させるためのＳＵＳ３０４製の剛性混合物外筒３０２を互いに平行に配置して構成される。
剛性冷媒外筒３０２の冷媒流通部分の長さは１０メートルであり、図１４に示すように、外径が２５．４ミリメートル、肉厚が２．０ミリメートルであり、内径が２１．４ミリメートルである。
(Second Embodiment)
A solution transfer cooling apparatus according to a second embodiment of the present invention will be described with reference to the drawings.
As shown in FIG. 13, the heat exchange tube 302 of the solution transfer cooling device of the second embodiment is a mixed solution containing a product in a solvent inside an iron rigid refrigerant outer cylinder 300 for circulating a refrigerant. The rigid mixture outer cylinders 302 made of SUS304 for distributing the gas are arranged in parallel to each other.
The length of the refrigerant circulation portion of the rigid refrigerant outer cylinder 302 is 10 meters, and as shown in FIG. 14, the outer diameter is 25.4 millimeters, the wall thickness is 2.0 millimeters, and the inner diameter is 21.4 millimeters. is there.
剛性溶液外筒３０２は、図１５に示すように、剛性溶液外筒３０２の両端部近傍の内部に固着された剛性溶液外筒支持板３０４に溶接３０６によって固着されている。 As shown in FIG. 15, the rigid solution outer cylinder 302 is fixed by welding 306 to a rigid solution outer cylinder support plate 304 fixed to the inside of both ends of the rigid solution outer cylinder 302.
剛性混合物外筒３０２のそれぞれの内部には、図１４及び図１５に示すように、薄肉内筒３１０が配置されている。薄肉内筒３１０は、内径が２１．３０ミリメートルであり、肉厚が０．０４ミリメートルである。薄肉内筒３１０の両端部は、図１５に示すように、かしめられて、剛性混合物外筒３０２の端部の上に固着される。 As shown in FIGS. 14 and 15, a thin inner cylinder 310 is disposed inside each of the rigid mixture outer cylinders 302. The thin inner cylinder 310 has an inner diameter of 21.30 millimeters and a wall thickness of 0.04 millimeters. As shown in FIG. 15, both ends of the thin inner cylinder 310 are caulked and fixed on the ends of the rigid mixture outer cylinder 302.
以下に、薄肉内筒３１０が、移送される溶液、例えば反応生成物と溶媒の混合液の温度及び圧力で伸張し、破断することなく剛性溶液外筒３０２の内面に接し、さらに除圧すなわち溶液を除去することにより薄肉内筒３１０が縮径して元の直径に戻ること、及び、移送される溶液すなわち液体固体混合物の温度及び圧力で伸張した時、薄肉内筒３１０が剛性溶液外筒３０２によりバックアップされるすなわち薄肉内筒３１０が剛性溶液外筒３０２によって周囲が支えられることを、演算によって説明する。 In the following, the thin inner cylinder 310 extends at the temperature and pressure of the solution to be transferred, for example, the mixture of the reaction product and the solvent, contacts the inner surface of the rigid solution outer cylinder 302 without breaking, and further releases the pressure, that is, the solution. When the thin inner cylinder 310 is reduced in diameter to return to its original diameter by removing the liquid, and when it is extended by the temperature and pressure of the solution to be transferred, that is, the liquid solid mixture, the thin inner cylinder 310 becomes the rigid solution outer cylinder 302. The fact that the periphery of the thin inner cylinder 310 is supported by the rigid solution outer cylinder 302 will be described by calculation.
薄肉円筒３１０のフープ力すなわち周方向の引っ張り応力σiＮ／ｍ2は、図１６に示すように、内径Ｄｍｍ、肉厚ｔｍｍ、長さｌｍｍ、内圧Ｐパスカルとするとき、
σi＝ｐＤｌ／２ｔｌ＝ＰＤ／２ｔ ・・・・・ （１）
である。例えば、株式会社技術評論社平成２４年５月２５日発行「入門材料力学」（有光隆著）第７０頁第８行の「円周方向に発生する引張り応力」に記載されているとおりである。
ここで、ＳＵＳ３０４の許容引張り応力は、JISG4303によると、４０℃において１９４メガパスカル、７５℃において１８０メガパスカル、１００℃において１７１メガパスカルである。
When the hoop force of the thin-walled cylinder 310, that is, the tensile stress σ i N / m 2 in the circumferential direction, is set to an inner diameter Dmm, a wall thickness tmm, a length 1 mm, and an internal pressure P Pascal, as shown in FIG.
