JP2012086145A5

JP2012086145A5 -

Info

Publication number: JP2012086145A5
Application number: JP2010234730A
Authority: JP
Filing date: 2010-10-19
Publication date: 2013-12-05
Anticipated expiration: 2030-10-19

Description

図１の噴霧プロセスを例とした場合の、ＣＯ_２供給圧力Ｐ−１、溶液供給圧力Ｐ−２、プロセス圧力Ｐ−４の関係について、図３に示す。高粘度有機性流体の粘度が高い場合は、ＣＯ_２との粘度差が大きくなるため、ミキサーの混合性能によって、プロセス圧力の変動は大きく影響を受ける。図３に示すように、プロセス圧力が変動した場合、高粘度である溶液供給圧力は、容易に変動に追従するが、ＣＯ_２は低流量であり、かつ一定温度で圧力に対する密度変化量が大きいため、昇圧に時間を要する。例えば、３５℃の条件で、１２ＭＰａから１４ＭＰａにプロセス圧力が変動した場合について、有機性流体をトルエンとして、ＣＯ_２との昇圧速度について、比較を行った。 FIG. 3 shows the relationship between the CO ₂ supply pressure P - 1, the solution supply pressure P - 2, and the process pressure P - 4 when the spray process of FIG. 1 is taken as an example. When the viscosity of the high-viscosity organic fluid is high, the difference in viscosity from CO ₂ becomes large. Therefore, the process pressure fluctuation is greatly affected by the mixing performance of the mixer. As shown in FIG. 3, when the process pressure fluctuates, the solution supply pressure having a high viscosity easily follows the fluctuation, but CO ₂ has a low flow rate and a large amount of density change with respect to the pressure at a constant temperature. Therefore, it takes time to boost the voltage. For example, when the process pressure fluctuated from 12 MPa to 14 MPa under the condition of 35 ° C., the organic fluid was toluene and the pressure increase rate with CO ₂ was compared.

このような現象を生じることにより、混合器以降の流体は、ＣＯ_２を溶解している領域と、ＣＯ_２を溶解していない領域が、間欠的に形成され、プロセス圧力Ｐ−４は、変動し、噴霧状態は不安定となる。そこで、本発明では、このような現象を回避するために、以下のような構成を採用することで、高圧二酸化炭素の断続的な供給を抑制し、その供給流量を安定化させる新しい技術を確立した。 By causing such a phenomenon, in the fluid after the mixer, a region in which CO ₂ is dissolved and a region in which CO ₂ is not dissolved are formed intermittently, and the process pressure P - 4 varies. However, the spray state becomes unstable. Therefore, in the present invention, in order to avoid such a phenomenon, a new technique for suppressing intermittent supply of high-pressure carbon dioxide and stabilizing the supply flow rate by adopting the following configuration is established. did.

図５に、既存法による二酸化炭素塗装装置の運転データを示す。図５に示すように、圧力上昇時に、混合後圧力Ｐ−４よりも、混合前ＣＯ_２圧力Ｐ−１の方が低い。この区間は、供給しているＣＯ_２は、昇圧に費やされ、混合器以降に流通していない。混合器流入前のＣＯ_２温度（ＣＯ_２背圧弁出口温度Ｔ−５）からも明らかなように、ＣＯ_２が昇圧に費やされ、混合器以降に流通していない区間では、ＣＯ_２加熱器で加熱されるはずのＣＯ_２温度上昇が抑制され、温度が低下していることが分かる。その際、ＣＯ_２が溶解していない高粘度流体が流れるため、圧力損失が大きくなり、混合後の塗料粘度を測定している差圧データは上昇する。また、ＣＯ_２が流通すると、粘度が低下するため、差圧も低下している。 In FIG. 5, the operation data of the carbon dioxide coating apparatus by the existing method are shown. As shown in FIG. 5, the pre-mixing CO ₂ pressure P- 1 is lower than the post-mixing pressure P- 4 when the pressure rises. In this section, the supplied CO ₂ is consumed for boosting and is not distributed after the mixer. As is clear from the CO ₂ temperature before the mixer inflow (CO ₂ back pressure valve outlet temperature T-5), the CO ₂ heater is used in the section where CO ₂ is consumed for pressure increase and does not flow after the mixer. It can be seen that the increase in the temperature of CO ₂ that should be heated at is suppressed and the temperature is lowered. At that time, since a high-viscosity fluid in which CO ₂ is not dissolved flows, the pressure loss increases, and the differential pressure data for measuring the viscosity of the paint after mixing increases. Further, when CO ₂ flows, the viscosity decreases, so the differential pressure also decreases.

