JP2000117001A - Cooling method of fluid to be condensed by condenser - Google Patents
Cooling method of fluid to be condensed by condenserInfo
- Publication number
- JP2000117001A JP2000117001A JP30954698A JP30954698A JP2000117001A JP 2000117001 A JP2000117001 A JP 2000117001A JP 30954698 A JP30954698 A JP 30954698A JP 30954698 A JP30954698 A JP 30954698A JP 2000117001 A JP2000117001 A JP 2000117001A
- Authority
- JP
- Japan
- Prior art keywords
- condensed
- heat transfer
- fluid
- condenser
- transfer tube
- 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
- 239000012530 fluid Substances 0.000 title claims abstract description 34
- 238000001816 cooling Methods 0.000 title claims abstract description 17
- 238000012546 transfer Methods 0.000 claims abstract description 69
- 238000000034 method Methods 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims description 54
- 238000006116 polymerization reaction Methods 0.000 claims description 29
- 239000001257 hydrogen Substances 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 239000004711 α-olefin Substances 0.000 claims description 12
- 239000002826 coolant Substances 0.000 claims description 8
- 230000002093 peripheral effect Effects 0.000 claims description 2
- 238000005192 partition Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 238000013461 design Methods 0.000 description 10
- 238000004364 calculation method Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 241000183024 Populus tremula Species 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- 241001125929 Trisopterus luscus Species 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 101100321669 Fagopyrum esculentum FA02 gene Proteins 0.000 description 1
- 101000917826 Homo sapiens Low affinity immunoglobulin gamma Fc region receptor II-a Proteins 0.000 description 1
- 101000917824 Homo sapiens Low affinity immunoglobulin gamma Fc region receptor II-b Proteins 0.000 description 1
- 102100029204 Low affinity immunoglobulin gamma Fc region receptor II-a Human genes 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 230000001680 brushing effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002681 magnesium compounds Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000013178 mathematical model Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002685 polymerization catalyst Substances 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
(57)【要約】
【課題】 縦型の多管式凝縮器を用いて、非凝縮成分を
含有する被凝縮流体を効率的に冷却する方法を提供す
る。
【解決手段】 非凝縮成分を含有する被凝縮流体を縦型
の多管式凝縮器の上部より下部に向って流通させ、その
際、凝縮器の伝熱管における被凝縮流体の線速を１．０
〜４．０ｍ／ｓｅｃの範囲で運転することを特徴とす
る。
PROBLEM TO BE SOLVED: To provide a method for efficiently cooling a fluid to be condensed containing non-condensable components by using a vertical multi-tube condenser. SOLUTION: A fluid to be condensed containing a non-condensable component is caused to flow from an upper portion to a lower portion of a vertical multi-tube condenser, and at this time, the linear velocity of the fluid to be condensed in a heat transfer tube of the condenser is set to 1. 0
It is characterized by operating in a range of up to 4.0 m / sec.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、凝縮器による被凝
縮ガスを含む被凝縮流体の冷却方法に関し、例えば、α
−オレフィンの重合に際して生ずるα−オレフィンと水
素を含む未反応ガスを凝縮器を用いて効率的に冷却する
方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for cooling a condensed fluid containing a gas to be condensed by a condenser.
The present invention relates to a method for efficiently cooling an unreacted gas containing α-olefin and hydrogen generated during the polymerization of olefin using a condenser.
【０００２】[0002]
【従来の技術】従来、α−オレフィンや塩化ビニル等の
重合性単量体を重合する際に発生する重合熱を除去する
ために、重合性単量体若しくは溶媒蒸気を含む被凝縮流
体を凝縮器で冷却して凝縮液化させ除熱することが行わ
れている。この被凝縮流体の冷却には一般的に多管式の
縦型の還流凝縮器が使用され、該還流凝縮器を通過する
被凝縮流体を冷却媒体で間接的に冷却し、生じた凝縮液
を重合槽内に戻す事により、重合熱の除去が図られてい
る。一般に凝縮器の設計はマス・ヒートバランスと熱交
換器設計方法に準じて行う。例えば既存のエンジニアリ
ングツールでは前者がＡＳＰＥＮ ＰＬＵＳ、ＰｒｏII
等が相当し、後者がＨＴＦＳ、ＨＴＲＩ等に相当する。
なおＡＳＰＥＮ ＰＬＵＳはＡｓｐｅｎ Ｔｅｃｈｎｏ
ｌｏｇｙ，Ｉｎｃ．ＰｒｏIIはＳｉｍｕｌａｔｉｏｎ
Ｓｃｉｅｎｃｅｓ，Ｉｎｃ．のソフトウェアで、共にプ
ラントにおける物理化学現象、例えば物質収支、熱収
支、相平衡等の数式モデルをコンピュータで数値的に解
くための世界的に普及している商用ソフトである。ま
た、ＨＴＦＳ、ＨＴＲＩは、熱交換器設計や既存熱交換
器の性能評価のための商用ソフトである。一方、最近の
市場要求としてポリプロピレンの高流動性が求められて
きており、反応器で低分子量側へシフトする必要性が高
まっている。この為、反応器の運転条件としては、プロ
ピレンの重合反応において、反応系の水素等を高濃度に
して対応する必要性があり、さらに、マグネシウム化合
物担持型の高活性触媒を使用した場合には、より高濃度
の水素濃度に設定することが必要となる。このプロピレ
ン等の被凝縮流体に水素等非凝縮ガスが含まれる系にお
いて、被凝縮成分を効率的に冷却して凝縮液化させるに
際し、被凝縮ガスは複雑な挙動を示し、その冷却効率を
低下させるため、凝縮器冷却システムの運転、及び設計
方法の両面から考慮する必要がある。2. Description of the Related Art Conventionally, a condensed fluid containing a polymerizable monomer or a solvent vapor is condensed in order to remove polymerization heat generated when polymerizing a polymerizable monomer such as an α-olefin or vinyl chloride. It is cooled in a vessel to condense and liquefy and remove heat. Generally, a multi-tube vertical reflux condenser is used for cooling the condensed fluid, and the condensed fluid passing through the reflux condenser is indirectly cooled with a cooling medium, and the generated condensate is discharged. By returning to the inside of the polymerization tank, the heat of polymerization is removed. Generally, the design of the condenser is performed in accordance with the mass heat balance and the heat exchanger design method. For example, in the existing engineering tools, the former is ASPEN PLUS, ProII
Etc., and the latter corresponds to HTFS, HTRI, etc.