σ i = pDl / 2tl = PD / 2t (1)
It is. For example, as described in “Tensile stress generated in the circumferential direction” on page 8, line 8 of “Technical Review Co., Ltd.” published on May 25, 2012, “Introductory Materials Mechanics” (by Takashi Arimitsu) .
Here, according to JISG4303, the allowable tensile stress of SUS304 is 194 megapascals at 40 ° C., 180 megapascals at 75 ° C., and 171 megapascals at 100 ° C.
工業上多く見られるような、被熱交換流体室高温部１４ａの温度が７０℃、１．２０メガパスカルであり、被熱交換流体室低温部１４ｂの温度が５７℃、１．１４メガパスカルであることを考慮し、以下の値により演算する。
剛性溶液外筒１０２の肉厚は、２．０ミリメートルである。剛性溶液外筒１０２の内径は、２１．４０ミリメートルである。薄肉内筒１１０は、外径が２１．３７ミリメートルである。薄肉内筒１１０の肉厚は、０．０４ミリメートルである。薄肉内筒１１０の内圧は、１．２０メガパスカルである。剛性溶液外筒１０２及び薄肉内筒１１０の材料であるＳＵＳ３０４のヤング率は、２００ギガパスカルである。
剛性溶液外筒１０２の内面と薄肉内筒１１０の外面のクリアランスすなわち間隔は、０．０３ミリメートルの半分の０．０１５ミリメートルである。
The temperature of the heat exchange fluid chamber high temperature portion 14a is 70 ° C. and 1.20 megapascals, and the temperature of the heat exchange fluid chamber low temperature portion 14b is 57 ° C. and 1.14 megapascals, which is often seen in industry. In consideration of the fact, the calculation is performed with the following values.
The thickness of the rigid solution outer cylinder 102 is 2.0 millimeters. The inner diameter of the rigid solution outer cylinder 102 is 21.40 millimeters. The thin inner cylinder 110 has an outer diameter of 21.37 millimeters. The wall thickness of the thin inner cylinder 110 is 0.04 mm. The internal pressure of the thin inner cylinder 110 is 1.20 megapascals. The Young's modulus of SUS304, which is a material of the rigid solution outer cylinder 102 and the thin inner cylinder 110, is 200 gigapascals.
The clearance or distance between the inner surface of the rigid solution outer cylinder 102 and the outer surface of the thin inner cylinder 110 is 0.015 millimeter, which is half of 0.03 millimeter.
（薄肉内筒が剛性溶液外筒に密着）
フープ力 σi＝ＰＤ／２ｔ
＝（１．２MPa×２１．３０mm）／（２×０．０４mm）
＝３１９．５（メガパスカル）
フックの法則により
歪みε＝応力σi ／ヤング率
＝３１９．５MPa／２００GPa
＝０．００１６（０．１６％）
従って、薄肉内筒１１０の外径は、内圧によって
２１．３７ｍｍ×０．００１６＝０．０３４ｍｍ
増加することになる。この値は、内圧によって薄肉内筒３１０が剛性溶液外筒３０２に密着する可能性を示す。
(The thin inner cylinder is in close contact with the rigid solution outer cylinder)
Hoop force σ i = PD / 2t
= (1.2MPa × 21.30mm) / (2 × 0.04mm)
= 319.5 (megapascal)
By hook's law
Strain ε = Stress σ i / Young's modulus
= 319.5MPa / 200GPa
= 0.0016 (0.16%)
Therefore, the outer diameter of the thin inner cylinder 110 depends on the internal pressure.
21.37 mm × 0.0016 = 0.034 mm
Will increase. This value indicates the possibility that the thin inner cylinder 310 is in close contact with the rigid solution outer cylinder 302 due to the internal pressure.
（剛性溶液外筒の薄肉内筒膨張のバックアップ）
剛性溶液外筒１０２に、内圧１．２０メガパスカルが負荷されたと仮定する。
フープ力 σi＝ＰＤ／２ｔ
＝（１．２MPa×２３．４０mm）／（２×２．０mm）
＝７．０２MPa
フックの法則により
歪みε＝応力σi ／ヤング率
＝７．０２ MPa／２００GPa
＝０．０００
従って、 剛性溶液外筒３０２に、内圧１．２０メガパスカルが負荷されたとしても、剛性溶液外筒３０２はほとんど伸張せず、薄肉内筒３１０のバックアップが可能である。
(Backing up expansion of thin inner cylinder of rigid solution outer cylinder)
Assume that the rigid solution outer cylinder 102 is loaded with an internal pressure of 1.20 megapascals.
