ベント配管6の付着物の生成を抑制する方法の2つ目として、ベント配管洗浄液投入口9及びベント配管洗浄液排出口10を設けベント配管洗浄液を流すことも有効である。ベント配管6の内壁で凝縮した揮発物の凝縮液が、乾燥して熱硬化する前に、ベント配管洗浄液を流すことによって、付着物の生成を防止できる。ベント配管洗浄液は連続的に流しても断続的に流しても良く、断続的に流す場合でも流すタイミングは如何なるタイミングでも良いが、タンクがバッチ処理を行うタンクである場合は、バッチ処理が終了しタンク内の処理液2を次工程に移送した直後であることが好ましい。好ましくは30分以内、より好ましくは10分以内、更に好ましくは5分以内である。ベント配管洗浄液もベント配管冷却用冷媒と同じ理由で、処理液2の温度よりも低く、より好ましくは10℃以上低く設定することが良い。なお、図1は、ベント配管6を冷却するジャケット8と、ベント配管6を洗浄するためのベント配管洗浄液投入口9とベント配管洗浄液排出口10が設けられたタンクを示す。
As a second method of suppressing the formation of the deposit on the vent pipe 6, it is also effective to provide the vent pipe cleaning liquid inlet 9 and the vent pipe cleaning liquid outlet 10 and to flow the vent pipe cleaning liquid. By flowing the cleaning solution for the vent pipe before the condensate of the volatile matter condensed on the inner wall of the vent pipe 6 is dried and thermally cured, it is possible to prevent the generation of the deposit. The vent pipe cleaning liquid may be flowed continuously or intermittently, and may be flowed at any timing even if it is flowed intermittently, but if the tank is a tank for batch processing, batch processing is completed. It is preferable that the treatment liquid 2 in the tank be transferred immediately to the next step. Preferably it is within 30 minutes, more preferably within 10 minutes, still more preferably within 5 minutes. It is preferable to set the temperature of the treatment solution 2 lower than the temperature of the treatment liquid 2 and more preferably 10 ° C. or more lower than the temperature of the treatment liquid 2 for the same reason as that of the cooling fluid for cooling the vent pipe. Incidentally, FIG. 1, a jacket 8 for cooling the vent pipe 6 shows the tank vent pipe cleaning liquid inlet 9 and the vent pipe cleaning liquid discharge port 10 is provided for cleaning the vent pipe 6.
下記、一連の工程は実施例1〜11及び比較例1、2の全てに共通である。
(着色剤分散工程)
トナー製造用タンクA1に、スチレンモノマーを100質量部、荷電制御剤であるジ‐t‐ブチルサリチル酸金属化合物を2質量部、着色剤であるC.I.ピグメントブルー15:3を10質量部投入し、20℃にて強攪拌し処理液A1を得た。
(樹脂溶解工程)
トナー製造用タンクA2に、スチレンモノマーを40質量部、n−ブチルアクリレートを30質量部、極性レジンである飽和ポリエステル(酸価10mgKOH/g、ピーク分子量;8500)を15質量部投入し、30℃で通常攪拌し処理液A2を得た。
(開始剤溶解工程)
トナー製造用タンクA3に、スチレンモノマーを30質量部、重合開始剤である2,2'−アゾビス(2,4−ジメチルバレロニトリル)を8質量部投入し、30℃にて通常攪拌し処理液A3を得た。
(離型剤溶解工程)
トナー製造用タンクA4に、処理液A1、処理液A2、処理液A3、離型剤であるワックス(融点65℃)を40質量部投入し、60℃にて通常攪拌して重合性単量体組成物である処理液A4を得た。
(造粒工程)
トナー製造用タンクBに、イオン交換水を700質量部、0.1M−Na3PO4水溶液を450質量部投入し、60℃に加温した後、クレアミックスCLS−30S(エム・テクニック社製)を用いて、4500rpmで撹拌した。これに1.0M−CaCl2水溶液68質量部を徐々に添加し、リン酸カルシウム塩を含む水系媒体を得た。
The following series of steps are common to all of Examples 1 to 11 and Comparative Examples 1 and 2.
(Colorant dispersion process)
100 parts by mass of a styrene monomer, 2 parts by mass of a metal compound of di-t-butylsalicylic acid as a charge control agent, and 2 parts by mass of a colorant, C.I. I. 10 parts by mass of pigment blue 15: 3 was added, and the mixture was vigorously stirred at 20 ° C. to obtain a treatment solution A1.
(Resin dissolution process)
40 parts by mass of styrene monomer, 30 parts by mass of n-butyl acrylate, and 15 parts by mass of saturated polyester (acid value 10 mg KOH / g, peak molecular weight; 8500) are charged into a toner production tank A2 at 30 ° C. The reaction solution A2 was obtained by stirring normally.
(Initiator dissolution process)
30 parts by mass of styrene monomer and 8 parts by mass of 2,2′-azobis (2,4-dimethylvaleronitrile) as a polymerization initiator are charged into a tank A3 for toner production, and the processing liquid is usually stirred at 30 ° C. I got A3.
(Mold release agent dissolution process)
40 parts by mass of a processing solution A1, a processing solution A2, a processing solution A3 and a wax (melting point 65 ° C.) which is a releasing agent are charged into a toner production tank A4, and the polymerizable monomer is usually stirred at 60 ° C. The processing liquid A4 which is a composition was obtained.
(Granulation process)
700 parts by mass of ion-exchanged water and 450 parts by mass of 0.1 M Na 3 PO 4 aqueous solution are charged into a tank B for toner production, heated to 60 ° C., Clairemix CLS-30S (manufactured by M. Tech. Co., Ltd.) The solution was stirred at 4500 rpm using To this was gradually added 68 parts by mass of a 1.0 M CaCl 2 aqueous solution to obtain an aqueous medium containing a calcium phosphate.