ASPEN PLUS is Aspen Techno
logic, Inc. ProII is Simulation
Sciences, Inc. Is commercial software that is widely used worldwide for numerically solving mathematical models of physicochemical phenomena in a plant, for example, material balance, heat balance, phase equilibrium, and the like by a computer. HTFS and HTRI are commercial software for heat exchanger design and performance evaluation of existing heat exchangers. On the other hand, as a recent market requirement, high fluidity of polypropylene has been demanded, and the need to shift to a lower molecular weight side in a reactor is increasing. For this reason, as the operating conditions of the reactor, in the polymerization reaction of propylene, it is necessary to cope with a high concentration of hydrogen or the like in the reaction system, and when a highly active catalyst supporting a magnesium compound is used, , It is necessary to set a higher hydrogen concentration. In a system in which a non-condensable gas such as hydrogen is contained in a fluid to be condensed such as propylene, when the component to be condensed is efficiently cooled and condensed and liquefied, the gas to be condensed has a complicated behavior, and the cooling efficiency is reduced. Therefore, it is necessary to consider both the operation of the condenser cooling system and the design method.
【０００３】[0003]
【発明が解決しようとする課題】発明者らの知見による
と、既存のエンジニアリングツール（ＨＴＦＳ、ＨＴＲ
Ｉ等）のみを用いた従来の設計方法は解析能力として充
分ではなく満足できるものではなかった。具体的には、
縦型の多管式凝縮器を非凝縮ガスが高濃度に含まれる系
にて、該エンジニアリングツールを用い解析した場合、
シミュレーションで期待される冷却能力が、実際は得ら
れないと言う課題を有していた。即ち、上記の水素等の
非凝縮ガスを含む被凝縮流体を縦型の凝縮器を使用した
場合、各伝熱管を通過するガス流量に偏りが生じ、つい
には下向きの流れが阻害され除熱性能が得られない伝熱
管が発生する。この伝熱管の発生が上述したエンジニア
リングツールによるシミュレーション結果と実際の冷却
能力の差異の要因である。本発明においては、上記の様
な除熱性能が得られない伝熱管の発生を抑制する為の凝
縮器の除熱方法を提供する事を目的とする。According to the knowledge of the inventors, existing engineering tools (HTFS, HTR
The conventional design method using only I) is not sufficient and not satisfactory as an analysis capability. In particular,
When a vertical multi-tube condenser is analyzed using the engineering tool in a system where non-condensable gas is contained in high concentration,
There is a problem that the cooling capacity expected in the simulation cannot be actually obtained. That is, when the condensed fluid containing the non-condensable gas such as hydrogen is used in a vertical condenser, the flow rate of the gas passing through each heat transfer tube is biased, and finally the downward flow is hindered and the heat removal performance is reduced. A heat transfer tube that cannot be obtained is generated. The generation of the heat transfer tubes is a factor of the difference between the simulation result by the engineering tool described above and the actual cooling capacity. An object of the present invention is to provide a method for removing heat of a condenser for suppressing generation of a heat transfer tube in which the above-described heat removal performance cannot be obtained.
【０００４】[0004]
【課題を解決するための手段】本発明者等は上記問題点
に鑑み、縦型の多管式凝縮器を用いて、非凝縮成分を含
有する被凝縮流体の効率的な冷却方法について鋭意検討
した結果、上記凝縮器の伝熱管内における被凝縮流体の
線速を特定の範囲にすること、即ち非凝縮ガスを重合槽
に戻す為のブロアーを選定、若しくは、非凝縮ガスの一
部をブロアーにて該凝縮器にリサイクルする事により、
上記問題点が解決できることを見出し、本発明を完成す
るに至った。SUMMARY OF THE INVENTION In view of the above problems, the present inventors have intensively studied a method for efficiently cooling a condensed fluid containing non-condensable components using a vertical multi-tube condenser. As a result, the linear velocity of the fluid to be condensed in the heat transfer pipe of the condenser is set to a specific range, that is, a blower for returning the non-condensable gas to the polymerization tank is selected, or a part of the non-condensable gas is blown. By recycling to the condenser at
The inventors have found that the above problems can be solved, and have completed the present invention.