Hoop force σ i = PD / 2t
= (1.2MPa × 23.40mm) / (2 × 2.0mm)
= 7.02 MPa
By hook's law
Strain ε = Stress σ i / Young's modulus
= 7.02 MPa / 200GPa
= 0.000
Therefore, even if the rigid solution outer cylinder 302 is loaded with an internal pressure of 1.20 megapascals, the rigid solution outer cylinder 302 hardly expands and the thin inner cylinder 310 can be backed up.
（薄肉内筒の縮径）
「東京都立産業技術研究センター研究報告、第５号、２０１０年」（第７８頁）等に記載された「０．２％耐力」は、ある圧力を負荷して除圧した時の残留歪みが０．２％以内であることを示す。同論文によると、ＳＵＳ３０４の０．２％耐力は、３１４MPaである。すなわち、３１４MPaは、ＳＵＳ３０４においては、降伏値以上の値である。ただし、本実施形態において、剛性溶液外筒３０２と薄肉内筒３１０のクリアランスが０．２％以内であれば、クリープ現象や金属疲労によって残留歪みが発生したとしても０．２％以内に留まる。仮に、剛性溶液外筒３０２と薄肉内筒３１０のクリアランスが０．１％以内であれば、薄肉内筒３１０は、剛性溶液外筒３０２に密着し、剛性溶液外筒３０２にバックアップされ、除圧後回復して原寸に戻る。
(Reduced diameter of thin inner cylinder)
“0.2% proof stress” described in “Research Report of Tokyo Metropolitan Industrial Technology Research Center, No. 5, 2010” (page 78) is the residual strain when a certain pressure is applied and the pressure is removed. It is within 0.2%. According to the paper, the 0.2% yield strength of SUS304 is 314 MPa. That is, 314 MPa is a value equal to or greater than the yield value in SUS304. However, in this embodiment, if the clearance between the rigid solution outer cylinder 302 and the thin inner cylinder 310 is within 0.2%, even if residual strain occurs due to creep phenomenon or metal fatigue, it remains within 0.2%. If the clearance between the rigid solution outer cylinder 302 and the thin inner cylinder 310 is within 0.1%, the thin inner cylinder 310 is in close contact with the rigid solution outer cylinder 302 and is backed up by the rigid solution outer cylinder 302 to remove pressure. It recovers afterwards and returns to the original size.
薄肉内筒３１０の内部には、図１５に示すように、上述した第１実施形態で使用した螺旋部材２０２と同一の構成の螺旋部材４００が配置される。 As shown in FIG. 15, a spiral member 400 having the same configuration as that of the spiral member 202 used in the first embodiment is disposed inside the thin inner cylinder 310.
次に、本発明の溶液移送冷却装置１の使用方法について説明する。最初に、剛性混合物外筒３０２に薄肉内筒３１０を挿入する。この際、薄肉内筒３１０が例えば５１４グラムと軽いことに加えて、剛性混合物外筒３０２の内面と薄肉内筒３１０の外面との間に空間があることから、例えば１０メートルに及ぶ長いものでも容易に挿入することができる。挿入された薄肉内筒３１０は、そのままでも良いが、好ましくは、かしめ加工等によって薄肉内筒３１０の両端部を剛性混合物外筒３０２の両端部に固着する。 Next, the usage method of the solution transfer cooling apparatus 1 of this invention is demonstrated. First, the thin inner cylinder 310 is inserted into the rigid mixture outer cylinder 302. At this time, since the thin inner cylinder 310 is light, for example, 514 grams, there is a space between the inner surface of the rigid mixture outer cylinder 302 and the outer surface of the thin inner cylinder 310. Can be inserted easily. The inserted thin inner cylinder 310 may be used as it is, but preferably, both ends of the thin inner cylinder 310 are fixed to both ends of the rigid mixture outer cylinder 302 by caulking or the like.