一方、図６に、本発明による二酸化炭素塗装装置の運転データを示す。混合前のＣＯ_２ラインに背圧弁を設けることにより、混合前ＣＯ_２圧力Ｐ−１は、混合部圧力Ｐ−４よりも高圧で、一定制御されている。ＣＯ_２温度Ｔ−５についても、一定温度を示し、安定して連続供給されていることが分かる。その結果、混合後塗料の粘度を示す差圧データが、既存法で見られたような大きな変動は生じていない。従って、混合後流体の性状は、安定化されたことが分かる。本実施例により、プロセス圧力の変動は生じなくなり、非常に安定した高圧プロセス操作が実現された。 On the other hand, FIG. 6 shows operation data of the carbon dioxide coating apparatus according to the present invention. By providing a back pressure valve in the CO ₂ line before mixing, the CO ₂ pressure P- 1 before mixing is higher than the mixing section pressure P- 4 and is controlled constantly. It can be seen that the CO ₂ temperature T-5 also shows a constant temperature and is stably supplied continuously. As a result, the pressure difference data indicating the viscosity of the paint after mixing does not change as much as that found in the existing method. Therefore, it can be seen that the properties of the fluid after mixing are stabilized. According to this example, the process pressure was not changed, and a very stable high-pressure process operation was realized.

Claims

A continuous mixing apparatus for continuously mixing a high-viscosity organic fluid containing a paint or a molten resin and high-pressure carbon dioxide in a high-pressure process,
A high-viscosity organic fluid supply line for continuously supplying the high-viscosity organic fluid;
A high-pressure carbon dioxide supply line for continuously supplying the high-pressure carbon dioxide,
A high-pressure mixing section for mixing the high-viscosity organic fluid and the high-pressure carbon dioxide;
A primary pressure control valve (PCV-2) for high-pressure carbon dioxide provided in the high-pressure carbon dioxide supply line in the vicinity of the high-pressure mixing unit;
Comprising
The continuous mixing apparatus, wherein the set pressure of the primary pressure control valve is 1 to 5 MPa higher than the pressure in the high pressure mixing section.

The continuous mixing apparatus according to claim 1, further comprising a mechanism for providing a pressure loss, which is provided downstream of the primary pressure control valve.

The continuous mixing apparatus according to claim 2, wherein the mechanism that imparts the pressure loss is a metering needle valve or a capillary tube.

Any one of Claims 1-3 further equipped with the secondary pressure control valve (PCV-4) for the high-viscosity organic fluid provided in the said high-viscosity organic-fluid supply line in the vicinity of the said mixing part. The continuous mixing apparatus of Claim 1.

The continuous mixing apparatus according to claim 4, further comprising a relief valve provided upstream of the secondary pressure regulating valve (PCV-4) for the high viscosity organic fluid.

6. The apparatus according to claim 1, further comprising a primary pressure regulating valve (PCV-3) that is provided downstream of the high-pressure mixing unit and controls the pressure of the fluid after mixing to be constant. Continuous mixing equipment.

The continuous mixing apparatus according to any one of claims 1 to 6, wherein the high-pressure mixing unit is a high-pressure micromixer using a microchannel.

The continuous mixing apparatus according to claim 7, wherein the high-pressure micromixer is a multistage division type high-pressure micromixer, a center collision micromixer, a T-shaped micromixer, or a swirl mixer.

A method of continuously mixing a high-viscosity organic fluid containing a paint or a molten resin and high-pressure carbon dioxide in a high-pressure process using the continuous mixing apparatus according to any one of claims 1 to 8. ,
Supply high viscosity organic fluid from high viscosity organic fluid source to high viscosity organic fluid supply line,
High-pressure carbon dioxide is supplied from a high-pressure carbon dioxide source to the high-pressure carbon dioxide supply line at a pressure lower than the set pressure P1, which is the maximum discharge pressure of the high-pressure carbon dioxide pump. Is controlled to the set pressure P2 of the primary pressure control valve (PCV-2),
In the high-pressure mixing section, the high-viscosity organic fluid and high-pressure carbon dioxide are mixed,
The set pressure P2 is set to be 1 to 5 MPa higher than the pressure in the mixing section, and is a continuous mixing method that stabilizes the supply flow rate of high-pressure carbon dioxide and suppresses fluctuations in process pressure.

10. The continuous mixing method according to claim 9, wherein the pressure in the high-pressure mixing unit is controlled to a set pressure P <b> 4 of a secondary pressure regulating valve (PCV-4) for a high-viscosity organic fluid.

When the supply flow rate of high-pressure carbon dioxide is low, a pressure loss is applied downstream of the primary pressure control valve (PCV-2) for high-pressure carbon dioxide, and the primary pressure control valve (PCV for high-pressure carbon dioxide). The continuous mixing method according to claim 9 or 10, wherein the controllability of -2) is improved.

The continuous mixing method according to any one of claims 9 to 11, wherein an increase in discharge pressure of the high-pressure pump in the high-viscosity organic fluid supply line is avoided by a Lily valve.

The continuous mixing method according to claim 9, wherein the fluid after mixing is discharged from a spray nozzle, and the high-viscosity organic fluid is continuously sprayed, continuously formed, or continuously atomized from a high-pressure environment.