【０００５】本発明の要旨は、実質的に垂直な直管状の
伝熱管からなる伝熱管束が、上下１対の水平隔板の間に
設置されており、被凝縮流体が上記伝熱管内の上部から
下部に向かって流通させられ、一方冷却媒体が上記一対
の水平隔板の間に流され、上記伝熱管の外周面に接触し
つつ流動する構造を有する縦型の多管式の凝縮器を用い
て被凝縮流体を冷却して凝縮液化させる方法において、
被凝縮流体が非凝縮成分を含有し、且つ該伝熱管におけ
る被凝縮流体の線速を１．０〜４．０ｍ／ｓｅｃの範囲
で運転することを特徴とする凝縮器による被凝縮流体の
冷却方法、に存する。[0005] The gist of the present invention is that a heat transfer tube bundle composed of a substantially vertical straight tube heat transfer tube is installed between a pair of upper and lower horizontal plates, and the fluid to be condensed is placed in the heat transfer tube. A vertical multi-tube condenser having a structure in which the cooling medium is caused to flow from the upper part to the lower part, while the cooling medium is caused to flow between the pair of horizontal diaphragms and flows while contacting the outer peripheral surface of the heat transfer tube. In the method of condensing and liquefying the fluid to be condensed using
The condensed fluid contains a non-condensed component, and operates at a linear velocity of the condensed fluid in the heat transfer tube within a range of 1.0 to 4.0 m / sec. The way, lies in.
【０００６】[0006]
【発明の実施の形態】以下、本発明の凝縮器を用いた被
凝縮流体の冷却方法における冷却システムを、図１に基
づき説明する。図１において、重合槽１に原料のα−オ
レフィン、水素等の分子量調整剤、重合触媒、場合によ
り溶媒として炭化水素が供給され、反応熱により上部か
ら蒸発したα−オレフィン他の該供給物がまず凝縮器２
に導入され、器内で凝縮が容易なガスを液化し、次のド
ラム３で気液分離し、非凝縮ガスはブロアー４で昇圧し
重合槽１、若しくは凝縮器２に戻し、他方、凝縮液も自
圧もしくはポンプで昇圧し重合槽１に戻す除熱システム
が使用される。システムの構成としては、凝縮させて除
熱するという目的が達成されるものであれば特に制限は
ない。ここで凝縮器とは前記縦型の多管式の凝縮器の様
な一般的な多管式の熱交換器が使用に供される。凝縮液
は、基本的には重合槽に戻されるが、その他の目的、例
えば洗浄用ブラッシング等に用いても構わない。非凝縮
ガスはブロアーにより昇圧され、基本的には重合槽に戻
されるが、重合槽の水素等の非凝縮ガスの濃度によって
は一部を凝縮器へリサイクルする。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A cooling system in a method for cooling a condensed fluid using a condenser according to the present invention will be described below with reference to FIG. In FIG. 1, a raw material α-olefin, a molecular weight regulator such as hydrogen, a polymerization catalyst, and a hydrocarbon as a solvent in some cases are supplied to a polymerization tank 1. First condenser 2
Liquefied gas which is easily condensed in the vessel, is separated into gas and liquid by the next drum 3, and the non-condensed gas is pressurized by the blower 4 and returned to the polymerization tank 1 or the condenser 2. Also, a heat removal system is used in which the pressure is raised by a self-pressure or a pump and returned to the polymerization tank 1. The configuration of the system is not particularly limited as long as the purpose of condensing and removing heat is achieved. Here, a general multi-tube heat exchanger such as the vertical multi-tube condenser is used for the condenser. The condensate is basically returned to the polymerization tank, but may be used for other purposes, for example, for brushing for cleaning. The pressure of the non-condensable gas is increased by a blower and returned to the polymerization tank, but a part of the gas is recycled to the condenser depending on the concentration of non-condensable gas such as hydrogen in the polymerization tank.
【０００７】本発明においては、凝縮器の伝熱管内を流
通させる被凝縮流体の線速を、１．０〜４．０ｍ／ｓｅ
ｃの範囲、好ましくは１．３〜４．０ｍ／ｓｅｃの範囲
で運転することを特徴とするものである。被凝縮流体の
線速が１．０ｍ／ｓｅｃ未満で流通した場合には、伝熱
管内平均ガス線速が極めて低くなる結果、各伝熱管を通
過するガス流量に偏りが生じる。より低流速の伝熱管に
おいては凝縮がより進行し、結果として、例えば水素等
非凝縮ガスが高濃度化し、ついにはその伝熱管内の平均
ガス密度ρｇ２が凝縮器入出の平均ガス密度ρｇ１より
低くなり、下向きの流れが阻害され除熱性能が得られな
い伝熱管が発生する。図２に模式図を示す。即ち、伝熱
管内の線速が低い場合は、正常に流通する伝熱管本数
は、伝熱管長をＨとすると、下式に示す様にその管内で
の動圧力損失ΔＰｓが２者（正常な流通のある伝熱管と
下向きの流れの阻害された伝熱管）のガスヘッド差と等
しくなる様に定まっていると推定される。In the present invention, the linear velocity of the fluid to be condensed flowing through the heat transfer tube of the condenser is 1.0 to 4.0 m / sec.
The operation is performed in the range of c, preferably in the range of 1.3 to 4.0 m / sec. If the fluid to be condensed flows at a linear velocity of less than 1.0 m / sec, the average gas linear velocity in the heat transfer tubes becomes extremely low, resulting in an uneven flow rate of the gas passing through each heat transfer tube. In a heat transfer tube having a lower flow rate, the condensation proceeds more, and as a result, a non-condensable gas such as hydrogen becomes highly concentrated. As a result, the average gas density ρg2 in the heat transfer tube is lower than the average gas density ρg1 in and out of the condenser. This causes a heat transfer tube in which the downward flow is impeded and heat removal performance cannot be obtained. FIG. 2 shows a schematic diagram. That is, when the linear velocity in the heat transfer tube is low, the number of heat transfer tubes normally flowing is as follows, assuming that the length of the heat transfer tube is H, the dynamic pressure loss ΔPs in the tube is two (normal It is presumed that it is determined to be equal to the gas head difference between the heat transfer tube with circulation and the heat transfer tube in which the downward flow is inhibited.