この状態で薄肉内筒３１０内に重合生成物を流入させれば、重合生成物の圧力によって薄肉内筒３１０が伸張して、薄肉内筒３１０の全外周面が剛性混合物外筒３０２の内周面に接する。その結果、薄肉内筒３１０の全外周面が剛性混合物外筒３０２の内周面によって支えられる。さらに、薄肉内筒３１０の全外周面が剛性混合物外筒３０２の内周面に接することにより、薄肉内筒３１０内を移送される重合生成物は、剛性混合物外筒３０２と剛性冷媒外筒３００の間を流動する冷媒によって効率的に冷却することができる。 If the polymerization product is allowed to flow into the thin inner cylinder 310 in this state, the thin inner cylinder 310 expands due to the pressure of the polymerization product, and the entire outer peripheral surface of the thin inner cylinder 310 becomes the inner periphery of the rigid mixture outer cylinder 302. Touch the surface. As a result, the entire outer peripheral surface of the thin inner cylinder 310 is supported by the inner peripheral surface of the rigid mixture outer cylinder 302. Further, since the entire outer peripheral surface of the thin inner cylinder 310 is in contact with the inner peripheral surface of the rigid mixture outer cylinder 302, the polymerization product transferred through the thin inner cylinder 310 is separated from the rigid mixture outer cylinder 302 and the rigid refrigerant outer cylinder 300. It can cool efficiently with the refrigerant | coolant which flows between.
液体固体混合物移送装置の長期間の連続作動により、薄肉内筒３１０内に重合体ファウリングが形成された場合、液体固体混合物移送装置への重合生成物の流入を止める。次に、薄肉内筒３１０より螺旋部材４００を引き抜く。一方、重合生成物の流入を止めることにより薄肉内筒３１０内部は、常圧に戻り、薄肉内筒３１０が縮小し、元の直径に戻る。この結果、剛性混合物外筒３０２の内周面と薄肉内筒３１０の外周面の間に空間ができ、薄肉内筒３１０を剛性混合物外筒３０２から容易に取り出すことができる。 When a polymer fouling is formed in the thin inner cylinder 310 by continuous operation of the liquid / solid mixture transfer device for a long period of time, the flow of the polymerization product into the liquid / solid mixture transfer device is stopped. Next, the spiral member 400 is pulled out from the thin inner cylinder 310. On the other hand, by stopping the inflow of the polymerization product, the inside of the thin inner cylinder 310 returns to normal pressure, and the thin inner cylinder 310 shrinks and returns to the original diameter. As a result, a space is formed between the inner peripheral surface of the rigid mixture outer cylinder 302 and the outer peripheral surface of the thin inner cylinder 310, and the thin inner cylinder 310 can be easily taken out from the rigid mixture outer cylinder 302.
取り出した螺旋部材４００及び薄肉内筒３１０は、工場等作業しやすい場所で重合体ファウリングを除去する。重合体ファウリングを除去された薄肉内筒１１０は、上述した方法によって剛性混合物外筒３０２に入れる。
予備の螺旋部材４００及び薄肉内筒１１０を準備して、重合体ファウリングが形成された螺旋部材４００及び薄肉内筒３１０を該予備の螺旋部材４００及び薄肉内筒１１０に置換することは、重合体ファウリングの高所除去作業を安全に且つ短時間に行うことであり、重合体の生産効率を高めるために極めて有効である。
The spiral member 400 and the thin inner cylinder 310 taken out remove the polymer fouling in a place where it is easy to work such as a factory. The thin inner cylinder 110 from which the polymer fouling has been removed is put into the rigid mixture outer cylinder 302 by the method described above.
Preparing the spare spiral member 400 and the thin inner cylinder 110 and replacing the spiral member 400 and the thin inner cylinder 310 formed with the polymer fouling with the spare spiral member 400 and the thin inner cylinder 110 is important. This is a safe and short time removal work for coalescence fouling in a high place, which is extremely effective for increasing the production efficiency of the polymer.
Ｒ 溶液
Ｗ 冷媒
１ 溶液移送冷却装置
１０ 冷媒シェル
１２ 熱交換チューブ支持板
１４ 溶液室
１６ 冷媒室
２０ シェルカバー
２２ 溶液入口
２４ 溶液出口
３０ 冷媒室蓋
１０２ 熱交換チューブ
２０２ａ 平板状部材
２０２ｂ 波板部材
２０２ｃ 螺旋部材
２０６ 折り曲げ波板
２２０ 第１エンボス螺旋部材
２２２ 第２エンボス螺旋部材
２３０ メッシュ螺旋板
３００ 剛性冷媒外筒
３０２ 剛性溶液外筒
３０４ 剛性溶液外筒支持板
３０６ 溶接
３１０ 薄肉内筒
R Solution W Refrigerant 1 Solution transfer cooling device 10 Refrigerant shell 12 Heat exchange tube support plate 14 Solution chamber 16 Refrigerant chamber 20 Shell cover 22 Solution inlet 24 Solution outlet 30 Refrigerant chamber lid 102 Heat exchange tube 202a Flat plate member 202b Corrugated plate member 202c Helical member 206 Bending corrugated plate 220 First embossed spiral member 222 Second embossed spiral member 230 Mesh spiral plate 300 Rigid refrigerant outer cylinder 302 Rigid solution outer cylinder 304 Rigid solution outer cylinder support plate 306 Welding 310 Thin inner cylinder
Claims (20)
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材が、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする溶液移送冷却装置。 In the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
Inside the heat exchange tube, a metal separation plate-like member that divides the cross section of the heat exchange tube into at least two equal parts is formed continuously and spirally along the entire length of the central axis of the heat exchange tube. A featured solution transfer cooling device.