【０００８】即ち、図２中、流れの阻害された伝熱管
（右側）においては、内部ガスが胴側の冷却水温まで温
度が低下する為、プロピレン凝縮がより進行し相対的に
水素比率が大きくなり、密度に関してはρｇ１＞ρｇ２
の関係がある。両者（左右）の圧力バランスを考えた場
合、伝熱管入圧をＰin、出圧をＰoutとすると、 １）正常伝熱管（左側）については、まず伝熱管の内部
ガスが出口側に圧力を加える（ρｇ１×Ｈ）。また、ガ
スの流通により圧力損失が発生（−ΔＰｓ）。即ち、Ｐ
out ＝Ｐin＋ρｇ１×Ｈ−ΔＰｓという関係が成り立
つ。２）流れの阻害された伝熱管についても、同様に内
部ガスが出口側に圧力を加える（ρｇ２×Ｈ）。ガスの
流通がない為、圧力損失は生じない。即ち、Ｐout ＝Ｐ
in＋ρｇ２×Ｈという関係が成り立つ。従って、１），
２）の連立方程式を解く事により、ΔＰｓ＝（ρｇ１−
ρｇ２）×Ｈ という関係式を得る事ができる。管内の
圧力損失は、Ｆａｎｎｉｎｇの式として化学工学的に広
く知られているように線速↑にて圧力損失↑する。ま
た、凝縮器に流入するガス量を一定と仮定すれば、流通
している伝熱管本数により個々の線速及び圧力損失が定
まる。That is, in FIG. 2, in the heat transfer tube (right side) where the flow is obstructed, the temperature of the internal gas decreases to the cooling water temperature on the body side, so that propylene condensation proceeds more and the hydrogen ratio becomes relatively large. And the density is ρg1> ρg2
There is a relationship. When considering the pressure balance between the two (left and right), assuming that the heat transfer tube input pressure is Pin and the output pressure is Pout, 1) For the normal heat transfer tube (left side), first, the gas inside the heat transfer tube applies pressure to the outlet side. (Ρg1 × H). In addition, pressure loss occurs due to gas flow (−ΔPs). That is, P
out = Pin + ρg1 × H−ΔPs holds. 2) The internal gas similarly applies pressure to the outlet side of the heat transfer tube in which the flow is inhibited (ρg2 × H). No pressure loss occurs because there is no gas flow. That is, Pout = P
The relationship of in + ρg2 × H holds. Therefore, 1),
By solving the simultaneous equations of 2), ΔPs = (ρg1-
ρg2) × H can be obtained. The pressure loss in the pipe decreases at a linear velocity {} as is widely known in chemical engineering as Fanning's equation. Further, assuming that the amount of gas flowing into the condenser is constant, each linear velocity and pressure loss are determined by the number of flowing heat transfer tubes.
【０００９】即ち、伝熱管本数↓ → 線速↑ → 圧
力損失ΔＰｓ↑ となり、ΔＰｓ＝（ρｇ１−ρｇ２）
×Ｈが成り立つような正常に流通する伝熱本数が定ま
る。従って、全ての伝熱管を有効に使用する為には、 ΔＰｓ≧（ρｇ１−ρｇ２）×Ｈ を満たす伝熱管内での流通線速にて運転する必要があ
る。That is, the number of heat transfer tubes ↓ → linear velocity ↑ → pressure loss ΔPs ↑, and ΔPs = (ρg1-ρg2)
The number of normally circulating heat transfer that satisfies × H is determined. Therefore, in order to use all the heat transfer tubes effectively, it is necessary to operate at a flow linear velocity in the heat transfer tubes that satisfies ΔPs ≧ (ρg1−ρg2) × H.
【００１０】更に、伝熱管内線速を４．０ｍ／ｓｅｃを
越えるように調整した場合には、この高流速に起因する
伝熱管内での圧力損失が増加し、気液分離ドラムの圧力
が低下し、凝縮液を自圧にて重合槽に戻す事が困難にな
り、ポンプで昇圧し重合槽に戻す設備を追加するか、若
しくは凝縮器及び気液分離ドラムを重合槽に対し更に高
い位置へ設置するプロット上の制限等が生ずる。Further, when the linear velocity in the heat transfer tube is adjusted to exceed 4.0 m / sec, the pressure loss in the heat transfer tube due to the high flow velocity increases, and the pressure of the gas-liquid separation drum decreases. However, it is difficult to return the condensed liquid to the polymerization tank under its own pressure.Add equipment to increase the pressure by a pump and return it to the polymerization tank, or move the condenser and gas-liquid separation drum to a position higher than the polymerization tank. There are restrictions on the plots to be installed.
【００１１】一方、該重合設備を用い、水素等非凝縮ガ
ス濃度が低い設定にて運転する場合を考慮すると、例え
ば重合槽ジャケットにおける冷却媒体と凝縮器の冷却媒
体が共通な場合は、高水素濃度設定と等しい生産能力を
得る為には、一般的により高い冷却媒体温度でヒートバ
ランスが得られる。従って、重合槽ジャケット等での除
熱負荷が減少し、相対的に凝縮器における除熱負荷が増
し、重合槽気相部における蒸発線速増加の要因となり、
重合液中に小粒径物が存在する場合は、エントレ、更に
凝縮器の汚れ速度を増加させる懸念がある。そこで、低
水素濃度にて該重合系を運転する場合は、凝縮器出口で
の非凝縮ガスの一部を凝縮器にリサイクルする事によ
り、重合槽での蒸発線速増加を抑制しつつ、上で述べた
伝熱管内線速を満足させる事が可能となる。On the other hand, considering the case where the polymerization equipment is used to operate at a low concentration of non-condensable gas such as hydrogen, for example, when the cooling medium in the polymerization tank jacket and the cooling medium for the condenser are common, high hydrogen In order to obtain a production capacity equal to the concentration setting, a heat balance is generally obtained at a higher cooling medium temperature. Therefore, the heat removal load in the polymerization tank jacket and the like is reduced, the heat removal load in the condenser is relatively increased, and the evaporation linear velocity in the polymerization tank gas phase is increased.
When small particles are present in the polymerization solution, there is a concern that the rate of fouling of the condenser and the condenser may be increased. Therefore, when operating the polymerization system at a low hydrogen concentration, a part of the non-condensable gas at the outlet of the condenser is recycled to the condenser, thereby suppressing an increase in the linear evaporation speed in the polymerization tank. It is possible to satisfy the linear velocity in the heat transfer tube described in (1).
【００１２】[0012]
【実施例】以下、実施例に沿って本発明を具体的に説明
する。 実施例１ 図３に示すパイロット設備を用いて実験した。図３にお
いて８は蒸発器で、ここで所定温度において蒸発したプ
ロピレンガスは、混合ドラム７へフィードされる。ここ
で水素を含む循環ガス系と混合されて凝縮器２へフィー
ドされる。更に気液分離ドラム３で分離された非凝縮ガ
スはブロアー４で混合ドラム７へ循環フィードされる。
凝縮プロピレンは蒸発器８へフィードされる。凝縮器２
の仕様としては、シェル内径；４５０ｍｍ、伝熱管長；
５ｍ及び３ｍのもの、伝熱管本数；２４０本、１２０本
及び８０本の三種、チューブ外径；１９ｍｍ。実験した
運転条件としては、混合ドラム温度；６５、７０℃、混
合ドラム圧力；２７．５〜３４．０ｋｇ／ｃｍ2 Ｇ、混
合ドラム気相部水素濃度；２、３、５、６、１２及び１
４ｍｏｌ％それぞれの濃度でテスト、凝縮器伝熱管入口
ガス線速；０．２〜２ｍ／ｓｅｃ、凝縮器除熱負荷；２
０〜２８０Ｍｃａｌ／Ｈである。また、解析の為に図３
に示す様に各所に温度計、圧力計、差圧計、プロセスガ
スクロ計を設置した。DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be specifically described below with reference to embodiments. Example 1 An experiment was performed using the pilot equipment shown in FIG. In FIG. 3, reference numeral 8 denotes an evaporator. Here, propylene gas evaporated at a predetermined temperature is fed to the mixing drum 7. Here, it is mixed with a circulating gas system containing hydrogen and fed to the condenser 2. Further, the non-condensed gas separated by the gas-liquid separation drum 3 is circulated and fed to the mixing drum 7 by the blower 4.
The condensed propylene is fed to the evaporator 8. Condenser 2
As the specifications of the shell inner diameter; 450 mm, heat transfer tube length;
5 m and 3 m, number of heat transfer tubes: 240, 120 and 80, three kinds of tube outer diameter: 19 mm. The operating conditions of the experiment were: mixing drum temperature; 65, 70 ° C .; mixing drum pressure; 27.5 to 34.0 kg / cm 2 G; mixing drum gas phase hydrogen concentration: 2, 3, 5, 6, 12, and 1
Tested at each concentration of 4 mol%, gas linear velocity at the inlet of the condenser heat transfer tube; 0.2 to 2 m / sec, condenser heat removal load; 2
0 to 280 Mcal / H. Fig. 3
A thermometer, a pressure gauge, a differential pressure gauge, and a process gas chromatograph were installed in various places as shown in (1).
【００１３】図４に本実験から得られた凝縮器総括伝熱
係数とＨＴＦＳが機器仕様から計算する総括伝熱係数を
比較した結果を示す。図４においては、実際の伝面が全
て熱交換に寄与するという前提に基いて総括伝熱係数を
算出したものである。実験からは、伝熱管入口での流通
線速の上昇に伴い総括伝熱係数が上昇するという合理的
な相関が得られたが、ＨＴＦＳが算出する該相関と比較
して遙かに小さい能力評価結果となった。また、線速が
１．０ｍ／ｓｅｃ以上の範囲では、両者の差異は縮小し
た。両者の差異は汚れ係数で０．０００５〜０．００１
５ｋｃａｌ／ｍ2 ｈ℃に相当し、絶対値にもバラツキに
関しても設備状況から説明のできない値であった。FIG. 4 shows the results obtained by comparing the overall heat transfer coefficient of the condenser obtained from this experiment with the overall heat transfer coefficient calculated by the HTFS from the equipment specifications. In FIG. 4, the overall heat transfer coefficient is calculated based on the assumption that all the actual transfer surfaces contribute to heat exchange. From the experiment, a reasonable correlation was obtained that the overall heat transfer coefficient increased with an increase in the flow velocity at the inlet of the heat transfer tube, but the capacity evaluation was much smaller than the correlation calculated by HTFS. The result was. When the linear velocity was in the range of 1.0 m / sec or more, the difference between the two was reduced. The difference between the two is a stain coefficient of 0.0005 to 0.001.