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を配置し、該金属分離板状部材が、長手方向に延びた中心領域の引っ張り抵抗より長手方向へ延びた両縁領域の引っ張り抵抗が大きい板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする溶液移送冷却装置。 In the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
A metal separation plate member that divides the cross section of the heat exchange tube into at least two equal parts is disposed inside the heat exchange tube, and the metal separation plate member is longer in the longitudinal direction than the tensile resistance of the central region extending in the longitudinal direction. A plate-like member having a large tensile resistance in both edge regions extending to the side is formed in a spiral shape continuously along the entire length of the central axis of the heat exchange tube.
前記冷却流路部は、冷媒シェルの内部に、複数の熱交換チューブを互いに平行に配置し、前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする重合体製造装置。 A polymer production apparatus having a polymerization reaction apparatus and a cooling flow path section connected to a polymerization product outlet section of the polymerization reaction apparatus and having a heat exchange function,
The cooling channel section has a plurality of heat exchange tubes arranged in parallel with each other in the refrigerant shell, and a metal separation plate-like member that divides the cross section of the heat exchange tube into at least two equal parts in the heat exchange tube Is formed continuously in a spiral shape along the entire length of the central axis of the heat exchange tube.
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成されていることを特徴とする溶液移送冷却装置の製造方法。 In the manufacturing method of the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
Inside the heat exchange tube, a metal separation plate-like member that divides the cross section of the heat exchange tube into at least two equal parts is formed continuously and spirally along the entire length of the central axis of the heat exchange tube. A manufacturing method of a solution transfer cooling device characterized by the above.
前記熱交換チューブの内部に、前記熱交換チューブの断面を少なくとも２等分割する金属分離板状部材を配置し、該金属分離板状部材が、長手方向に延びた中心領域の引っ張り抵抗より長手方向へ延びた両縁領域の引っ張り抵抗が大きい板状部材を、前記熱交換チューブの中心軸線全長に沿って連続して螺旋状に形成することを特徴とする溶液移送冷却装置の製造方法。 In the manufacturing method of the solution transfer cooling device in which a plurality of heat exchange tubes are arranged in parallel with each other inside the refrigerant shell,
A metal separation plate member that divides the cross section of the heat exchange tube into at least two equal parts is disposed inside the heat exchange tube, and the metal separation plate member is longer in the longitudinal direction than the tensile resistance of the central region extending in the longitudinal direction. A method for manufacturing a solution transfer cooling device, comprising: forming a plate-like member having a large tensile resistance in both edge regions extending in a spiral manner along the entire length of the central axis of the heat exchange tube.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015016275A JP2016148459A (en) | 2015-01-30 | 2015-01-30 | Solution transfer cooling device and manufacturing method |
| PCT/JP2016/052718 WO2016121949A1 (en) | 2015-01-30 | 2016-01-29 | Fluid heat-exchanging, mixing, and transferring device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015016275A JP2016148459A (en) | 2015-01-30 | 2015-01-30 | Solution transfer cooling device and manufacturing method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2016148459A true JP2016148459A (en) | 2016-08-18 |
Family
ID=56688304
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2015016275A Pending JP2016148459A (en) | 2015-01-30 | 2015-01-30 | Solution transfer cooling device and manufacturing method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2016148459A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57187596A (en) * | 1981-05-13 | 1982-11-18 | Hitachi Ltd | Method of removing soil in pipe line |
| JPS61103529A (en) * | 1984-10-29 | 1986-05-22 | Mitsubishi Heavy Ind Ltd | Stirring device for material having high viscosity |
| JPH11349605A (en) * | 1998-06-09 | 1999-12-21 | Nichiban Co Ltd | Photo-polymerization unit and manufacture of polymer therewith |