The value was equivalent to 5 kcal / m 2 h ° C., and the absolute value and the variation could not be explained from the equipment status.
【００１４】実験結果の中から伝熱管長３ｍ、本数８０
本の凝縮器を用いた場合を例に一条件について上記に示
した「下向きの流れの阻害された伝熱管」の本数を推算
した結果を以下に示す。即ち、実験結果から正常な伝熱
管内の平均ガス密度ρｇ１は、凝縮器入口ガス組成、及
び入出口での温度指示から、６５．３ｋｇ／ｍ3 と計算
され、一方、流れの阻害された伝熱管内の平均ガス密度
ρｇ１は、該ガスが冷却水温度まで冷却、凝縮されてい
ると仮定して、４９．４ｋｇ／ｍ3 と計算される。両ガ
スが伝熱管下部に与えるヘッド差は、 （６５．３−４９．４）×３＝４８ｋｇ／ｍ2 と算出される。従って、正常な流通にある伝熱管での動
圧力損失が、４８ｋｇ／ｍ2 になるように除熱に寄与し
ている伝熱管が定まり、全８０本中５４本という計算結
果となった。From the experimental results, the heat transfer tube length was 3 m and the number of tubes was 80.
The result of estimating the number of “heat transfer tubes in which the downward flow is inhibited” shown above under one condition using a condenser as an example is shown below. That is, from the experimental results, the average gas density ρg1 in the normal heat transfer tube was calculated to be 65.3 kg / m 3 from the gas composition at the inlet of the condenser and the temperature indication at the inlet and outlet. The average gas density ρg1 in the heat pipe is calculated to be 49.4 kg / m 3 , assuming that the gas has been cooled and condensed to the cooling water temperature. The head difference that both gases give to the lower part of the heat transfer tube is calculated as (65.3-49.4) × 3 = 48 kg / m 2 . Therefore, the heat transfer tubes contributing to heat removal were determined so that the dynamic pressure loss in the heat transfer tubes in normal circulation was 48 kg / m 2 , and the calculation result was 54 tubes out of 80 tubes in total.
【００１５】即ち、式 ΔＰｓ＝（ρｇ１−ρｇ２）×Ｈ の右辺は上記したように４８ｋｇ／ｍ2 である。一方、
左辺の圧力損失は、Ｆａｎｎｉｎｇ式により計算でき
る。 ΔＰｓ＝（４ｆ）（Ｌ／Ｄ）（ｕ2 ／２ｇｃ）ρ ｆ；Ｆａｎｎｉｎｇの流体摩擦係数 Ｌ；その間の距離 Ｄ；管の内径 ｇｃ；重力換算係数 ｕ；断面平均速度 ρ；流体密度That is, the right side of the equation ΔPs = (ρg1-ρg2) × H is 48 kg / m 2 as described above. on the other hand,
The pressure loss on the left side can be calculated by the Fanning equation. ΔPs = (4f) (L / D) (u 2 / 2gc) ρ f; Fluid friction coefficient of Fanning L; distance between them D; inner diameter of pipe gc; gravity conversion coefficient u; average sectional velocity ρ; fluid density
【００１６】このように、Ｆａｎｎｉｎｇ式により圧力
損失は算出できるが、実際の伝熱管内部は流体が下方に
進むに従って、温度変化に伴い、プロピレンの凝縮が進
み、流体の線速、ガス密度等が高さ位置により異なる
為、手計算はかなり煩雑となる。従って、今回はＨＴＦ
Ｓにより圧力損失を計算した。該ソフトウェアは凝縮器
内部を高さ方向に分割し（分割数等詳細の計算方法は不
明）、各々の部分での圧力損失を計算し、トータルの圧
力損失を容易に算出する事ができる。As described above, the pressure loss can be calculated by the Fanning equation. However, as the fluid proceeds downward in the actual heat transfer tube, the propylene condenses as the temperature changes, and the linear velocity of the fluid, gas density, etc. Since the calculation differs depending on the height position, the manual calculation becomes considerably complicated. Therefore, this time HTF
The pressure loss was calculated by S. The software divides the inside of the condenser in the height direction (the calculation method of details such as the number of divisions is unknown), calculates the pressure loss at each part, and can easily calculate the total pressure loss.
【００１７】ここでは、伝熱管本数を８０（全数）〜４
０本に振り圧力損失をＨＴＦＳにて算出した。結果は以
下の通り。 ────────────── 本 数 圧力損失 （本） (kg/m2) ────────────── ８０ ２４ ７０ ３０ ６０ ４０ ５０ ５３ ４０ ７７ ──────────────Here, the number of heat transfer tubes is set to 80 (total number) to 4
The pressure loss was calculated by HTFS. The results are as follows. ────────────── Number Pressure loss (pcs) (kg / m 2 ) ────────────── 80 24 70 30 60 40 50 50 53 40 77 ──────────────
【００１８】従って、右辺と等しい圧力損失（４８ｋｇ
／ｍ2 ）は５４本となる。一方、動圧力損失を実測する
と５１ｋｇ／ｍ2 であり、両者はかなり良く一致した。
また、全伝熱管に均等にガスが流通していると仮定した
場合の動圧力損失は２３ｋｇ／ｍ2 と計算され、実測値
とは掛け離れた値となる。以上より本発明が有効なこと
が理解される。Therefore, the pressure loss equal to the right side (48 kg
/ M 2 ) is 54 lines. On the other hand, when the dynamic pressure loss was actually measured, it was 51 kg / m 2 , and both values agreed well.
The dynamic pressure loss is calculated to be 23 kg / m 2 , assuming that the gas is uniformly distributed in all the heat transfer tubes, and is a value far from the actually measured value. From the above, it is understood that the present invention is effective.
【００１９】同様の方法により各実験条件の有効な伝熱
管本数を算出し、その伝熱面積から総括伝熱係数を算出
し、それとＨＴＦＳが算出するそれとの比較結果を図５
に示す。妥当な汚れ係数値０．０００２ｋｃａｌ／ｍ2
ｈ℃付近で、両者はデータの振れはあるもののかなり良
く一致を示した。この結果は非凝縮ガスを含む系におい
ては、伝熱管の線速が低い場合には流れの阻害される伝
熱管が発生していることを示している。In the same manner, the effective number of heat transfer tubes under each experimental condition was calculated, the overall heat transfer coefficient was calculated from the heat transfer area, and the results of comparison with those calculated by HTFS are shown in FIG.
Shown in Reasonable dirt coefficient value 0.0002 kcal / m 2
Around h ° C., the two showed good agreement with each other, although the data fluctuated. This result indicates that, in the system containing the non-condensable gas, when the linear velocity of the heat transfer tube is low, a heat transfer tube whose flow is inhibited is generated.
【００２０】換言すれば、ＨＴＦＳ等の機器設計ツール
と、伝熱管内の線速が低い場合は、正常に流通する伝熱
管本数はその管内での動圧力損失ΔＰｓが、正常な流通
のある伝熱管と下向きの流れの阻害された伝熱管のガス
ヘッド差と等しくなるように定まっているという推論を
組み合わせることにより、より正確な凝縮器の設計が可
能となることを示すものである。In other words, when the equipment design tool such as HTFS and the linear velocity in the heat transfer pipe are low, the number of heat transfer pipes that normally flow is determined by the dynamic pressure loss ΔPs in the pipe and the heat transfer pipe with normal flow. It is shown that the combination of the inference that the gas head difference between the heat tube and the heat transfer tube in which the downward flow is obstructed is determined to be equal allows a more accurate condenser design.
【００２１】[0021]
【発明の効果】本発明の方法によれば、従来の機器設計
ツールだけでは成し得なかった、非凝縮ガスが含まれた
系での凝縮器における適切な伝熱管内線速の算出、適切
な循環ガスブロアーの選定、及び凝縮器の設計が可能と
なる。この結果、本発明は、良好な流動性を有するα−
オレフィンを主成分とするα−オレフィンの重合体の低
コストでの製造を可能とするものであり、その工業的価
値は大きいものがある。且つ、この方法は一般的な非凝
縮ガスを含む、冷却系システムにも適用でき、より正確
な機器設計及び解析に役立つものと考えられる。According to the method of the present invention, calculation of an appropriate linear velocity in a heat transfer tube in a condenser in a system containing non-condensable gas, which cannot be performed only by a conventional equipment design tool, The selection of the circulating gas blower and the design of the condenser become possible. As a result, the present invention provides α-
It enables low-cost production of a polymer of α-olefin containing olefin as a main component, and its industrial value is large. In addition, this method can be applied to a cooling system including general non-condensable gas, and is considered to be useful for more accurate equipment design and analysis.
【図１】本発明を適用するα−オレフィンの重合装置の
１例を示す説明図である。FIG. 1 is an explanatory view showing one example of an α-olefin polymerization apparatus to which the present invention is applied.
【図２】凝縮器内の模式図を示す。FIG. 2 shows a schematic diagram inside the condenser.
【図３】本発明を実験する為に用いたパイロット設備を
示す図である。FIG. 3 is a diagram showing a pilot facility used to test the present invention.
【図４】本発明の実験結果とＨＴＦＳ計算結果による総
括伝熱係数比較結果を示すグラフである。FIG. 4 is a graph showing overall heat transfer coefficient comparison results based on experimental results and HTFS calculation results of the present invention.
【図５】図４の比較結果を本発明に基づき、換算した結
果を示すグラフである。FIG. 5 is a graph showing a result obtained by converting the comparison result of FIG. 4 based on the present invention.