| US7087097B1 (en) * | 1999-06-09 | 2006-08-08 | Technische Universitat Munchen Lehrstuhl Fur Thermische Kraftanlagen | Facility for the gasification of carbon-containing feed materials |
| JP2006528719A (en) * | 2003-05-19 | 2006-12-21 | テサ・アクチエンゲゼルシヤフト | Continuous production method of polymer comprising vinyl compound by material and / or solvent polymerization |
| JP2008111119A (en) * | 2006-10-30 | 2008-05-15 | Rohm & Haas Co | Method for stripping polymer dispersion |
| JP2008531959A (en) * | 2005-02-10 | 2008-08-14 | サン−ゴバン・ベトロテ・フランス | Equipment for extracting heat from gas and recovering condensate |
| JP2011006632A (en) * | 2009-06-29 | 2011-01-13 | Konica Minolta Business Technologies Inc | Tubular flow reactor and method for producing resin fine particle using the tubular flow reactor |
-
2015
- 2015-01-30 JP JP2015016275A patent/JP2016148459A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57187596A (en) * | 1981-05-13 | 1982-11-18 | Hitachi Ltd | Method of removing soil in pipe line |
| JPS61103529A (en) * | 1984-10-29 | 1986-05-22 | Mitsubishi Heavy Ind Ltd | Stirring device for material having high viscosity |
| JPH11349605A (en) * | 1998-06-09 | 1999-12-21 | Nichiban Co Ltd | Photo-polymerization unit and manufacture of polymer therewith |
| US7087097B1 (en) * | 1999-06-09 | 2006-08-08 | Technische Universitat Munchen Lehrstuhl Fur Thermische Kraftanlagen | Facility for the gasification of carbon-containing feed materials |
| JP2006528719A (en) * | 2003-05-19 | 2006-12-21 | テサ・アクチエンゲゼルシヤフト | Continuous production method of polymer comprising vinyl compound by material and / or solvent polymerization |
| JP2008531959A (en) * | 2005-02-10 | 2008-08-14 | サン−ゴバン・ベトロテ・フランス | Equipment for extracting heat from gas and recovering condensate |
| JP2008111119A (en) * | 2006-10-30 | 2008-05-15 | Rohm & Haas Co | Method for stripping polymer dispersion |
| JP2011006632A (en) * | 2009-06-29 | 2011-01-13 | Konica Minolta Business Technologies Inc | Tubular flow reactor and method for producing resin fine particle using the tubular flow reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5953619B2 (en) | Solution transfer cooling system | |
| EP0029701B1 (en) | Process and apparatus for the prevention of solids deposits in a tubular reactor | |
| EP0944431A1 (en) | Device for continuously carrying out chemical reactions | |
| KR102187726B1 (en) | Method and system for distributing liquid in (meth)acrylic monomer process vessels | |
| JP2002001017A (en) | Solid removing device | |
| CN102686310A (en) | Separation vessels for use in polymerization processes and methods for cleaning same | |
| JP2016148459A (en) | Solution transfer cooling device and manufacturing method | |
| JP6675132B2 (en) | Heat exchange mixing device and solution transfer cooling device | |
| JP3208713U (en) | Heat exchange mixing device and solution transfer cooling device | |
| WO2017085944A1 (en) | Heat exchange mixing device and solution conveying/cooling device | |
| US11571678B2 (en) | High pressure strippers for use in urea plants | |
| US10899981B2 (en) | Method for removing fouling downstream of an ODH reactor | |
| US10851041B2 (en) | Fouling-resistant distillation column and process for the manufacture of compounds | |
| US20150126771A1 (en) | Multi-phase reactor system with slinger liquid reflux distributor | |
| WO2020157089A1 (en) | High pressure strippers for use in urea plants | |
| JP2005170931A (en) | Container for easily polymerizable compound | |
| EP3471872A1 (en) | Scallop support distributor for radial flow reactor | |
| JPS6063205A (en) | Tubular ring-shaped reactor for polymerization of alpha-olefin | |
| PL179096B1 (en) | Method of feeding reactants to comntinuously operating reactors for production of polyacetals |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A02 | Decision of refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A02 Effective date: 20160112 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20160421 |
|
| A911 | Transfer of reconsideration by examiner before appeal (zenchi) |
Free format text: JAPANESE INTERMEDIATE CODE: A911 Effective date: 20160519 |
|
| A912 | Removal of reconsideration by examiner before appeal (zenchi) |
Free format text: JAPANESE INTERMEDIATE CODE: A912 Effective date: 20160805 |