１ 重合槽 ２ 凝縮器 ３ 気液分離ドラム ４ ブロアー ５ 原料 ６ α−オレフィン重合体他 ７ プロピレン−水素混合ドラム ８ 蒸発器 ９ ポンプ １０ 温度計 １１ 圧力計 １２ 差圧計 １３ プロセスガスクロ計 DESCRIPTION OF SYMBOLS 1 Polymerization tank 2 Condenser 3 Gas-liquid separation drum 4 Blower 5 Raw material 6 Alpha-olefin polymer etc. 7 Propylene-hydrogen mixing drum 8 Evaporator 9 Pump 10 Thermometer 11 Pressure gauge 12 Differential pressure gauge 13 Process gas chromameter
───────────────────────────────────────────────────── フロントページの続き (72)発明者 小原 聡 岡山県倉敷市潮通３丁目10番地 三菱化学 株式会社水島事業所内 (72)発明者 渡邊 文尚 三重県四日市市東邦町１番地 三菱化学株 式会社四日市事業所内 (72)発明者 山本 禎宏 岡山県倉敷市潮通３丁目10番地 三菱化学 株式会社水島事業所内 Ｆターム(参考） 4D076 AA13 AA15 AA22 BC02 BC25 BC27 CD32 EA09Y EA12X EA13X EA14X EA14Y EA16Y EA16Z EA20X EA36 FA02 FA13 FA33 FA37 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Satoshi Ohara 3-10, Ushidori, Kurashiki-shi, Okayama Mitsubishi Chemical Co., Ltd. Mizushima Office (72) Inventor Fumitaka Watanabe 1 Toho-cho, Yokkaichi-shi, Mie Mitsubishi Chemical Corporation (72) Inventor Yoshihiro Yamamoto 3-10-10 Ushidori, Kurashiki City, Okayama Prefecture Mitsubishi Chemical Corporation Mizushima Office F-term (reference) 4D076 AA13 AA15 AA22 BC02 BC25 BC27 CD32 EA09Y EA12X EA13X EA14X EA14Y EA16Y EAZ EA20X EA36 FA02 FA13 FA33 FA37
Claims (4)
伝熱管束が、上下１対の水平隔板の間に設置されてお
り、被凝縮流体が上記伝熱管内の上部から下部に向かっ
て流通させられ、一方冷却媒体が上記一対の水平隔板の
間に流され、上記伝熱管の外周面に接触しつつ流動する
構造を有する縦型の多管式の凝縮器を用いて被凝縮流体
を冷却して凝縮液化させる方法において、被凝縮流体が
非凝縮成分を含有し、且つ該伝熱管における被凝縮流体
の線速を１．０〜４．０ｍ／ｓｅｃの範囲で運転するこ
とを特徴とする凝縮器による被凝縮流体の冷却方法。1. A heat transfer tube bundle comprising a substantially vertical straight tube heat transfer tube is provided between a pair of upper and lower horizontal partition plates, and a condensed fluid flows from an upper portion to a lower portion in the heat transfer tube. The cooling medium is flowed between the pair of horizontal plates, and is cooled using a vertical multi-tube condenser having a structure in which the cooling medium flows while contacting the outer peripheral surface of the heat transfer tube. In the method for condensing and liquefying a condensed fluid, the condensed fluid contains a non-condensed component, and the linear velocity of the condensed fluid in the heat transfer tube is in the range of 1.0 to 4.0 m / sec. A method for cooling a fluid to be condensed by a condenser.
じたα−オレフィンと水素を含有する未凝縮ガスである
請求項１に記載の被凝縮流体の冷却方法。2. The method for cooling a fluid to be condensed according to claim 1, wherein the fluid to be condensed is an uncondensed gas containing α-olefin produced by polymerization of α-olefin and hydrogen.
で生じたα−オレフィンと水素を含有する未凝縮ガスで
あり、これを凝縮器で凝縮液化させ、非凝縮ガスを昇圧
して重合反応器へ循環する請求項１に記載の被凝縮流体
の冷却方法。3. The condensed fluid is an uncondensed gas containing an α-olefin and hydrogen generated by a polymerization reaction of an α-olefin, which is condensed and liquefied in a condenser, and the non-condensed gas is pressurized to increase the polymerization reaction. The method for cooling a fluid to be condensed according to claim 1 circulating in a vessel.
で生じたα−オレフィンと水素を含有する未凝縮ガスで
あり、これを凝縮器で凝縮液化させ、非凝縮ガスを昇圧
後その一部を凝縮器に循環し、残部を重合反応器へ循環
する請求項１に記載の被凝縮流体の冷却方法。4. A fluid to be condensed is an uncondensed gas containing an α-olefin and hydrogen generated by a polymerization reaction of an α-olefin, which is condensed and liquefied by a condenser, and a non-condensed gas is partially pressurized after being pressurized. The method for cooling a condensed fluid according to claim 1, wherein the water is circulated to a condenser, and the remainder is circulated to a polymerization reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30954698A JP2000117001A (en) | 1998-10-16 | 1998-10-16 | Cooling method of fluid to be condensed by condenser |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30954698A JP2000117001A (en) | 1998-10-16 | 1998-10-16 | Cooling method of fluid to be condensed by condenser |
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| Publication Number | Publication Date |
|---|---|
| JP2000117001A true JP2000117001A (en) | 2000-04-25 |
Family
ID=17994326
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP30954698A Pending JP2000117001A (en) | 1998-10-16 | 1998-10-16 | Cooling method of fluid to be condensed by condenser |
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| Country | Link |
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| JP (1) | JP2000117001A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2015189740A (en) * | 2014-03-28 | 2015-11-02 | 三菱化学株式会社 | Method for producing α-olefin low polymer |
| JP2017066130A (en) * | 2015-09-28 | 2017-04-06 | 三菱化学株式会社 | METHOD AND APPARATUS FOR PRODUCING α-OLEFIN LOW POLYMER |
| JP2017122516A (en) * | 2016-01-05 | 2017-07-13 | 株式会社あい・あいエナジーアソシエイツ | Evaporation type cooler |
-
1998
- 1998-10-16 JP JP30954698A patent/JP2000117001A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2015189740A (en) * | 2014-03-28 | 2015-11-02 | 三菱化学株式会社 | Method for producing α-olefin low polymer |
| JP2017066130A (en) * | 2015-09-28 | 2017-04-06 | 三菱化学株式会社 | METHOD AND APPARATUS FOR PRODUCING α-OLEFIN LOW POLYMER |
| KR20180062972A (en) * | 2015-09-28 | 2018-06-11 | 미쯔비시 케미컬 주식회사 | Method and device for manufacturing α-olefin oligomer |
| KR102661572B1 (en) * | 2015-09-28 | 2024-04-26 | 미쯔비시 케미컬 주식회사 | Method and device for manufacturing α-olefin oligomer |
| JP2017122516A (en) * | 2016-01-05 | 2017-07-13 | 株式会社あい・あいエナジーアソシエイツ | Evaporation type cooler |
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